CN102559256A

CN102559256A - Combination method of hydrogenised aromatic hydrocarbon partial saturation of coal-liquefied oil

Info

Publication number: CN102559256A
Application number: CN2011103375621A
Authority: CN
Inventors: 何巨堂
Original assignee: Individual
Current assignee: Individual
Priority date: 2011-10-16
Filing date: 2011-10-16
Publication date: 2012-07-11

Abstract

The invention relates to a combination method of hydrogenised aromatic hydrocarbon partial saturation of coal-liquefied oil. The combination method can effectively improve consistence of effective hydrogen donor elements of hydrogen donor solvent oil during coal liquefying reaction by the following steps of: separating the coal-liquefied oil to realizing relative separation of bicyclic structure aromatic hydrocarbon and polycyclic structure aromatic hydrocarbon or the relative separation of tricyclic structure aromatic hydrocarbon and tetracyclic or more structure aromatic hydrocarbon to obtain light distillate and heavy distillate, carrying out a hydrogenised aromatic hydrocarbon partial saturation reaction by selecting self optimal reaction conditions (catalyst formula, catalyst airspeed, reaction temperature and the like) of the light distillate and the heavy distillate, and carrying out combined separation on effluents of an aromatic hydrocarbon hydrogenization saturation reaction. The combination method disclosed by the invention further has effects of stable operation and increased operation safety of devices.

Description

A kind of hydrogenation aromatic hydrocarbons fractional saturation combined method of liquefied coal coil

Technical field

The present invention relates to a kind of hydrogenation aromatic hydrocarbons fractional saturation combined method of liquefied coal coil, be used for improving the content of hydrogenation saturated oil fractional saturation aromatic component; Say especially; The present invention relates to a kind of liquefied coal coil and produce hydrogen supply dissolvent oil classification hydrogenation saturation process: twin nuclei aromatic hydrocarbons and polynuclear plane aromatic hydrocarbons relative separation or tricyclic structure aromatic hydrocarbons and Fourth Ring and isolating benzoline of above structure aromatic hydrocarbons relative separation and heavy distillate; Select separately The optimum reaction conditions (catalyst formulation, catalyzer air speed, temperature of reaction etc.) to carry out the reaction of aromatic hydrogenation fractional saturation, aromatic hydrogenation saturated reaction elute combined separation.

Background technology

As its name suggests, in the gelatin liquefaction reaction process, the major function of hydrogen supply dissolvent oil is a hydrogen supply; The dicyclo of fractional saturation or polycyclic aromatic hydrocarbons all have hydrogen supply capacity, belong to effective hydrogen donor component, like naphthane and 1; The 4-dihydronaphthalene; And perhydronaphthalene is because Stability Analysis of Structures, though hydrogeneous at most, hydrogen supply capacity is very poor.

The hydrogen supply speed of dihydro body is all greater than the tetrahydrochysene body, and the dihydro body of thrcylic aromatic hydrocarbon and the dihydro body of double ring arene are compared, and it is low that its hydrogen supply speed has height to have; Test verifiedly,, the ability of transmitting hydrogen is arranged though polycyclic aromatic hydrocarbons does not have hydrogen supply capacity;

Naphthalene 1,4-dihydronaphthalene naphthane perhydronaphthalene

In the time of 400 ℃, the relative hydrogen supply speed of following solvent is following:

After the gelatin liquefaction reaction process works well; Hydrogen supply dissolvent oil adopts the hydrogenation modification oil of the self-produced liquefied coal coil (being generally the distillate that conventional boiling range is higher than 165 ℃) of gelatin liquefaction reaction process usually; The major objective of liquefied coal coil hydrogenation modification process is that production gelatin liquefaction reaction process is used solvent oil; Its main purpose is to improve the content of " effectively hydrogen donor component " in the oil product; Such as improving naphthenic base benzene class, bicyclic alkyl benzene class components contents; Contain a large amount of twin nuclei aromatic hydrocarbons, tricyclic structure aromatic hydrocarbons and Fourth Ring and above this fact of structure aromatic hydrocarbons thereof based on liquefied coal coil, liquefied coal coil hydrogenation modification process is an incomplete saturation history of aromatic hydrogenation aromatic hydrogenation appropriateness saturation history in other words conj.or perhaps.

Direct hydrogenation liquefaction of coal process according to the invention; Refer in the presence of solvent oil the method that makes gelatin liquefaction through coal hydrogenation; Difference according to the different and processing condition of different, the pyrolysis way of solvent oil and catalyzer and hydrogenation mode can be divided into following several kinds of technologies:

1. dissolve the pyrolysis liquefaction process: utilize heavy solvent can make low-ash extract (Japan claims the swelling charcoal) to the coal cracking extracting; Utilizing the extracting under super critical condition of lightweight solvent can obtain with the BO is main oils.This method is without hydrogen, though preceding a kind of process yield height product still is a solid, a kind of technology in back such as supercritical extraction (extraction) method (SCE) extract content are not too high;

2. solvent hydrogenation extracting liquefaction process: if any solvent refined coal process 1 and II (SRC-1 and SRC-II), Exxon donor solvent process EDS, Japanese New Energy Development Organization liquefaction process (NEDOL) etc. use hydrogen, but pressure are not too high, and solvent oil has tangible effect;

3. high pressure shortening method: all belong to this type like the old and new's liquefaction process (IG and NewlG) of Germany and the H-coal process (H-Coal) of the U.S. etc.;

4. coal and residual oil are united processing method (COprocessing): with residual oil is that solvent oil is with coal single pass reactor drum, without turning oil.Hydrocracking takes place and is converted into lightweight oil in residual oil simultaneously.The technology that the U.S., Canada, Germany and the FSU etc. have nothing in common with each other;

5. underground liquefaction process: solvent is injected subterranean coal, make coal depolymerization and dissolving, it is diffusing to add that the fluidic surging force collapses coal, and not consoluet coal then is suspended in the solvent, solution is extracted out and separation processing with pump;

6. a kind of thermally dissolving and catalytic method of producing liquid fuel with brown coal of stating clearly of patent CN100547055C.

Which kind of DCL/Direct coal liquefaction process no matter; Its target all is to obtain oil product, and the function of pursuit all is " coal changes oil ", and the chemical transformation that must exist is " coal hydrogenation "; This type of technological common trait is to use solvent oil and catalyzer at present; It is 200～400 ℃ that the conventional boiling range of solvent oil is generally 200～450 ℃, majority, and the solvent oil majority is a distilled oil, and contained aromatic hydrocarbons majority is the aromatic hydrocarbons of 2～4 ring structures.

Gelatin liquefaction reaction process according to the invention; Referring to coal is raw material with the molecule hydrogen that possibly exist; With specific oil product (being generally the hydrogenation modification oil of liquefied coal coil) is hydrogen supply dissolvent oil; Under certain operational condition (like service temperature, working pressure, solvent oil/coal weight ratio, hydrogen/solvent oil volume ratio and suitable hydrogenation catalyst), the reaction process of carbon-carbon bond thermally splitting, hydrogenation liquefaction directly takes place in coal.

Liquefied coal coil according to the invention refers to the oil product that said gelatin liquefaction reaction process produces, and it is present in the coal hydrogenation liquefaction reaction elute, is based on hydrogen supply dissolvent oil, reaction consumes coal and reaction and shifts the hydrocarbon ils product in the combined reaction product of hydrogen.

Patent CN100547055C states clearly, and a kind of to produce the thermally dissolving and catalytic of liquid fuel with brown coal owned by France in brown coal medium-pressure hydrocracking direct liquefaction process, comprises gelatin liquefaction reaction process and liquefied coal coil hydrogenation modification process totally two processes.For the transformation efficiency that improves coal direct liquefaction gets into the gelatin liquefaction reactor drum with the realization coal feedstock; Coal is processed coal dust before getting into the gelatin liquefaction reactor drum usually; Be made into coal oil mixture with the solvent oil that possesses good hydrogen supply capacity, coal oil mixture gets into the gelatin liquefaction reactor drum after pressurization, heating.

Typical brown coal are produced the liquefaction oil of the thermally dissolving and catalytic method of liquid fuel, the character of liquefaction light oil is seen table 1.The coal direct liquefaction oil light oil of gulf coal system oil process, the character of coal direct liquefaction oil heavy oil are seen table 2 in the Shenhua.

Table 1 brown coal coal system oil process oil property

Gulf coal system oil process oil property in table 2 Shenhua

The typical aromatic component of table 3 and contrast hydrogenate boiling point, condensation point and density summary sheet

Table 3 has been listed part aromatic component and contrast hydrogenate boiling point and the density data that occurs in the table 1; The boiling point, condensation point and the density that are used for comparative illustration typical case aromatic component; Be used for typical aromatic component and the variation that contrasts hydrogenate boiling point, condensation point and density simultaneously; With the listed character of table 1 be representative the brown coal thermally dissolving and catalytic method liquefaction oil of producing liquid fuel belong to high aromatic hydrocarbons high-density hydrocarbon ils; Normally comprising conventional boiling range is the high-density oil product that is rich in aromatic hydrocarbons of 165～450 ℃ of hydrocarbon components; With regard to its boiling range, in most cases contain two kinds or three kinds in petroleum naphtha fraction, fraction of diesel oil, the multiple cut of heavy fraction simultaneously, comprise 20～65% conventional boiling range usually and be the lighting end 1F that 265～450 ℃ last running 2F (being the high last running of polynuclear plane aromaticity content) and 20～65% conventional boiling range be 165～265 ℃ (be twin nuclei aromaticity content height and the low lighting end of polynuclear plane aromaticity content).The character of above-mentioned last running 2F and lighting end 1F (such as double ring arene content, polycyclic aromatic hydrocarbon content, nitrogen content, density, boiling point, hydrogen richness, viscosity, carbon residue content, metal content, oxygen level, sulphur content, cetane value) difference is very big; When double ring arene and polycyclic aromatic hydrocarbons carry out the saturated production hydrogen supply dissolvent oil of hydrogenation simultaneously; Because the difference of component molecular structure, best reaction mechanism, reaction pressure and TR, catalyzer configuration, hydrogen consumption, the cycle of operation, fractionation mode and quality product difference are very big.Produce the process of solvent oil for the small-scale liquefied coal coil, adopt conventional associating processing scheme (the different boiling ranges fraction mixes and processes), can simplify flow process, reduce construction investment.But produce the situation of diesel component for mass-producing reconstructed coal liquefaction oil; When a certain oil property is similar to the oil product of the listed character of table 1; It is very big that last running 2F and the conventional boiling range that based on conventional boiling range is 265～450 ℃ is that 165～265 ℃ lighting end 1F compares the size and the differences in shape of mean molecule; Thrcylic aromatic hydrocarbon is realized the saturated hydroconversion condition of aromatic hydrocarbons of appropriate depth; Then must form the saturated naphthenic base benzene that makes of excessive hydrogenation and be converted into dicyclo naphthenic hydrocarbon, reduce effective hydrogen donor component content and increase the hydrogen consumption double ring arene; The saturated hydroconversion condition of aromatic hydrocarbons to di pah realization appropriate depth then can not be converted into bicyclic alkyl benzene to thrcylic aromatic hydrocarbon degree of saturation deficiency, can not effectively improve effective hydrogen donor component content; Unite processing and exist following shortcoming:

1. because the only hydrocatalyst for saturating arylhydrocarbon prescription of the hydrogenation saturation history of the different aromatic hydrocarbons of number of rings is inevitable different; The catalyzer that associating processing can't be selected gently, last running is best separately; Can realize the hydrocatalyst for saturating arylhydrocarbon of last running 2F appropriate depth; Usually it is saturated to form the aromatic hydrocarbons excessive hydrogenation to the lighting end 1F of less carbon number, increases the hydrogen consumption, reduces " effectively hydrogen donor component " content, has increased the difficulty of selecting optimum catalyst;

The only temperature of reaction of the aromatic hydrogenation saturation history of 2. light under the uniform pressure, last running is inevitable different; Associating processing can't be selected gently, the last running service temperature of performance separately; As the aromatic hydrogenation of realizing last running 2F appropriate depth is saturated; Usually it is saturated to form the aromatic hydrocarbons excessive hydrogenation to the lighting end 1F of less carbon number, increases the hydrogen consumption, reduces " effectively hydrogen donor component " content;

3. since light when adopting identical hydrocatalyst for saturating arylhydrocarbon, last running the only time span of aromatic hydrogenation saturation history is inevitable different separately; Unite add can't realize simultaneously man-hour gently, reaction times that last running is best separately; Can realize the reaction times of the last running 2F suitable reactions degree of depth; Usually it is saturated to form the aromatic hydrocarbons excessive hydrogenation to the lighting end 1F of less carbon number, increases the hydrogen consumption, reduces " effectively hydrogen donor component " content;

4. under certain condition; When having had last running 2F and the lighting end 1F of relative separation, unite the mixing process that last running 2F and lighting end 1F have in fact been accomplished in processing, reduced the component concentrations value; Sacrifice the relative separation degree that has formed, will increase separating energy consumption;

5. lighting end 1F can carry out hydrogenation reaction down at lesser temps (as 320～380 ℃) and lower pressure (like 6.0～10.0MPa MPa); Last running 2F (could accomplish hydrogenation reaction as 10.0～18.0MPa) times at comparatively high temps (as 360～420 ℃) and elevated pressures; Therefore unite and add man-hour, have following production operation safety risk:

A, transform by expection in order to make raw material; Must promptly adopt the catalyzer of comparatively high temps, elevated pressures condition and greater activity according to last running 2F character coupling catalyzer and reaction conditions, and with this understanding; Lighting end 1F speed of reaction is too fast; Reaction heat gathers rapidly, causes the reactor bed temperature rise to be difficult to control even overtemperature;

B, in order to alleviate above-mentioned situation, need the compelled temperature of reaction that reduces, with the temperature rise of control bed; After temperature reduced, the reaction of lighting end was eased, but the reaction of a part of last running can be terminated; After temperature reduced, viscosity increased, mobile variation; Hinder flowing of lighting end and hydrogen, and heavy constituent rest on for a long time and can not participate in hydrogenation reaction in the hot environment, will condensation, coking; The blocking catalyst duct so forms vicious cycle, causes the beds pressure drop to be risen rapidly;

C, when serious overtemperature appears in beds, the compelled emergency decompression that starts its objective is rapid reduction reacting system pressure, stops or slows down hydrogenation reaction significantly; For the Hydrobon catalyst bed, last running 2F generally can reach the purpose that suppresses hydrogenation reaction speed significantly when pressure is lower than 9.0～10.0MPa, and the hydrogenation reaction of lighting end 1F just can receive inhibition significantly when pressure is lower than 6.0MPa; When start quick pressure releasing (such as blowdown rate be first minute 15 crust/minute) during system; Pressure is reduced to about 3～4 minutes clock times of 9.0MPa from 13.5MPa, and after promptly 3～4 minutes, the reaction of last running 2F is stopped by basic; But the reaction of lighting end this moment 1F is still being carried out; Bed temperature continues to raise, and system pressure was reduced to below the 6.0MPa after pressure release started about 7 minutes, and the pressure condition that suppresses lighting end 1F reaction just can reach; But the heat that sustained reaction is emitted that lighting end 1F is about 7 minutes; Because flow hydrogen gas is not smooth during emergency decompression; Reaction heat can not in time be carried away, has accomplished heat accumulation at beds, in case make the Hydrobon catalyst bed temperature rise to more than 460 ℃; Hydrobon catalyst has possessed quite active heat from hydrogenation cracking function; What take place immediately is: beds temperature runaway (temperature can rise to more than 800 ℃) process causes reactor body impaired, catalyst metal form deterioration; In short unite processing and have accidental depressurization temperature runaway risk;

6. the oil-producing capacity smallest size of national regulation coal liquification device is 1,000,000 tons/year; Therefore liquefied coal coil hydrogenation modification full scale plant is huge; By brown coal catalysis thermosol technology gelatin liquefaction rate 30m%, solvent/coal mass ratio is calculating in 2: 1, and liquefied coal coil hydrogenation modification full scale plant scale is 7,670,000 tons/year (the outer oil extraction total amounts of solvent oil and liquefaction process); By deified technology gelatin liquefaction rate 60m%, solvent/coal mass ratio is calculating in 2: 1, and liquefied coal coil hydrogenation modification full scale plant scale is 4,330,000 tons/year (the outer oil extraction total amounts of solvent oil and liquefaction process); Under the above-mentioned condition, build two covering devices and build a covering device and compare and have certain investment competitive power: can adopt reasonably lower working pressure, optimize the catalyzer configuration, reduce air speed, reduce service temperature such as the device of handling the liquefied coal coil lighting end;

7. unite and add man-hour, gained hydrogenation modification oil must just can obtain the lighting end and the last running of hydrogenation modification oil through sepn process, just can carry out hydrogenation modification oil classification hydrocracking, will increase corresponding sepn process, produces a large amount of separating energy consumptions.

For the process of producing coal liquefaction solvent oil; When processing is being rich in twin nuclei aromatic hydrocarbons and being rich in the direct hydrogenation liquefaction of coal oil of polynuclear plane aromatic hydrocarbons of representative with the listed character of table 1; The listed boiling point data suggest of table 3: with reference to conventional boiling point (177 ℃) of indane and the conventional boiling point (278 ℃) of acenaphthene; With 165 ℃ and 265 ℃ is dividing point; About conventional boiling point is that aromatic hydrocarbons that 165～265 ℃ cut will be basically contain tricyclic structure is that maximum ring structure numbers of most of aromatic hydrocarbons are 2, and the aromatic hydrocarbons of polynuclear plane is most to be concentrated and be present in the cut that conventional boiling point is higher than 265 ℃.Therefore can propose following operating principle: conventional boiling point is higher than 265 ℃ cut, and to be defined as the polynuclear plane aromatic fraction be last running 2F; It is lighting end 1F that the cut of 165～265 ℃ of conventional boiling point positions is defined as the twin nuclei aromatic fraction, selects separately The optimum reaction conditions to carry out the aromatic hydrogenation saturated reaction then.

For the process of producing coal liquefaction solvent oil; When processing listed when being 265～450 ℃ the direct hydrogenation liquefaction of coal oil of fractions consisting mainly with table 2 by conventional boiling point; The listed boiling point data suggest of table 3: with reference to conventional boiling point (278 ℃) of acenaphthene and anthracene (or luxuriant and rich with fragrance) conventional boiling point (340 ℃); With 265 ℃ and 355 ℃ is dividing point; With its fractionation for mainly by conventional boiling point be 265～355 ℃ fractions consisting lighting end with main be the last running of 355～450 ℃ fractions consisting by conventional boiling point; Lighting end is compared with last running, and the density of aromatic hydrocarbon of tricyclic structure is high relatively and Fourth Ring structure density of aromatic hydrocarbon is low relatively in the lighting end, and the density of aromatic hydrocarbon of tricyclic structure is low relatively and Fourth Ring structure density of aromatic hydrocarbon is high relatively in the last running.Therefore can propose following operating principle: with conventional boiling point is that 355～450 ℃ cut is defined as last running 2F; With conventional boiling point is that 265～355 ℃ cut is defined as lighting end 1F, selects separately The optimum reaction conditions to carry out the aromatic hydrogenation saturated reaction then.

Based on above analysis; Following " the classification hydrogenation is saturated " technological principle can be proposed: twin nuclei aromatic hydrocarbons and polynuclear plane aromatic hydrocarbons relative separation or tricyclic structure aromatic hydrocarbons and Fourth Ring and isolating benzoline of above structure aromatic hydrocarbons relative separation and heavy distillate; Select separately The optimum reaction conditions (catalyst formulation, catalyzer air speed, temperature of reaction etc.) to carry out the reaction of aromatic hydrogenation fractional saturation; The content of fractional saturation aromatic component in the hydrogenation saturated oil can be effectively improved, smooth operation property, intensifier processing safety can be improved; Aromatic hydrogenation saturated reaction elute combined separation can reduce plant investment then.

Therefore; The present invention proposes a kind of saturated combined method of hydrogenation that hydrogen supply dissolvent oil is produced in liquefied coal coil lighting end and last running that is suitable for; According to the technical process principle of " classification hydrogenation ", hydrogenation process selection differences operational condition (catalyzer, catalyzer air speed and service temperature) is avoided lighting end 1F supersaturation, improves effective hydrogen donor component content, is reduced the hydrogen consumption; Aromatic hydrogenation saturated reaction elute combined separation reduces construction investment.

The stable hydrogenation process of known liquefied coal coil has: the stable hydrogenation process of a kind of liquefied coal coil of CN1141362C patent, a kind of liquefied coal coil adverse current of CN1600837A publication application stable hydrogenation process, the method for a kind of liquefied coal coil stabilized hydrogenation of CN100378201C patent, the combined technical method of a kind of converting coal liquefied oil at maximum of CN100378204C patent, CN1224677C patent are a kind of produces a kind of method from liquefied coal coil greatly preparing hihg-quality diesel oil or rocket(engine)fuel of combined technical method, the CN1162516C patent of fine-quality diesel oil etc. by liquefied coal coil; Produce hydrogen supply dissolvent oil classification hydrogenation saturation process about liquefied coal coil, do not appear in the newspapers.

The saturated combined method of the hydrogenation of different boiling ranges high aromatic oil according to the invention is not appeared in the newspapers.

Therefore, first purpose of the present invention is to provide a kind of hydrogenation aromatic hydrocarbons fractional saturation combined method of liquefied coal coil.

Second purpose of the present invention is to provide the saturated combined method of hydrogenation of the different boiling ranges cut of the thermally dissolving and catalytic method liquefaction oil that a kind of brown coal produce liquid fuel.

The 3rd purpose of the present invention be to provide a kind of mainly by conventional boiling point be the liquefaction oil formed of 265～480 ℃ hydrocarbon the saturated combined method of hydrogenation.

The ultimate aim of gelatin liquefaction reaction process is to produce the outer oil product that supplies; Usually the hydrogenation modification oil content of liquefied coal coil hydrogenation modification process generation is two portions: with hydrogen supply dissolvent oil, a part is used as the outer oil extraction of gelatin liquefaction system oil process to a part as the gelatin liquefaction reaction process.Usually; At least a portion gelatin liquefaction light oil that the gelatin liquefaction reaction process produces is as the outer oil extraction A of coal system oil process; Remaining liquefied coal coil is used as liquefied coal coil hydrogenation modification process raw oil production gelatin liquefaction reaction process with hydrogen supply dissolvent oil and outer oil extraction B; Have the outer oil extraction of A and B two-way this moment, the final whereabouts of the outer oil extraction of A and B two-way all is such as diesel oil distillate, naphtha fraction usually through hydroconversion process production high-quality oil product.

Produce the process of diesel oil distillate for gelatin liquefaction hydrogenation solvent oil hydrogenation upgrading; When processing with table 1 or the listed character of table 2 be representative the hydrogenation modification oil of direct hydrogenation liquefaction of coal oil the time; Naphthalene or naphthalene series substance or indenes or indenes be the desirable upgrading approach of thing be accomplish first aromatic ring saturated, then to this saturated rings open loop, this is that hydrogen consumption is low, density reduces the big feasible program of amplitude; Acenaphthene or acenaphthene are that thing or fluorenes or fluorenes are that thing or anthracene or anthracene are that the desirable upgrading approach of thing is that saturated (normally two aromatic rings in the outside) of accomplishing two aromatic rings carry out the hydrogen cracking open loop to this hydrogenate then; This is rational process; But under the prior art condition, must handle well and reduce this contradiction of productive rate that density reduces petroleum naphtha and gas simultaneously as far as possible significantly; As industrial production; Should select high hydrocracking catalyst of diesel yield and operational condition as far as possible, reduce low carbon number sub product output as far as possible.According to the present invention, aromatic hydrocarbons saturated reaction elute adopts hot high score flow process usually, has promptly formed the hot high score oil (high boiling component content is high) and the cold high score oil (amount of components having low boiling points is high) of relative separation, controls hot high score temperature, can control the relative separation degree.This analysis explanation, carry out the upgrading of hydrogenation solvent oil hydrogenation according to the technological principle of " upgrading of classification hydrogenation " and produce the process of diesel oil distillate and have following advantage:

1. light, the heavy constituent " the high score oil of relative separation " that form based on liquefaction oil hydrogenation modification reaction effluent high pressure separation process of the present invention; Light constituent high score oil is carried out condition 1 hydrogenation upgrading; Heavy constituent high score oil is carried out condition 2 hydrogenation upgradings; Realize the upgrading of hydrogenation modification oil classification hydrogenation, avoid the light fraction overcracking, improve diesel yield, reduce the hydrogen consumption, improve the process synthesis economic performance; When the working pressure of condition 1 and condition 2 near the time, the hydrogenation reaction effluent of two hydrogenation processes can be provided with the combined recovery sepn process, reduces investment outlay;

2. according to the technical process principle of " classification hydrogenation upgrading "; Hydrogenation upgrading reaction process can the selection differences reaction pressure reduce construction investment; When the quantity of hydrogenation upgrading reaction raw materials oil must be built bi serie or multi-series hydrogenation unit greatly, the present invention also had the effect that reduces plant investment, quiet run, intensifier processing safety.

Therefore, the 4th purpose of the present invention is to provide the combined method of the saturated and hydrogenation saturated oil hydrogenation upgrading of a kind of hydrogenation of liquefied coal coil.

The liquefaction oil of the different boiling ranges that the thermally dissolving and catalytic method that the 5th purpose of the present invention is to provide a kind of brown coal to produce liquid fuel is produced is produced the combined method that diesel oil distillate is produced in hydrogen supply dissolvent oil and the upgrading of hydrogenation saturated oil hydrogenation thereof.

Summary of the invention

The hydrogenation aromatic hydrocarbons fractional saturation combined method of a kind of liquefied coal coil of the present invention comprises the steps:

1. at gelatin liquefaction reaction effluent Separation and Recovery part FSU, separate gelatin liquefaction reaction effluent F recovery hydro carbons wherein and obtain a lighting end 1F and a last running 2F, the average conventional boiling point of last running 2F is higher than the average conventional boiling point of lighting end 1F;

2. at lighting end 1F hydrogenation modification functional zone 1Z: at 1F hydrogenation modification reactive moieties 1R; It is hydrogenation modification reaction effluent 1P that 1F carries out aromatic hydrogenation fractional saturation reaction conversion, and the 1R hydrogenation conditions is: temperature is that 200～420 ℃, pressure are that 6.0～20.0MPa, hydrogenation catalyst 1CAT volume space velocity are 0.05～10.0hr ^-1, hydrogen/raw oil volume ratio is 300: 1～3000: 1; Conventional boiling point is higher than 165 ℃ the target components weight concentration value 1PC of full cut than the ratio 1PC/1FC=1K of the target components weight concentration value 1FC among the 1F among the 1P, and 1K is greater than 1.05; Said target components refers to the double ring arene of fractional saturation and the polycyclic aromatic hydrocarbons of fractional saturation;

3. at last running 2F hydrogenation modification functional zone 2Z: at 2F hydrogenation modification reactive moieties 2R; It is hydrogenation modification reaction effluent 2P that 2F carries out aromatic hydrogenation fractional saturation reaction conversion, and the 2R hydrogenation conditions is: temperature is that 260～460 ℃, pressure are that 6.0～20.0MPa, 2F hydrogenation catalyst 2CAT volume space velocity are 0.05～10.0hr ^-1, hydrogen/raw oil volume ratio is 300: 1～4000: 1; Conventional boiling point is higher than the ratio 2PC/2FC=2K of target components weight concentration value 2FC in 165 ℃ the full cut among the 2P, and 2K is greater than 1.05;

4. at associating high pressure separation process HS, 1P is separated into cold anticyclone with 2P entering cold anticyclone separate part CHPS and separates gas CHPV and cold anticyclone separating oil CHPL; At least a portion cold anticyclone separation gas CHPV returns the hydrogenation modification reactive moieties and recycles; Cold anticyclone separate part CHPS operational condition is: temperature is that 30～75 ℃, pressure are 6.0～20.0MPa;

Reclaim the hydrocarbon that the conventional boiling point of at least a portion among the CHPL is higher than 165 ℃ and obtain aromatic hydrocarbons fractional saturation oil distillate 1RSO.

When associating high pressure separation process HS was provided with thermal high separate part HHPS, characteristic of the present invention also was:

1. the average conventional boiling point of last running 2F is higher 50～250 ℃ than the average conventional boiling point of lighting end 1F, and the ratio N1/N2 of lighting end 1F weight rate N1 and last running 2F weight rate N2 is 0.1～10;

4. at associating high pressure separation process HS; 1P and 2P get into thermal high separate part HHPS and are separated into hot high score gas HHPV and hot high score oil HHPL; HHPV mainly is made up of hydrogen, impurity composition, conventional gas hydrocarbon, conventional liq hydrocarbon; HHPL mainly is made up of conventional liq hydrocarbon and dissolved hydrogen, and thermal high separate part HHPS operational condition is: temperature is that 150～380 ℃, pressure are 6.0～20.0MPa; In the cold anticyclone sepn process, HHPV gets into cold anticyclone separate part CHPS and is separated into cold anticyclone separation gas CHPV and cold anticyclone separating oil CHPL;

Reclaim the hydrocarbon that CHPL and at least a portion routine boiling point among the HHPL be higher than 165 ℃ and obtain aromatic hydrocarbons fractional saturation oil distillate 1RSO.

When 1P and 2P were provided with the thermal high separate part respectively, characteristic of the present invention also was:

2. at lighting end 1F hydrogenation modification functional zone 1Z: in the sepn process of 1P thermal high; 1P gets into thermal high separate part 1HHPS and is separated into hot high score gas 1HHPV and hot high score oil 1HHPL; 1HHPV mainly is made up of hydrogen, impurity composition, conventional gas hydrocarbon, conventional liq hydrocarbon; 1HHPL mainly is made up of conventional liq hydrocarbon and dissolved hydrogen, and thermal high separate part 1HHPS operational condition is: temperature is that 150～380 ℃, pressure are 6.0～20.0MPa;

3. at last running 2F hydrogenation modification functional zone 2Z: in the sepn process of 2P thermal high; 2P gets into thermal high separate part 2HHPS and is separated into hot high score gas 2HHPV and hot high score oil 2HHPL; 2HHPV mainly is made up of hydrogen, conventional gas hydrocarbon, conventional liq hydrocarbon, impurity composition, and 2HHPL mainly is made up of conventional liq hydrocarbon and dissolved hydrogen; Thermal high separate part 2HHPS operational condition is: temperature is that 150～400 ℃, pressure are 6.0～20.0MPa;

4. at associating high pressure separation process HS, 1HHPV is separated into cold anticyclone with 2HHPV entering cold anticyclone separate part CHPS and separates gas CHPV and cold anticyclone separating oil CHPL; At least a portion cold anticyclone is separated gas CHPV and is returned 1R; Cold anticyclone separate part CHPS operational condition is: temperature is that 30～75 ℃, pressure are 6.0～20.0MPa;

Reclaim the hydrocarbon that the conventional boiling point of at least a portion among 1HHPL, 2HHPL and the CHPL is higher than 165 ℃ and obtain aromatic hydrocarbons fractional saturation oil distillate 1RSO.

When 1P and 2P were provided with the thermal high separate part respectively, preferred operations condition of the present invention was:

1. the average conventional boiling point of last running 2F is higher 60～180 ℃ than the average conventional boiling point of lighting end 1F, and the ratio N1/N2 of lighting end 1F weight rate N1 and last running 2F weight rate N2 is 0.2～8;

2. the 1R hydrogenation conditions is: temperature is that 240～420 ℃, pressure are that 7.0～18.0MPa, hydrogenation catalyst 1CAT volume space velocity are 0.15～5.0hr ^-1, hydrogen/raw oil volume ratio is 500: 1～2500: 1; 1K is greater than 1.10;

Thermal high separate part 1HHPS operational condition is: temperature is that 150～320 ℃, pressure are 7.0～18.0MPa; Cold anticyclone separate part 1LHPS operational condition is: temperature is that 40～55 ℃, pressure are 7.0～18.0MPa;

3. the 2R hydrogenation conditions is: temperature is that 300～440 ℃, pressure are that 7.0～18.0MPa, 2F hydrogenation catalyst 2CAT volume space velocity are 0.15～5.0hr ^-1, hydrogen/raw oil volume ratio is 500: 1～3000: 1; 2K is greater than 1.10;

Thermal high separate part 2HHPS operational condition is: temperature is that 150～360 ℃, pressure are 7.0～18.0MPa; Cold anticyclone separate part 2LHPS operational condition is: temperature is that 40～55 ℃, pressure are 7.0～18.0MPa.

Lighting end 1F is rich in double ring arene, when last running 2F is rich in polycyclic aromatic hydrocarbons, preferred operations condition of the present invention is:

1. at gelatin liquefaction reaction effluent Separation and Recovery part FSU, separate gelatin liquefaction reaction effluent F reclaim wherein hydro carbons obtain one mainly by conventional boiling point be the lighting end 1F that forms of 165～265 ℃ hydrocarbon and one main be the last running 2F that 265～420 ℃ hydrocarbon is formed by conventional boiling point;

2. the 1R hydrogenation conditions is: temperature is that 200～400 ℃, pressure are that 7.0～15.0MPa, hydrogenation catalyst 1CAT volume space velocity are 0.35～5.0hr ^-1, hydrogen/raw oil volume ratio is 500: 1～2500: 1; 1K is greater than 1.10;

3. the 2R hydrogenation conditions is: temperature is that 260～420 ℃, pressure are that 7.0～15.0MPa, 2F hydrogenation catalyst 2CAT volume space velocity are 0.15～4.0hr ^-1, hydrogen/raw oil volume ratio is 500: 1～3000: 1; 2K is greater than 1.10;

4. cold anticyclone separate part CHPS operational condition is: temperature is that 40～55 ℃, pressure are 7.0～15.0MPa.

Lighting end 1F is rich in double ring arene, when last running 2F is rich in polycyclic aromatic hydrocarbons, unites high pressure separation process HS thermal high separate part HHPS is set, and this moment, preferred operations condition of the present invention was:

3. the 2R hydrogenation conditions is: temperature is that 260～420 ℃, pressure are that 7.0～15.0MPa, 2F hydrogenation catalyst 2CAT volume space velocity are 0.15～4.0hr ^-1, hydrogen/raw oil volume ratio is 500: 1～3000: 1; 2K is greater than 1.10.

4. thermal high separate part HHPS operational condition is: temperature is that 150～280 ℃, pressure are 7.0～15.0MPa; Cold anticyclone separate part CHPS operational condition is: temperature is that 40～55 ℃, pressure are 7.0～15.0MPa.

Lighting end 1F is rich in double ring arene, when last running 2F is rich in polycyclic aromatic hydrocarbons, 1P and 2P are provided with the thermal high separate part respectively, this moment, preferred operations condition of the present invention was:

Thermal high separate part 1HHPS operational condition is: temperature is that 150～280 ℃, pressure are 7.0～15.0MPa;

Thermal high separate part 2HHPS operational condition is: temperature is that 150～280 ℃, pressure are 7.0～15.0MPa;

Lighting end 1F is rich in double ring arene, when last running 2F is rich in polycyclic aromatic hydrocarbons, this moment, the preferred operations pressure condition of hydrogenation reaction of the present invention was:

2. 1R hydrogenation reaction pressure is 9.0～15.0MPa;

3. 2R hydrogenation reaction pressure is 9.0～15.0MPa.

The present invention is particularly suitable for handling brown coal and produces the hydro carbons in the thermally dissolving and catalytic method gelatin liquefaction reaction effluent of liquid fuel, and N1/N2 is 0.25～4 usually.

Lighting end 1F is rich in thrcylic aromatic hydrocarbon, when last running 2F is rich in Fourth Ring aromatic hydrocarbons, unites high pressure separation process HS thermal high separate part HHPS is set, and this moment, preferred operations condition of the present invention was:

1. at gelatin liquefaction reaction effluent Separation and Recovery part FSU, separate gelatin liquefaction reaction effluent F reclaim wherein hydro carbons obtain one mainly by conventional boiling point be the lighting end 1F that forms of 265～355 ℃ hydrocarbon and one main be the last running 2F that 355～480 ℃ hydrocarbon is formed by conventional boiling point;

2. the 1R hydrogenation conditions is: temperature is that 260～420 ℃, pressure are that 10.0～18.0MPa, hydrogenation catalyst 1CAT volume space velocity are 0.15～4.0hr ^-1, hydrogen/raw oil volume ratio is 500: 1～2500: 1; 1K is greater than 1.10;

3. the 2R hydrogenation conditions is: temperature is that 300～440 ℃, pressure are that 10.0～18.0MPa, 2F hydrogenation catalyst 2CAT volume space velocity are 0.10～2.0hr ^-1, hydrogen/raw oil volume ratio is 500: 1～3000: 1; 2K is greater than 1.10;

4. thermal high separate part HHPS operational condition is: temperature is that 150～280 ℃, pressure are 10.0～18.0MPa; Cold anticyclone separate part CHPS operational condition is: temperature is that 40～55 ℃, pressure are 10.0～18.0MPa.

Lighting end 1F is rich in thrcylic aromatic hydrocarbon, when last running 2F is rich in Fourth Ring aromatic hydrocarbons, when 1P and 2P were provided with the thermal high separate part respectively, operational condition of the present invention was:

2. the 1R hydrogenation conditions is: temperature is that 200～400 ℃, pressure are that 10.0～18.0MPa, hydrogenation catalyst 1CAT volume space velocity are 0.35～5.0hr ^-1, hydrogen/raw oil volume ratio is 500: 1～2500: 1; 1K is greater than 1.10;

Thermal high separate part 1HHPS operational condition is: temperature is that 150～280 ℃, pressure are 10.0～18.0MPa;

3. the 2R hydrogenation conditions is: temperature is that 260～420 ℃, pressure are that 10.0～18.0MPa, 2F hydrogenation catalyst 2CAT volume space velocity are 0.15～4.0hr ^-1, hydrogen/raw oil volume ratio is 500: 1～3000: 1; 2K is greater than 1.10.

Thermal high separate part 2HHPS operational condition is: temperature is that 150～280 ℃, pressure are 10.0～18.0MPa;

4. cold anticyclone separate part CHPS operational condition is: temperature is that 40～55 ℃, pressure are 10.0～18.0MPa.

Lighting end 1F is rich in thrcylic aromatic hydrocarbon, when last running 2F is rich in Fourth Ring aromatic hydrocarbons, this moment, preferred operations pressure condition of the present invention was:

2. 1R hydrogenation reaction pressure is 13.0～18.0MPa;

3. 2R hydrogenation reaction pressure is 13.0～18.0MPa.

Lighting end 1F is rich in thrcylic aromatic hydrocarbon, when last running 2F is rich in Fourth Ring aromatic hydrocarbons, is 0.25～4 like N1/N2 that effect of the present invention is better.

Lighting end 1F is rich in double ring arene, when last running 2F is rich in polycyclic aromatic hydrocarbons, the aromatic hydrocarbons saturated oil hydrogenation upgrading functional zone UZ operational condition of setting of the present invention is:

4. at aromatic hydrocarbons saturated oil hydrogenation upgrading functional zone UZ:

A, a part of hot high score oil 1HHPL are as material 1MF;

Material 1MF is that 165～265 ℃ hydrocarbon is formed by conventional boiling point mainly; At hydrogenation reaction part 1MR1; Material 1MF carries out the aromatic hydrogenation saturated reaction and is converted into hydrogenation reaction effluent 1MR1P, and the 1MR1 hydrogenation conditions is: temperature is that 200～460 ℃, pressure are that 4.0～25.0MPa, 1MR1 hydrogenation catalyst volume space velocity are 0.05～5.0hr ^-1, hydrogen/raw oil volume ratio is 500: 1～4000: 1;

Hydrogenation reaction effluent 1MR1P gets into high pressure separate part 1MHPS, is separated into cold high score gas 1MHPV and high score oil 1MHPL; At least a portion 1MHPV gets into hydrogenation reaction part 1MR1 and recycles;

At high score oil 1MHPL separate part, separate high score oil 1MHPL and obtain the narrow fraction oil product;

B, a part of hot high score oil 2HHPL are as material 2MF;

Material 2MF is that 265～450 ℃ hydrocarbon is formed by conventional boiling point mainly; At hydrogenation reaction part 2MR1; Material 2MF carries out the aromatic hydrogenation saturated reaction and is converted into hydrogenation reaction effluent 2MR1P, and the 2MR1 hydrogenation conditions is: temperature is that 200～460 ℃, pressure are that 7.0～30.0MPa, 2MR1 hydrogenation catalyst volume space velocity are 0.05～5.0hr ^-1, hydrogen/raw oil volume ratio is 500: 1～4000: 1;

At hydrogenation reaction part 2MR2; Hydrogenation reaction effluent 2MR1P carries out hydrocracking reaction and is converted into hydrogenation reaction effluent 2MR2P, and the 2MR2 hydrogenation conditions is: it is low and function, 2MR2 hydrogenation catalyst volume space velocity that diesel yield is high are 0.05～5.0hr that temperature is that 260～460 ℃, pressure are that 7.0～30.0MPa, 2MR2 hydrogenation catalyst possess gas yield ^-1, hydrogen/raw oil volume ratio is 500: 1～4000: 1;

Hydrogenation reaction effluent 2MR2P gets into high pressure separate part 2MHPS, is separated into high score gas 2MHPV and high score oil 2MHPL; At least a portion high score gas 2MHPV gets into hydrogenation reaction part 2MR2;

At high score oil 2MHPL separate part, separate high score oil 2MHPL and obtain the narrow fraction oil product.

Lighting end 1F is rich in double ring arene, when last running 2F is rich in polycyclic aromatic hydrocarbons, the aromatic hydrocarbons saturated oil hydrogenation upgrading functional zone UZ that the present invention is provided with, 1MR1 and the best differentiation of 2MR1 working pressure, operational condition of the present invention is generally at this moment:

A, 1MR1 hydrogenation conditions are: temperature is that 230～400 ℃, pressure are that 6.0～15.0MPa, 1MR1 hydrogenation catalyst volume space velocity are 0.15～3.0hr ^-1, hydrogen/raw oil volume ratio is 500: 1～4000: 1; 1MR1 hydrogenation reaction working pressure is than the low 2.5MPa at least of 2MR1 hydrogenation reaction working pressure;

B, 2MR1 hydrogenation conditions are: temperature is that 300～420 ℃, pressure are that 7.0～20.0MPa, 2MR1 hydrogenation catalyst volume space velocity are 0.15～3.0hr ^-1, hydrogen/raw oil volume ratio is 500: 1～4000: 1;

The 2MR2 hydrogenation conditions is: it is low and function, 2MR2 hydrogenation catalyst volume space velocity that diesel yield is high are 0.50～3.0hr that temperature is that 330～440 ℃, pressure are that 7.0～20.0MPa, 2MR2 hydrogenation catalyst possess gas yield ^-1, hydrogen/raw oil volume ratio is 500: 1～4000: 1.

A, 1MR1 hydrogenation reaction pressure are 7.0～13.0MPa, and 1MR1 hydrogenation reaction working pressure is than the low 3.5MPa at least of 2MR1 hydrogenation reaction working pressure;

B, 2MR1 hydrogenation reaction pressure are 12.0～20.0MPa;

2MR2 hydrogenation reaction pressure is 12.0～20.0MPa.

Lighting end 1F is rich in double ring arene, when last running 2F is rich in polycyclic aromatic hydrocarbons, the aromatic hydrocarbons saturated oil hydrogenation upgrading functional zone UZ that the present invention is provided with, 1MR1P and 2MR2P can combined separation, at this moment:

Hydrogenation reaction effluent 2MR2P mixes the back and gets into high pressure separate part 1MHPS with hydrogenation reaction effluent 1MR1P, be separated into cold high score gas 1MHPV and high score oil 1MHPL; At least a portion 1MHPV gets into hydrogenation reaction and partly recycles.

Lighting end 1F is rich in double ring arene, when last running 2F is rich in polycyclic aromatic hydrocarbons, the aromatic hydrocarbons saturated oil hydrogenation upgrading functional zone UZ that the present invention is provided with, 1MR1P and 2MR2P combined separation, operational condition preferably of the present invention is at this moment:

A, 1MR1 hydrogenation conditions are: temperature is that 230～400 ℃, pressure are that 7.0～20.0MPa, 1MR1 hydrogenation catalyst volume space velocity are 0.15～3.0hr ^-1, hydrogen/raw oil volume ratio is 500: 1～4000: 1;

At hydrogenation reaction part 2MR2; Hydrogenation reaction effluent 2MR1P carries out hydrocracking reaction and is converted into hydrogenation reaction effluent 2MR2P, and the 2MR2 hydrogenation conditions is: it is low and function, 2MR2 hydrogenation catalyst volume space velocity that diesel yield is high are 0.50～3.0hr that temperature is that 330～440 ℃, pressure are that 7.0～20.0MPa, 2MR2 hydrogenation catalyst possess gas yield ^-1, hydrogen/raw oil volume ratio is 500: 1～4000: 1.

Lighting end 1F is rich in double ring arene, when last running 2F is rich in polycyclic aromatic hydrocarbons, the aromatic hydrocarbons saturated oil hydrogenation upgrading functional zone UZ that the present invention is provided with, 1MR1P and 2MR2P combined separation, the preferred person of operation pressure condition of the present invention is at this moment:

A, 1MR1 hydrogenation reaction pressure are 10.0～15.0MPa;

B, 2MR1 hydrogenation reaction pressure are 10.0～15.0MPa;

2MR2 hydrogenation reaction pressure is 10.0～15.0MPa.

Lighting end 1F is rich in double ring arene, when last running 2F is rich in polycyclic aromatic hydrocarbons, the aromatic hydrocarbons saturated oil hydrogenation upgrading functional zone UZ that the present invention is provided with, in order to reduce aromaticity content in the 1MR1 charging, this moment, circulation process of the present invention can be:

A, at high score oil 1MHPL separate part, separating high score oil 1MHPL, to obtain mainly by conventional boiling point be the narrow fraction oil product 1PD that 165～265 ℃ hydrocarbon is formed, part 1PD returns hydrogenation reaction part 1MR1 and recycles.

Lighting end 1F is rich in double ring arene, when last running 2F is rich in polycyclic aromatic hydrocarbons, the aromatic hydrocarbons saturated oil hydrogenation upgrading functional zone UZ that the present invention is provided with, in order to reduce aromaticity content in the 2MR1 charging, this moment, circulation process of the present invention can be:

B, at high score oil 2MHPL separate part, separate high score oil 2MHPL and obtain the narrow fraction oil product 2PD that density (20 ℃) is higher than 900 kilograms/cubic metre, part 2PD returns hydrogenation reaction part 2MR1 and recycles.

Lighting end 1F is rich in double ring arene, when last running 2F is rich in polycyclic aromatic hydrocarbons, the aromatic hydrocarbons saturated oil hydrogenation upgrading functional zone UZ that the present invention is provided with, for the cracking 2PD that circulates, this moment, circulation process of the present invention can be:

B, at high score oil 2MHPL separate part, separate high score oil 2MHPL and obtain the narrow fraction oil product 2PD that density (20 ℃) is higher than 900 kilograms/cubic metre, part 2PD returns hydrogenation reaction part 2MR2 and recycles.

Lighting end 1F is rich in double ring arene, when last running 2F is rich in polycyclic aromatic hydrocarbons, the aromatic hydrocarbons saturated oil hydrogenation upgrading functional zone UZ that the present invention is provided with, in order to process the low cold high score oil CHPL of polycyclic aromatic hydrocarbon content, this moment, flow process of the present invention can be:

A, a part of cold high score oil CHPL are as material 1MF.

Lighting end 1F is rich in double ring arene, when last running 2F is rich in polycyclic aromatic hydrocarbons, the aromatic hydrocarbons saturated oil hydrogenation upgrading functional zone UZ that the present invention is provided with, in order to process the high cold high score oil CHPL of polycyclic aromatic hydrocarbon content, this moment, flow process of the present invention can be:

A, a part of cold high score oil CHPL are as material 2MF.

When associating high pressure separation process HS was provided with thermal high separate part HHPS, the present invention can carry out the hydrogenation upgrading respectively to hot high score oil HHPL and cold high score oil CHPL, and the present invention's this moment is characterised in that:

4. at aromatic hydrocarbons saturated oil hydrogenation upgrading functional zone UZX:

A, a part of cold high score oil CHPL are as material 1XMF;

Material 1XMF is that 165～265 ℃ the high aromatic hydrocarbons high-density of low nitrogen lighting end is formed by conventional boiling point mainly; At hydrogenation reaction part 1XMR1; Material 1XMF carries out the aromatic hydrogenation saturated reaction and is converted into hydrogenation reaction effluent 1XMR1P, and the 1XMR1 hydrogenation conditions is: temperature is that 200～460 ℃, pressure are that 4.0～25.0MPa, 1XMR1 hydrogenation catalyst volume space velocity are 0.05～5.0hr ^-1, hydrogen/raw oil volume ratio is 500: 1～4000: 1;

Hydrogenation reaction effluent 1XMR1P gets into high pressure separate part 1XMHPS, is separated into cold high score gas 1XMHPV and high score oil 1XMHPL; At least a portion 1XMHPV gets into hydrogenation reaction part 1XMR1 and recycles;

B, a part of hot high score oil HHPL are as material 2XMF;

Material 2XMF is that 265～450 ℃ the high aromatic hydrocarbons high-density of low nitrogen last running is formed by conventional boiling point mainly; At hydrogenation reaction part 2XMR1; Material 2XMF carries out the aromatic hydrogenation saturated reaction and is converted into hydrogenation reaction effluent 2XMR1P, and the 2XMR1 hydrogenation conditions is: temperature is that 200～460 ℃, pressure are that 7.0～30.0MPa, 2MR1 hydrogenation catalyst volume space velocity are 0.05～5.0hr ^-1, hydrogen/raw oil volume ratio is 500: 1～4000: 1;

At hydrogenation reaction part 2XMR2; Hydrogenation reaction effluent 2MR1P carries out hydrocracking reaction and is converted into hydrogenation reaction effluent 2XMR2P, and the 2XMR2 hydrogenation conditions is: it is low and function, 2MR2 hydrogenation catalyst volume space velocity that diesel yield is high are 0.05～5.0hr that temperature is that 260～460 ℃, pressure are that 7.0～30.0MPa, 2XMR2 hydrogenation catalyst possess gas yield ^-1, hydrogen/raw oil volume ratio is 500: 1～4000: 1;

Hydrogenation reaction effluent 2XMR2P gets into high pressure separate part 2XMHPS, is separated into high score gas 2XMHPV and high score oil 2XMHPL; At least a portion high score gas 2XMHPV gets into hydrogenation reaction part 2XMR2;

At high score oil 2XMHPL separate part, separate high score oil 2XMHPL and obtain the narrow fraction oil product.

Associating high pressure separation process HS is provided with thermal high separate part HHPS, hot high score oil HHPL and cold high score oil CHPL is carried out the hydrogenation upgrading respectively then during hydrogenation upgrading reaction effluent combined separation, the present invention:

B, hydrogenation reaction effluent 2XMR2P get into the high pressure separate part 1XMHPS that handles hydrogenation reaction effluent 1XMR1P.

Embodiment

Below describe the present invention in detail.

Conventional boiling point of the present invention refers to vapour, the liquid equilibrium temperature of material under a barometric point.

Conventional liq hydrocarbon of the present invention refers to the hydro carbons that is in a liquid state under the normal condition, comprises the hydro carbons that pentane and boiling point thereof are higher.

Impurity composition of the present invention refers to hydrogenation products non-hydrogen in the raw oil, non-carbon comprises water, hydrogen sulfide, ammonia, hydrogenchloride etc.

Proportion of the present invention unless stated otherwise, refers to the ratio of water-mass density under fluid density and normal pressure under normal pressure, the 15.6 ℃ of conditions, the 15.6 ℃ of conditions.

The composition of component of the present invention or concentration or content value unless stated otherwise, are the weight basis value, and weight percent is expressed as m%.

Petroleum naphtha fraction according to the invention refers to the hydro carbons that conventional boiling point is generally 60～190 ℃, is generally 60～180 ℃.

Fraction of diesel oil according to the invention refers to the hydro carbons that conventional boiling point is generally 160～390 ℃, is generally 180～370 ℃.

Wide fraction high aromatic oil according to the invention; Be that 165～480 ℃ hydrocarbon is formed mainly by conventional boiling point; Wherein conventional boiling point is the weight content of 165～480 ℃ hydrocarbon: generally greater than 65%, usually greater than 75%, especially greater than 85%; Its nitrogen content generally is lower than 4000PPm, is usually less than 2500PPm, is lower than 1500PPm especially; Density (20 ℃) generally be higher than 940 kilograms/cubic metre, usually above 960 kilograms/cube, be higher than 980 kilograms/cubic metre especially, aromaticity content generally is higher than 40%, usually above 55%, be higher than 70% especially.The character data scope of wide fraction high aromatic oil according to the invention only is to be used for expressing its hydrogenation characteristic, rather than is used for limiting its rerum natura or source.The main character of wide fraction high aromatic oil according to the invention is: not only contained a large amount of twin nuclei aromatic hydrocarbons and contained not only a large amount of polynuclear plane aromatic hydrocarbons simultaneously, or promptly contain a large amount of tricyclic structure aromatic hydrocarbons simultaneously but also contain a large amount of Fourth Rings structure aromatic hydrocarbons.

The character data scope of lighting end 1F according to the invention and last running 2F only is to be used for expressing its relative aromatic hydrogenation saturation characteristic, rather than is used for limiting its rerum natura or source.

Last running 2F according to the invention is for lighting end 1F according to the invention; When wide fraction high aromatic oil F when mainly to be the liquefied coal coil formed of 165～420 ℃ hydrocarbon such as brown coal produce the liquefaction oil that the thermally dissolving and catalytic method of liquid fuel obtains by conventional boiling point; Can be following situation: when lighting end 1F contained a large amount of twin nuclei aromatic hydrocarbons and contains a small amount of tricyclic structure aromatic hydrocarbons simultaneously, last running 2F contains a large amount of tricyclic structure aromatic hydrocarbons and contains a small amount of twin nuclei aromatic hydrocarbons simultaneously.At this moment; Lighting end 1F according to the invention; The hydrocarbon that refers to conventional boiling point and be 165～265 ℃ is formed; Its nitrogen content generally is lower than and generally is lower than 2500PPm, is usually less than 2000PPm, is lower than 1500PPm especially; Density (20 ℃) generally be higher than 940 kilograms/cubic metre, usually above 960 kilograms/cubic metre, be higher than 980 kilograms/cubic metre especially, aromaticity content generally is higher than 40%, usually above 55%, be higher than 70% especially, said lighting end 1F also has the situation that exceeds above-mentioned range data.At this moment; Last running 2F according to the invention; Its conventional boiling point is 265～420 ℃, and its nitrogen content generally is lower than 5000PPm, is usually less than 3000PPm, is lower than 2000PPm especially, density (20 ℃) generally be higher than 950 kilograms/cubic metre, usually above 970 kilograms/cube, be higher than 990 kilograms/cubic metre especially; Aromaticity content generally is higher than 40%, usually above 55%, be higher than 70% especially, said last running 2F also has the situation that exceeds above-mentioned range data.At this moment, the ratio N1/N2 of lighting end 1F weight rate N1 and last running 2F weight rate N2: be generally 0.1～10, be generally 0.2～8.

Last running 2F according to the invention is for lighting end 1F according to the invention; When wide fraction high aromatic oil F for mainly by conventional boiling point be 265～480 ℃ hydrocarbon form liquefied coal coil the time; Can be following situation: when lighting end 1F contained a large amount of tricyclic structure aromatic hydrocarbons and contains a small amount of Fourth Ring structure aromatic hydrocarbons simultaneously, last running 2F contains a large amount of Fourth Rings structure aromatic hydrocarbons and contains a small amount of tricyclic structure aromatic hydrocarbons simultaneously.At this moment; Lighting end 1F according to the invention; The hydrocarbon that refers to conventional boiling point and be 265～355 ℃ is formed; Its nitrogen content generally is lower than and generally is lower than 3500PPm, is usually less than 2500PPm, is lower than 1500PPm especially; Density (20 ℃) generally be higher than 950 kilograms/cubic metre, usually above 970 kilograms/cubic metre, be higher than 990 kilograms/cubic metre especially, aromaticity content generally is higher than 40%, usually above 55%, be higher than 70% especially, said lighting end 1F also has the situation that exceeds above-mentioned range data.At this moment; Last running 2F according to the invention; Its conventional boiling point is 265～450 ℃, and its nitrogen content generally is lower than 6000PPm, is usually less than 4000PPm, is lower than 2500PPm especially, density (20 ℃) generally be higher than 960 kilograms/cubic metre, usually above 980 kilograms/cube, be higher than 1000 kilograms/cubic metre especially; Aromaticity content generally is higher than 40%, usually above 55%, be higher than 70% especially, said last running 2F also has the situation that exceeds above-mentioned range data.At this moment, the ratio N1/N2 of lighting end 1F weight rate N1 and last running 2F weight rate N2: be generally 0.1～10, be generally 0.2～8.

Wide fraction high aromatic oil according to the invention can be liquefied coal coil or their mixing oil, because the source is different and source process condition all changes within the specific limits, said gelatin liquefaction oil properties according to the invention also changes within the specific limits.

No matter be which kind of DCL/Direct coal liquefaction process, the liquefied coal coil that it produces as long as its composition possesses raw material compositing characteristic according to the invention, all can use the inventive method to process.

According to the present invention, said wide fraction high aromatic oil is generally liquefied coal coil, because liquefied coal coil contains solid particulate usually, therefore gets into before the hydrogenation process of producing hydrogen supply dissolvent oil the process of passing through the filtering and removing solid particulate usually.

Characteristic of the present invention is below described.

2. at lighting end 1F hydrogenation modification functional zone 1Z: in the sepn process of 1P thermal high; 1P gets into thermal high separate part 1HHPS and is separated into hot high score gas 1HHPV and hot high score oil 1HHPL; 1HHPV mainly is made up of hydrogen, impurity composition, conventional gas hydrocarbon, conventional liq hydrocarbon; 1HHPL mainly is made up of conventional liq hydrocarbon and dissolved hydrogen, and thermal high separate part 1HHPS operational condition is: temperature is that 150～380 ℃, pressure are 6.0～20.0MPa:

2. 1R hydrogenation reaction pressure is 9.0～15.0MPa;

3. 2R hydrogenation reaction pressure is 9.0～15.0MPa.

2. 1R hydrogenation reaction pressure is 13.0～18.0MPa;

3. 2R hydrogenation reaction pressure is 13.0～18.0MPa.

A, a part of hot high score oil 1HHPL are as material 1MF;

B, a part of hot high score oil 2HHPL are as material 2MF;

B, 2MR1 hydrogenation reaction pressure are 12.0～20.0MPa;

2MR2 hydrogenation reaction pressure is 12.0～20.0MPa.

A, 1MR1 hydrogenation reaction pressure are 10.0～15.0MPa;

B, 2MR1 hydrogenation reaction pressure are 10.0～15.0MPa;

2MR2 hydrogenation reaction pressure is 10.0～15.0MPa.

A, a part of cold high score oil CHPL are as material 1MF.

A, a part of cold high score oil CHPL are as material 2MF.

A, a part of cold high score oil CHPL are as material 1XMF;

B, a part of hot high score oil HHPL are as material 2XMF;

Below describe each step of the present invention in detail.

Below describe 1F hydrogenation modification reactive moieties 1R of the present invention in detail.

At hydrogenation modification reactive moieties 1R; Under hydrogenation catalyst 1CAT existence condition; Said lighting end 1F accomplishes the reaction of aromatic hydrogenation fractional saturation, generates a hydrogenation modification reaction effluent 1P who is made up of hydrogen, impurity component, conventional gas hydrocarbon, conventional liq hydrocarbon.

Lighting end 1F aromatic hydrogenation fractional saturation reaction of the present invention; Refer to the reaction process of the consumption hydrogen that lighting end 1F takes place under hydrogen and suitable hydrogenation catalyst 1CAT (aromatic hydrogenation fractional saturation catalyzer) existence condition; Its minimum reaction depth should possess MIN industrial significance: promptly lighting end 1F is accomplished expection aromatic hydrogenation fractional saturation; This hydrogenation reaction degree of depth should be confirmed according to the aromatic hydrocarbons fractional saturation degree of aromatic component structure and expection among the lighting end 1F; Conventional boiling point among the hydrogenation modification reaction effluent 1P be in 165～480 ℃ the hydrocarbon-fraction target components weight concentration value than the ratio of the target components weight concentration value among the 1F greater than 1.05, expectation is high more good more, said target components refers to the double ring arene of fractional saturation and the polycyclic aromatic hydrocarbons of fractional saturation.

Described hydrogenation modification reactive moieties 1R; Different because of the difference of lighting end 1F character (metal content, oxygen level content, olefin(e) centent, sulphur content, nitrogen content, aromaticity content, boiling range, proportion) and hydrogenation reaction (hydrogenation deoxidation, hydrogenating desulfurization, hydrodenitrification, hydrogenation the are saturated) degree of depth; The variation range of its operational condition is very wide, should confirm according to concrete process condition.

Said hydrogenation modification reactive moieties 1R, the hydrogenation catalyst 1CAT of use can be one or both or multiple Hydrobon catalyst series combination with load in mixture.Hydrogenation catalyst 1CAT; Can be the special-purpose catalyst to concrete raw material, also can be Hydrobon catalyst and combination thereof with functions such as HDM or hydrogenation deoxidation or hydrogenating desulfurization or hydrodenitrification or hydrogenation are saturated that the unifining process of suitable refining of petroleum heavy gas oil type or wax oil type uses.

Said hydrogenation modification reactive moieties 1R, the hydrogenation catalyst 1CAT of use comprises hydrocatalyst for saturating arylhydrocarbon at least, also comprises Hydrodemetalation catalyst (the flow process position is positioned at before the hydrocatalyst for saturating arylhydrocarbon bed) usually.

Can any make-up sulphur be added hydrogenation modification reactive moieties 1R as required, with guarantee the necessary minimum concentration of hydrogen sulfide of reactive moieties such as 500PPm (v) or 1000PPm (v), to guarantee that the necessary hydrogen sulfide sectional pressure of catalyzer is not less than minimum must value.Described make-up sulphur can be sulfide hydrogen maybe can be converted into hydrogen sulfide hydroconversion process is not had the material of undesirable action, such as hydrogen sulfide containing gas or oil product, or contact dithiocarbonic anhydride or the DMDS etc. that the back generates hydrogen sulfide with high-temperature hydrogen.

Below describe 2F hydrogenation modification reactive moieties 2R of the present invention in detail.

At hydrogenation modification reactive moieties 2R; Under hydrogenation catalyst 2CAT existence condition; Said last running 2F accomplishes the reaction of aromatic hydrogenation fractional saturation, generates a hydrogenation modification reaction effluent 2P who is made up of hydrogen, impurity component, conventional gas hydrocarbon, conventional liq hydrocarbon.

Last running 2F aromatic hydrogenation fractional saturation reaction of the present invention; Refer to the reaction process of the consumption hydrogen that last running 2F takes place under hydrogen and suitable hydrogenation catalyst 2CAT (aromatic hydrogenation fractional saturation catalyzer) existence condition; Its minimum reaction depth should possess MIN industrial significance: promptly last running 2F is accomplished expection aromatic hydrogenation fractional saturation; This hydrogenation reaction degree of depth should be confirmed according to the aromatic hydrocarbons fractional saturation degree of aromatic component structure and expection among the last running 2F; Conventional boiling point among the hydrogenation modification reaction effluent 2P be in 165～480 ℃ the hydrocarbon-fraction target components weight concentration value than the ratio of the target components weight concentration value among the 2F greater than 1.05, expectation is high more good more, said target components refers to the double ring arene of fractional saturation and the polycyclic aromatic hydrocarbons of fractional saturation.

Described hydrogenation modification reactive moieties 2R; Different because of the difference of last running 2F character (metal content, oxygen level content, olefin(e) centent, sulphur content, nitrogen content, aromaticity content, boiling range, proportion) and hydrogenation reaction (hydrogenation deoxidation, hydrogenating desulfurization, hydrodenitrification, hydrogenation the are saturated) degree of depth; The variation range of its operational condition is very wide, should confirm according to concrete process condition.

Said hydrogenation modification reactive moieties 2R, the hydrogenation catalyst 2CAT of use can be one or both or multiple Hydrobon catalyst series combination with load in mixture.Hydrogenation catalyst 2CAT; Can be the special-purpose catalyst to concrete raw material, also can be Hydrobon catalyst and combination thereof with functions such as HDM or hydrogenation deoxidation or hydrogenating desulfurization or hydrodenitrification or hydrogenation are saturated that the unifining process of suitable refining of petroleum heavy gas oil type or wax oil type uses.

Said hydrogenation modification reactive moieties 2R, the hydrogenation catalyst 2CAT of use comprises hydrocatalyst for saturating arylhydrocarbon at least, also comprises Hydrodemetalation catalyst (the flow process position is positioned at before the hydrocatalyst for saturating arylhydrocarbon bed) usually.

Can any make-up sulphur be added hydrogenation modification reactive moieties 2R as required, with guarantee the necessary minimum concentration of hydrogen sulfide of reactive moieties such as 500PPm (v) or 1000PPm (v), to guarantee that the necessary hydrogen sulfide sectional pressure of catalyzer is not less than minimum must value.Described make-up sulphur can be sulfide hydrogen maybe can be converted into hydrogen sulfide hydroconversion process is not had the material of undesirable action, such as hydrogen sulfide containing gas or oil product, or contact dithiocarbonic anhydride or the DMDS etc. that the back generates hydrogen sulfide with high-temperature hydrogen.

The advantage that the present invention is applied to the method for liquefied coal coil production hydrogen supply dissolvent oil is:

1. to the fraction of different boiling ranges, select suitable separately hydrogenation catalyst, can improve " effectively hydrogen donor component " content, quiet run, avoid the excessive hydrogen consumption, save and separate power consumption;

2. to the fraction of different boiling ranges, select suitable separately hydrogenation reaction temperature, can improve " effectively hydrogen donor component " content, quiet run, avoid the excessive hydrogen consumption, save and separate power consumption;

3. to the fraction of different boiling ranges, select the suitable separately hydrogenation conditions residence time, can improve " effectively hydrogen donor component " content, quiet run, avoid the excessive hydrogen consumption, save and separate power consumption;

4. hydrogenation reaction effluent can combined separation, simplify flow process;

5. adopt device smooth operation of the present invention;

6. adopt device emergency shutdown process safety of the present invention;

7. the present invention is suitable for new device or existing plant modification, is particularly suitable for the large-scale processing device.

Below describe aromatic hydrocarbons saturated oil hydrogenation upgrading functional zone UZ of the present invention in detail.

The present invention handle mainly by conventional boiling point be 165～420 ℃ hydrocarbon forms liquefied coal coil the time, the aromatic hydrocarbons saturated oil hydrogenation upgrading functional zone UZ formation combination process that can be provided with.

At hydrogenation reaction part 1MR1, under 1MR1 hydrogenation catalyst existence condition, said material 1MF accomplishes hydrogenation reaction, generates a hydrogenation reaction effluent 1MR1P who is made up of hydrogen, impurity component, conventional gas hydrocarbon, conventional liq hydrocarbon.

The hydrogenation reaction that said material 1MF according to the invention accomplishes; Be commonly referred to as the hydrofining reaction of the consumption hydrogen that material 1MF takes place under hydrogen and appropriate catalyst existence condition; Its minimum reaction depth should possess MIN industrial significance: promptly material 1MF is accomplished the unifining of expection; This hydrogenation reaction degree of depth should be confirmed according to material 1MF character and hydrogenation target call; The nitrogen content (MV) of this process gained hydrogenated oil is lower than 50PPm, should be lower than 30PPm, be preferably lower than 15PPm; The saturated transformation efficiency of the aromatic hydrogenation of lighting end 1F is usually above 40% in this process, and the aromaticity content of gained hydrogenated oil (MV) is lower than 45%, should be lower than 35%, be preferably lower than 25%, and the cetane value (MV) of this process gained hydrogenated diesel oil generally is higher than 26, usually above 28; The nitrogen content (MV) of this process gained hydrotreated naphtha is lower than 10PPm, should be lower than 4PPm, be preferably lower than 2PPm, to be suitable for doing petroleum naphtha catalytic reforming raw material blend component.

The hydrogenation reaction that described material 1MF accomplishes; Because of the difference of material 1MF character (metal content, oxygen level, sulphur content, nitrogen content, aromaticity content, boiling range, proportion) with change the different of hydrogenation reaction (hydrogenation deoxidation, hydrogenating desulfurization, hydrodenitrification, hydrogenation the are saturated) degree of depth; The variation range of its operational condition is very wide, should confirm according to concrete process condition.

The hydrogenation reaction that described material 1MF accomplishes, the 1MR1 hydrogenation catalyst of use can be one or both or multiple catalyzer series combination with load in mixture.The 3rd hydrogenation catalyst can be the special-purpose Hydrobon catalyst to concrete raw material.Also can be the Hydrobon catalyst and the combination thereof of functions such as the HDM that uses of suitable refining of petroleum diesel oil hydrofining process or hydrogenation deoxidation or hydrogenating desulfurization or hydrodenitrification or hydrogenation are saturated.

Said hydrogenation reaction part 1MR1; Can any make-up sulphur be added reactive moieties as required; With guarantee the necessary minimum concentration of hydrogen sulfide of reactive moieties such as 500PPm (v) or 1000PPm (v), to guarantee that the necessary hydrogen sulfide sectional pressure of catalyzer is not less than minimum must value.Described make-up sulphur can be sulfide hydrogen maybe can be converted into hydrogen sulfide hydroconversion process is not had the material of undesirable action, such as hydrogen sulfide containing gas or oil product, or with the dithiocarbonic anhydride that is converted into hydrogen sulfide after high-temperature hydrogen contacts or DMDS etc.

Below describe the follow-up hydrogenation reactive moieties 1MR2 of hydrogenation reaction part 1MR1 of the present invention in detail.

When having hydrogenation reaction part 1MR2; Hydrocarbon fraction completion twin nuclei hydrocarbon hydrogenation ring-opening reaction among the hydrogenation reaction effluent 1MR1P in general this process; Its minimum reaction depth should possess MIN industrial significance: the nitrogen content (MV) of this process gained hydrotreated naphtha is lower than 4PPm, should be lower than 2PPm, be preferably lower than 1PPm, to be suitable for doing petroleum naphtha catalytic reforming raw material blend component; The cetane value (MV) of this process gained hydrogenated diesel oil generally is higher than 30, usually above 32, the preferably is higher than 35; In this process the transformation efficiency of twin nuclei aromatic hydrogenation cracking reaction generally be higher than 40%, usually above 50%, the preferably is higher than 60%.

When having hydrogenation reaction part 1MR2, hydrogenation reaction part 1MR1 and follow-up hydrogenation reactive moieties 1MR2 should treat as a complete operation, and at this moment, hydrogenation reaction part 1MR1 can regard the preparatory hydrogenation process of hydrogenation reaction part 1MR2 as.

Below describe the hydrogenation catalyst of 1MR2 of the present invention in detail.

The hydrogenation catalyst of 1MR2; Preferably possess double ring arene or dicyclo naphthenic hydrocarbon selective hydrogenation open loop function; It can be any one suitable diesel oil selective hydrogenation ring opening catalyst; Can be that the high double ring arene content of typical petroleum base catalytic diesel oil is with selective hydrogenation open loop dearomatization catalyst; These technology have the MCI technology of China Petroleum and Chemical Corporation Fushun Petrochemical Research Institute, the RICH technology of Beijing Research Institute of Petro-Chemical Engineering of Sinopec Group etc., put down in writing the document of this type technology and see table 4.The lysate diesel yield of diesel component in the 4th hydrogenation reaction part hydrocarbon oil crude material: generally greater than 85%, usually greater than 90%, more preferably greater than 95%.

According to the present invention; The hydrogenation catalyst of 1MR2 can be any suitable hydrocracking catalyst, such as can being but that the catalyzer identical with the hydrogenation catalyst of 2MR2 its service temperature, liquid hourly space velocity differ bigger: usually 1MR2 hydrogenation catalyst liquid hourly space velocity higher such as high 30% or more, service temperature is low such as hanging down 15～30 ℃.

The publication of table 4 record arenes selectivity hydrogenation ring opening catalyst

When the present invention uses hydrogenation reaction part 1MR2; At hydrogenation reaction part 1MR2; The hydrogenation ring-opening reaction that hydrogenation reaction effluent 1MR1P carries out double ring arene or naphthenic base benzene class is converted into hydrogenation reaction effluent 1MR2P, and the 1MR2 hydrogenation conditions is: temperature is that 200～460 ℃, pressure are that 4.0～25.0MPa, 1MR2 hydrogenation catalyst possess highly selective double ring arene hydrogenation open loop function, 1MR2 hydrogenation catalyst volume space velocity is 0.05～5.0hr ^-1, hydrogen/raw oil volume ratio is 500: 1～4000: 1; Hydrogenation reaction effluent 1MR2P gets into high pressure separate part 1MHPS.

Hydrogenation reaction part 1MR2 operational condition of the present invention is generally: hydrogenation reaction effluent 1MR1P accomplishes double ring arene open loop rate and is higher than 40% highly selective double ring arene hydrogenation ring-opening reaction and is converted into hydrogenation reaction effluent 1MR2P, and hydrogenation reaction part 1MR2 hydrogenation conditions is: temperature is that 250～420 ℃, pressure are that 6.0～15.0MPa, 1MR2 hydrogenation catalyst possess highly selective double ring arene hydrogenation open loop function, 1MR2 hydrogenation catalyst volume space velocity is 0.25～2.0hr ^-1, hydrogen/raw oil volume ratio is 500: 1～2000: 1.

Hydrogenation reaction part 2MR1 of the present invention; Be commonly referred to as the reaction process of the consumption hydrogen that material 2MF takes place under hydrogen and suitable 2MR1 hydrogenation catalyst (Hydrobon catalyst) existence condition; Its minimum reaction depth should possess MIN industrial significance: promptly material 2MF is accomplished the unifining of expection; This hydrogenation reaction degree of depth should be confirmed ingredient requirement according to material 2MF character and follow-up hydrogenation reaction process 2MR2; The nitrogen content (MV) of this hydrogenation process gained hydrogenated oil is usually less than 50PPm, should be lower than 30PPm, be preferably lower than 15PPm; The aromatic hydrogenation saturated reaction transformation efficiency of material 1MF is usually above 40% in this process; The aromaticity content of gained hydrogenated oil (MV) is lower than 45%, should be lower than 35%, be preferably lower than 25%, to be suitable for doing hydrocracking process 2MR2 raw oil.

Described at hydrogenation reaction part 2MR1; Different because of the difference of material 2MF character (metal content, oxygen level content, olefin(e) centent, sulphur content, nitrogen content, aromaticity content, boiling range, proportion) and this hydrogenation reaction (hydrogenation deoxidation, hydrogenating desulfurization, hydrodenitrification, hydrogenation are saturated) degree of depth; The variation range of its operational condition is very wide, should confirm according to concrete process condition.

Said at hydrogenation reaction part 2MR1, the 2MR1 hydrogenation catalyst of use can be one or both or multiple Hydrobon catalyst series combination with load in mixture.The 1MR1 hydrogenation catalyst; Can be the special-purpose catalyst to concrete raw material, also can be Hydrobon catalyst and combination thereof with functions such as HDM or hydrogenation deoxidation or hydrogenating desulfurization or hydrodenitrification or hydrogenation are saturated that the unifining process of suitable refining of petroleum heavy gas oil type or wax oil type uses.

Can any make-up sulphur be added in hydrogenation reaction part 2MR1 as required, with guarantee the necessary minimum concentration of hydrogen sulfide of reactive moieties such as 500PPm (v) or 1000PPm (v), to guarantee that the necessary hydrogen sulfide sectional pressure of catalyzer is not less than minimum must value.Described make-up sulphur can be sulfide hydrogen maybe can be converted into hydrogen sulfide hydroconversion process is not had the material of undesirable action, such as hydrogen sulfide containing gas or oil product, or contact dithiocarbonic anhydride or the DMDS etc. that the back generates hydrogen sulfide with high-temperature hydrogen.

Hydrogenation reaction part 2MR1 and hydrogenation reaction part 2MR2 should treat as a complete operation, and hydrogenation reaction part 2MR1 can regard the preparatory hydrogenation process of hydrogenation reaction part 2MR2 as.

Below describe hydrogenation reaction part 2MR2 of the present invention in detail.

Hydrogenation reaction part 2MR2 of the present invention; Be commonly referred to as the reaction process of the consumption hydrogen that the hydrocarbon fraction takes place among the hydrogenation reaction effluent 2MR1P under hydrogenation catalyst (hydrocracking catalyst) existence condition of hydrogen and suitable 2MR2; Its minimum cracking reaction degree of depth should possess MIN industrial significance: promptly accomplish the hydrogen cracking of expection; The nitrogen content (MV) of this process gained hydrotreated naphtha is lower than 10PPm, should be lower than 4PPm, be preferably lower than 2PPm, to be suitable for doing petroleum naphtha catalytic reforming raw material blend component; The cetane value (MV) of this process gained hydrogenated diesel oil generally is higher than 30, usually above 35, preferable be higher than 40.In this process among the hydrogenation reaction effluent 2MR1P hydrogen cracking cracking rate of hydrocarbon fraction be determined on a case-by-case basis, the density of the whole diesel oil in second hydrogenation reaction effluent (20 ℃) reduces by 30～100kg/ cubic meter than the density (20 ℃) of last running 2F.

At hydrogenation reaction part 2MR2; Under the hydrocracking catalyst existence condition; At least a portion hydrocarbon fraction among the hydrogenation reaction effluent 2MR1P and hydrogen are accomplished hydrocracking reaction, generate one and form hydrogenation reaction effluent 2MR2P by hydrogen, impurity component, conventional gas hydrocarbon, conventional liq hydrocarbon.

Said hydrogenation reaction part 2MR2, different because of the hydrocracking reaction degree of depth of the difference of its feedstock property (nitrogen content, aromaticity content, density) and expection, the variation range of its operational condition is very wide, should confirm according to concrete process condition.

The hydrocracking catalyst that hydrogenation reaction part 2MR2 uses can be one or both or multiple catalyzer series combination with load in mixture.Hydrocracking catalyst can be the catalyzer to concrete raw material, also can be suitable petroleum refining process poor ignition quality fuel and/or wax oil/or the hydrocracking process of heavy oil hydrocracking catalyst (comprise and relax cracking catalyst) and combination thereof of using.

Hydrogenation reaction part 2MR2; Can select amorphous (sial) hydrocracking catalyst of not fusion molecular sieve or amorphous (sial) hydrocracking catalyst of a small amount of fusion molecular sieve for use; To strengthen adaptive faculty as far as possible, improve the diesel component productive rate to organic nitrogen compound in the raw material.Second hydrogenation reaction part also can use hydrocracking catalyst and rear portion Hydrobon catalyst to carry out grating, and the rear portion Hydrobon catalyst is used for the mercaptan that cracking process produces is converted into purposes such as hydrogen sulfide.

Hydrocracking reaction one speech of hydrogenation reaction part 2MR2; Refer under hydrogen and appropriate catalyst existence condition; The reaction process (comprising cracking reaction usually) of the consumption hydrogen that the hydrocracking raw material fry dried food ingredients is given birth to; Its minimum reaction depth should possess MIN industrial significance: such as the fraction of diesel oil of producing expection character; Should confirm according to hydrocracking reaction part material oiliness matter, expection fraction of diesel oil character and hydrocracking catalyst performance: in the hope of improving the fraction of diesel oil cetane value, reducing fraction of diesel oil density to re-set target, take into account liquid yield simultaneously, this process cracking conversion rate is generally 15～70%, is generally 25～55%.

Below describe the rule of the high pressure separation process of hydrogenation reaction effluent of the present invention in detail.

The high pressure separation process of hydrogenation reaction effluent all comprises cold high pressure separator; When hydrocarbon ils density in the hydrogenation reaction effluent big (approaching) or viscosity is big or when being difficult to separate with emulsifying water with water-mass density; High pressure hot separator also is set; Hydrogenation reaction effluent entering this moment high pressure hot separator is separated into a hot high score gas gas and the hot high score fluid body of mainly being made up of the conventional liq hydrocarbon on volume, mainly be made up of hydrogen; Hot high score gas gets into cold high pressure separator and is separated into cold high score oil and cold high score gas; Because a large amount of high boiling components get in the hot high score fluid body, have realized following target: cold high score oil density diminishes or viscosity diminishes or be easy to separate with water.The high pressure separation process of hydrogenation reaction effluent is provided with high pressure hot separator, also possesses the advantage that reduces calorific loss, because hot high score fluid body can be avoided the use air cooler of hot high score gas experience or the process that cools of water cooler.Can the hydrogenation process that portion of hot high score fluid body returns the upper reaches be recycled, improving the total raw material character of the hydrogenation process that receives this turning oil, or to this turning oil hydrogenation that circulates.

Hydrogenation reaction effluent or hot high score gas get into before the cold anticyclone separate part; Usually reduce temperature (generally being and reactive moieties charging heat exchange) to about 220～100 ℃ (this temperature should be higher than sulphur hydrogenation ammonia Tc in this hydrogenation reaction effluent gas phase) earlier; Usually form water filling back end hydrogenation reaction effluent to wherein injecting washing water then; Washing water are used to absorb ammonia and issuable other impurity such as hydrogenchloride etc., and absorb the inevitable absorbing hydrogen sulphide of the aqueous solution behind the ammonia.At cold separate part, said water filling back end hydrogenation reaction effluent is separated into: a cold high score gas of on volume, mainly being made up of hydrogen, cold high score oil, a main cold high score water that be made up of water and that be dissolved with hydrogen sulfide, ammonia of mainly being made up of conventional liq hydrocarbon and dissolved hydrogen.Said cold high score water, wherein the content of ammonia is generally 0.5～15% (w), is preferably 1～8% (w).A purpose annotating washing water is ammonia and the hydrogen sulfide that absorbs in the hydrogenation reaction effluent, prevents to form sulphur hydrogenation ammonia or the crystallization of many sulphur ammonia and stops up heat exchanger channel, increases system pressure drop.The IR of said washing water, should confirm according to following principle: on the one hand, washing water are divided into vapour phase water and liquid phase water after injecting hydrogenation reaction effluent, the liquid phase water yield must be greater than zero, be preferably the washing water total amount 30% or more; On the one hand, washing water are used for absorbing the ammonia of hydrogenation reaction effluent, prevent that the ammonia concentration of high score gas is too high again, reduce catalyst activity, and the ammonia volumetric concentration of high score gas is low more good more usually, generally is not more than 200PPm and (v), preferably is not more than 50PPm (v).Described cold high pressure separator working pressure falls for the hydrogenation reaction partial pressure deducts true pressure, and the difference of cold anticyclone separate part working pressure and hydrogenation reaction pressure should not be crossed lowly or too high, is generally 0.5～1.2MPa.The hydrogen volume concentration value of described cold high score gas, should not be low excessively (causing the device working pressure to rise), generally should be not less than 70% and (v), should be not less than 80% and (v), preferably be not less than 85% (v).As previously mentioned at least a portion, be generally 85～100% cold high score gas and return in hydrogenation reaction and partly recycle, so that necessary amounts of hydrogen of hydrogenation reaction part and hydrogen concentration to be provided; In order to improve plant investment efficient, must guarantee that recycle hydrogen concentration is not less than aforesaid low limit value,, distribute according to concrete feedstock property, reaction conditions, product for this reason, can get rid of the said cold high score gas of a part to get rid of methane, the ethane that reaction produces.For the cold high score gas of discharging, can adopt conventional membrane separation process or pressure swing adsorption technique or oil wash technology to realize that hydrogen separates with non-hydrogen gaseous fraction, and the hydrogen that reclaims is used as new hydrogen.

New hydrogen gets into and adds hydrogen partial to replenish the hydrogen that adds hydrogen partial consumption, and new hydrogen hydrogen concentration is high more good more, generally should not be lower than 95% and (v), preferably be not less than 99% (v).Can all new hydrogen be introduced arbitrary hydrogenation reaction part.

The advantage that liquefied coal coil of the present invention is produced the combined method of hydrogen supply dissolvent oil and diesel component is:

1. to the hydrogenation saturated oil (cold high score oil and hot high score oil) of different boiling ranges, select suitable separately hydrogenation catalyst or the service temperature or the residence time, can improve production of diesel oil, quiet run, avoid the excessive hydrogen consumption, save and separate power consumption;

2. to the fraction of different boiling ranges, select suitable separately hydrogenation reaction pressure, can reduce construction investment;

3. the hydrogenation saturated oil of high pressure conditions or high temperature, high pressure conditions directly gets into the hydro-upgrading reaction process, reduces the pressurization energy consumption;

4. the hydrogenation saturated oil of high temperature, high pressure conditions directly gets into the hydro-upgrading reaction process, reduces heat-energy losses;

5. high pressure conditions or high temperature, high pressure conditions the hydrogenation saturated oil directly get into the hydro-upgrading reaction process, formed the high pressure associating, simplified flow process, significantly save construction investment;

6. high pressure conditions or high temperature, high pressure conditions the hydrogenation saturated oil directly get into the hydro-upgrading reaction process, reduced step, shortened the residence time of this process, reduced condensation, the coking of aromatic hydrocarbons.

Embodiment one

The hydrogenation modification process that certain brown coal is produced the thermally dissolving and catalytic method production fluid carburetion of liquid fuel adopts the present invention, and wide fraction high aromatic oil F is the listed oil product A of table 1, and its major objective is a production high-quality hydrogen supply dissolvent oil.

Reference examples one: adopt conventional liquefied coal coil hydrogenation technique; The hydrogenation aromatic hydrocarbons fractional saturation reaction process of lighting end 1F and last running 2F is accomplished in same process among the oil product A; Hydrogenation conditions is: temperature is that 330～400 ℃, pressure are 8.5～12.0MPa; Can't realize The optimum reaction conditions separately, target components weight concentration value is lower in the product aromatic hydrocarbons fractional saturation oil distillate.

Embodiment one, adopts the present invention, and each procedure condition is following:

1. wide fraction high aromatic oil F is the listed oil product A of table 1; Be that 165～360 ℃ hydrocarbon is formed by conventional boiling point mainly, its conventional boiling point is lower than 265 ℃ ingredients constitute 43%, the ingredients constitute 33% that conventional boiling point is 164～265 ℃; The ingredients constitute 57% that conventional boiling point is 265～380 ℃; Adopt the present invention, it is accomplished underpressure distillation separate (accomplishing dehydration simultaneously), reboiler furnace (also can establish separation column charging process furnace) at the bottom of the fractionation Tata is set; Fractionator overhead pressure is～0.05MPa (absolute pressure); The separation column hypomere is a stripping section, and the separation column epimere is a rectifying section, and all oil product A are separated into oily (265～380 ℃ of conventional boiling points) at the bottom of the tower of discharging at the bottom of overhead oil (conventional boiling point is lower than 265 ℃) that return tank of top of the tower discharges and the tower.Overhead oil is as lighting end 1F, and oil is as last running 2F at the bottom of the tower; The ratio N1/N2 of lighting end 1F weight rate N1 and last running 2F weight rate N2 is 0.75;

2. the 1R hydrogenation conditions is: temperature is that 260～380 ℃, pressure are that 8.5～12.0MPa, hydrogenation catalyst 1CAT volume space velocity are 0.45～2.0hr ^-1, hydrogen/raw oil volume ratio is 800: 1～1500: 1;

3. the 2R hydrogenation conditions is: temperature is that 330～400 ℃, pressure are that 8.5～12.0MPa, 2F hydrogenation catalyst 2CAT volume space velocity are 0.35～1.5hr ^-1, hydrogen/raw oil volume ratio is 1000: 1～2000: 1;

4. at associating high pressure separation process HS; 1P and 2P get into thermal high separate part HHPS and are separated into hot high score gas HHPV and hot high score oil HHPL; HHPV mainly is made up of hydrogen, impurity composition, conventional gas hydrocarbon, conventional liq hydrocarbon; HHPL mainly is made up of conventional liq hydrocarbon and dissolved hydrogen, and thermal high separate part HHPS operational condition is: temperature is that 180～280 ℃, pressure are 8.2～11.7MPa; In the cold anticyclone sepn process, HHPV gets into cold anticyclone separate part CHPS and is separated into cold anticyclone separation gas CHPV and cold anticyclone separating oil CHPL; At least a portion cold anticyclone separation gas CHPV returns the hydrogenation modification reactive moieties and recycles; Cold anticyclone separate part CHPS operational condition is: temperature is that 45～55 ℃, pressure are 8.0～11.5MPa;

Conventional boiling point among recovery CHPL and the HHPL is that 165～480 ℃ hydrocarbon obtains aromatic hydrocarbons fractional saturation oil distillate 1RSO.

The present invention makes the hydrogenation aromatic hydrocarbons fractional saturation reaction process of lighting end 1F and last running 2F accomplish in different processes; Realize The optimum reaction conditions separately, target components weight concentration value exceeds more than 5～7% than target components weight concentration value in the product aromatic hydrocarbons fractional saturation oil distillate of reference examples one in the product aromatic hydrocarbons fractional saturation oil distillate.

Select best separately catalyzer and operation condition for use like the hydrogenation aromatic hydrocarbons fractional saturation reaction process of embodiment one lighting end 1F and last running 2F, target components weight concentration value is higher than target components weight concentration value increase rate in the product aromatic hydrocarbons fractional saturation oil distillate of reference examples one in the product aromatic hydrocarbons fractional saturation oil distillate.

Table 5 reference examples one, embodiment one form with catalyzer at hydrogenation reaction part 1R and 2R

Embodiment two

Reference examples two: adopt conventional liquefied coal coil hydrogenation technique; 800 tons of total amount of finish of oil product A/time; In order to overcome the equipment enlarging difficulty, to reduce cost; Be provided with according to the bi serie device, the hydrogenation aromatic hydrocarbons fractional saturation reaction process of lighting end 1F and last running 2F is accomplished at identical process among the oil product A, and hydrogenation conditions is: temperature is that 330～400 ℃, pressure are 8.5～12.0MPa; Can't realize The optimum reaction conditions separately, target components weight concentration value is lower in the product aromatic hydrocarbons fractional saturation oil distillate.

Embodiment two, based on embodiment one, and 800 tons of total amount of finish of oil product A/time; 1F hydrogenation modification reactive moieties 1R process raw material 344 tons/time; 2F hydrogenation modification reactive moieties 2R process raw material 456 tons/time, compare with reference examples two, be bi serie equally; Realize The optimum reaction conditions separately, target components weight concentration value exceeds more than 5～7% than target components weight concentration value in the product aromatic hydrocarbons fractional saturation oil distillate of reference examples one in the product aromatic hydrocarbons fractional saturation oil distillate.

Embodiment three

The hydrogenation modification process of high-pressure coal hydrogenation direct liquefaction oil adopts the present invention, and wide fraction high aromatic oil F is the listed oil product S of table 2, and its major objective is a production high-quality hydrogen supply dissolvent oil.

Reference examples three: adopt conventional liquefied coal coil hydrogenation technique; The hydrogenation aromatic hydrocarbons fractional saturation reaction process of lighting end 1F and last running 2F is accomplished in same process among the oil product A; Hydrogenation conditions is: temperature is that 330～400 ℃, pressure are 13.5～16.0MPa; Can't realize The optimum reaction conditions separately, target components weight concentration value is lower in the product aromatic hydrocarbons fractional saturation oil distillate.

Embodiment three, adopt the present invention, and each procedure condition is following:

1. wide fraction high aromatic oil F is the listed oil product S of table 2; Be that 200～480 ℃ hydrocarbon is formed by conventional boiling point mainly, its conventional boiling point is lower than 265 ℃ ingredients constitute 10%, the ingredients constitute 53% that conventional boiling point is 265～355 ℃; The ingredients constitute 37% that conventional boiling point is 355～480 ℃; Adopt the present invention, it is accomplished underpressure distillation separate (accomplishing dehydration simultaneously), reboiler furnace (also can establish separation column charging process furnace) at the bottom of the fractionation Tata is set; Fractionator overhead pressure is～0.05MPa (absolute pressure); The separation column hypomere is a stripping section, and the separation column epimere is a rectifying section, and all oil product A are separated into oily (355～480 ℃ of conventional boiling points) at the bottom of the tower of discharging at the bottom of overhead oil (conventional boiling point is lower than 355 ℃) that return tank of top of the tower discharges and the tower.Overhead oil is as lighting end 1F, and oil is as last running 2F at the bottom of the tower; The ratio N1/N2 of lighting end 1F weight rate N1 and last running 2F weight rate N2 is 1.7;

2. the 1R hydrogenation conditions is: temperature is that 260～420 ℃, pressure are that 13.5～16.0MPa, hydrogenation catalyst 1CAT volume space velocity are 0.35～1.5hr ^-1, hydrogen/raw oil volume ratio is 500: 1～2500: 1;

3. the 2R hydrogenation conditions is: temperature is that 300～440 ℃, pressure are that 13.5～16.0MPa, 2F hydrogenation catalyst 2CAT volume space velocity are 0.35～1.2hr ^-1, hydrogen/raw oil volume ratio is 500: 1～3000: 1;

Table 6 is formed with catalyzer at hydrogenation reaction part 1R and 2R

The present invention makes the hydrogenation aromatic hydrocarbons fractional saturation reaction process of lighting end 1F and last running 2F accomplish in different processes; Realize The optimum reaction conditions separately, target components weight concentration value exceeds more than 4～6% than target components weight concentration value in the product aromatic hydrocarbons fractional saturation oil distillate of reference examples one in the product aromatic hydrocarbons fractional saturation oil distillate.

Embodiment four

Adopt the present invention, each procedure condition is following:

In the sepn process of 1P thermal high; 1P gets into thermal high separate part 1HHPS and is separated into hot high score gas 1HHPV and hot high score oil 1HHPL; 1HHPV mainly is made up of hydrogen, impurity composition, conventional gas hydrocarbon, conventional liq hydrocarbon; 1HHPL mainly is made up of conventional liq hydrocarbon and dissolved hydrogen, and thermal high separate part 1HHPS operational condition is: temperature is that 180～280 ℃, pressure are 8.5～12.0MPa;

In the sepn process of 2P thermal high; 2P gets into thermal high separate part 2HHPS and is separated into hot high score gas 2HHPV and hot high score oil 2HHPL; 2HHPV mainly is made up of hydrogen, conventional gas hydrocarbon, conventional liq hydrocarbon, impurity composition, and 2HHPL mainly is made up of conventional liq hydrocarbon and dissolved hydrogen; Thermal high separate part 2HHPS operational condition is: temperature is that 180～280 ℃, pressure are 8.5～12.0MPa;

4. at associating high pressure separation process HS, 1HHPV is separated into cold anticyclone with 2HHPV entering cold anticyclone separate part CHPS and separates gas CHPV and cold anticyclone separating oil CHPL; At least a portion cold anticyclone separation gas CHPV returns the hydrogenation modification reactive moieties and recycles; Cold anticyclone separate part CHPS operational condition is: temperature is that 45～55 ℃, pressure are 8.0～11.5MPa;

Conventional boiling point among recovery CHPL, 1HHPL and the 2HHPL is that 165～480 ℃ hydrocarbon obtains aromatic hydrocarbons fractional saturation oil distillate 1RSO.Aromatic hydrocarbons saturated oil hydrogenation upgrading functional zone UZ is set:

A, 9.7% hot high score oil 1HHPL and 9.7% CHPL are as material 1MF;

Material 1MF is that 165～265 ℃ the high aromatic hydrocarbons high-density of low nitrogen lighting end is formed by conventional boiling point mainly, and the 1MR1 hydrogenation conditions is: temperature is that 230～400 ℃, pressure are that 8.0～11.0MPa, 1MR1 hydrogenation catalyst volume space velocity are 0.55～1.0hr ^-1, hydrogen/raw oil volume ratio is 1000: 1～2000: 1; 1MR1 hydrogenation reaction working pressure is than the low 4.5MPa at least of 2MR1 hydrogenation reaction working pressure;

Hydrogenation reaction part 1MR2 operational condition is: temperature is that 280～400 ℃, pressure are that 8.0～11.0MPa, 1MR2 hydrogenation catalyst possess highly selective double ring arene hydrogenation open loop function, 1MR2 hydrogenation catalyst volume space velocity is 1.0～1.5hr ^-1, hydrogen/raw oil volume ratio is 1000: 1～2000: 1;

At high score oil 1MHPL separate part, separating high score oil 1MHPL, to obtain mainly by conventional boiling point be the narrow fraction oil product 1PD that 165～265 ℃ hydrocarbon is formed, and 20% 1PD can return hydrogenation reaction part 1MR1 and recycle.

B, 9.7% hot high score oil 2HHPL are as material 2MF;

Material 2MF is that 265～450 ℃ the high aromatic hydrocarbons high-density of low nitrogen last running is formed by conventional boiling point mainly, and the 2MR1 hydrogenation conditions is: temperature is that 300～420 ℃, pressure are that 13.0～16.0MPa, 2MR1 hydrogenation catalyst volume space velocity are 0.45～0.8hr ^-1, hydrogen/raw oil volume ratio is 1500: 1～2000: 1;

The 2MR2 hydrogenation conditions is: it is low and function, 2MR2 hydrogenation catalyst volume space velocity that diesel yield is high are 0.60～1.2hr that temperature is that 330～440 ℃, pressure are that 13.0～16.0MPa, 2MR2 hydrogenation catalyst possess gas yield ^-1, hydrogen/raw oil volume ratio is 1500: 1～2000: 1;

At high score oil 2MHPL separate part, separate high score oil 2MHPL and obtain the narrow fraction oil product 2PD that density (20 ℃) is higher than 900 kilograms/cubic metre, 30% 2PD can return hydrogenation reaction part 2MR1 or 2MR2 recycles.

The hydrogenation catalyst that uses is formed and seen that table 7～table 10, technical scheme of the present invention realized the production purpose: the nitrogen content (MV) of hydrogenation upgrading petroleum naphtha fraction is lower than 2PPm (present embodiment is controlled to be below the 1PPm), all the cetane value (MV) of hydrogenation upgrading fraction of diesel oil is 33～38 (present embodiment is controlled to be more than 33).

Table 7 is formed with catalyzer at hydrogenation reaction part 1MR1

Table 8 is formed with catalyzer at hydrogenation reaction part 1MR2

Table 9 is formed with catalyzer at hydrogenation reaction part 2MR1

Table 10 is formed with catalyzer at hydrogenation reaction part 2MR2

Table 11 hydrogenation upgrading product oil property

Embodiment five

At the separate part of coal liquification device gelatin liquefaction reaction effluent, obtain lighting end 1F and last running 2F among the embodiment one, the hydrogenation process of 1F and 2F is with embodiment one.

This example is used to explain that the mode that obtains lighting end 1F and last running 2F is unrestricted.

Lift five embodiment although this paper just lists, be enough to show effect of the present invention.

Claims

1. the hydrogenation aromatic hydrocarbons fractional saturation combined method of a liquefied coal coil comprises the steps:

2. method according to claim 1 is characterized in that:

3. method according to claim 1 is characterized in that:

4. method according to claim 3 is characterized in that:

5. method according to claim 1 is characterized in that:

6. method according to claim 2 is characterized in that:

7. method according to claim 3 is characterized in that:

8. according to claim 5 or 6 or 7 described methods, it is characterized in that:

2. 1R hydrogenation reaction pressure is 9.0～15.0MPa;

3. 2R hydrogenation reaction pressure is 9.0～15.0MPa.

9. according to claim 5 or 6 or 7 described methods, it is characterized in that:

1. the gelatin liquefaction reaction effluent is the thermally dissolving and catalytic method gelatin liquefaction reaction effluent that brown coal are produced liquid fuel, and N1/N2 is 0.25～4.

10. method according to claim 2 is characterized in that:

11. method according to claim 3 is characterized in that:

12., it is characterized in that according to claim 10 or 11 described methods:

2. 1R hydrogenation reaction pressure is 13.0～18.0MPa;

3. 2R hydrogenation reaction pressure is 13.0～18.0MPa.

13. method according to claim 12 is characterized in that:

1. N1/N2 is 0.25～4.

14., it is characterized in that according to claim 3 or 7 described methods:

A, a part of hot high score oil 1HHPL are as material 1MF;

B, a part of hot high score oil 2HHPL are as material 2MF;

15. method according to claim 14 is characterized in that:

16. method according to claim 15 is characterized in that:

B, 2MR1 hydrogenation reaction pressure are 12.0～20.0MPa;

2MR2 hydrogenation reaction pressure is 12.0～20.0MPa.

17. method according to claim 14 is characterized in that:

18. method according to claim 17 is characterized in that:

19. method according to claim 18 is characterized in that:

A, 1MR1 hydrogenation reaction pressure are 10.0～15.0MPa;

B, 2MR1 hydrogenation reaction pressure are 10.0～15.0MPa;

2MR2 hydrogenation reaction pressure is 10.0～15.0MPa.

20. method according to claim 14 is characterized in that:

21. method according to claim 14 is characterized in that:

22. method according to claim 14 is characterized in that:

23. method according to claim 14 is characterized in that:

A, a part of cold high score oil CHPL are as material 1MF.

24. method according to claim 14 is characterized in that:

A, a part of cold high score oil CHPL are as material 2MF.

25., it is characterized in that according to claim 2 or 6 described methods:

A, a part of cold high score oil CHPL are as material 1XMF;

B, a part of hot high score oil HHPL are as material 2XMF;

26. method according to claim 25 is characterized in that:

27. method according to claim 14 is characterized in that:

A, a part of hot high score oil 1HHPL are as material 1MF;

At hydrogenation reaction part 1MR2; The hydrogenation ring-opening reaction that hydrogenation reaction effluent 1MR1P carries out double ring arene or naphthenic base benzene class is converted into hydrogenation reaction effluent 1MR2P, and the 1MR2 hydrogenation conditions is: temperature is that 200～460 ℃, pressure are that 4.0～25.0MPa, 1MR2 hydrogenation catalyst possess highly selective double ring arene hydrogenation open loop function, 1MR2 hydrogenation catalyst volume space velocity is 0.05～5.0hr ^-1, hydrogen/raw oil volume ratio is 500: 1～4000: 1;

Hydrogenation reaction effluent 1MR2P gets into high pressure separate part 1MHPS.

28. method according to claim 27 is characterized in that:

A, a part of hot high score oil 1HHPL are as material 1MF;

Hydrogenation reaction part 1MR2 operational condition is: hydrogenation reaction effluent 1MR1P accomplishes double ring arene open loop rate and is higher than 40% highly selective double ring arene hydrogenation ring-opening reaction and is converted into hydrogenation reaction effluent 1MR2P, and hydrogenation reaction part 1MR2 hydrogenation conditions is: temperature is that 250～420 ℃, pressure are that 6.0～15.0MPa, 1MR2 hydrogenation catalyst possess highly selective double ring arene hydrogenation open loop function, 1MR2 hydrogenation catalyst volume space velocity is 0.25～2.0hr ^-1, hydrogen/raw oil volume ratio is 500: 1～2000: 1.