CN101173189B - Two-stage hydrogenation cracking method for producing industrial chemicals - Google Patents
Two-stage hydrogenation cracking method for producing industrial chemicals Download PDFInfo
- Publication number
- CN101173189B CN101173189B CN200610134153A CN200610134153A CN101173189B CN 101173189 B CN101173189 B CN 101173189B CN 200610134153 A CN200610134153 A CN 200610134153A CN 200610134153 A CN200610134153 A CN 200610134153A CN 101173189 B CN101173189 B CN 101173189B
- Authority
- CN
- China
- Prior art keywords
- oil
- hydrogen
- cracking
- reaction
- hydrocracking
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Images
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Catalysts (AREA)
Abstract
The invention discloses a hydrocracking method for manufacturing industrial chemicals, which is characterized in that: the weighty raw oil and the hydrogen are mixed and then enter the first hydrogenation process region; the hydrogen-rich gas obtained by separating the outflow from the first region enters directly the second hydrocracking reaction region and the liquid enters a fractionator to fractionate; the obtained gas, the naphtha and the tail oil are used as the industrial chemicals and go out of the system and the middle distillate oil single or mixing with other bad distillate oil enters the second hydrogenation process region to crack, and the gas obtained from the second region can be recycled and the liquid enters the fractionator. Compared with the prior art, the invention has the advantages of adopting two reaction regions to share a circular hydrogen system, and enabling to transform two or more bad materials into products with high added value.
Description
Technical field
The present invention relates to the refining of petroleum field, specifically, relate to a kind of two-segment hydrocracking method of producing industrial chemicals.
Background technology
Along with the develop rapidly of world economy, the demand of Chemicals is sharply increased, correspondingly, the industrial chemicals demand of producing these Chemicals is also increased substantially.Producing industrial chemicals from petroleum fractions is one of very important means, topmost industrial chemicals has benzene,toluene,xylene, and ethene, propylene etc., and petroleum fractions obtains the important source that heavy naphtha is light aromatic hydrocarbons such as benzene,toluene,xylene through hydrocracking, obtaining light naphthar and hydrocracking tail oil, to have quality good, therefore purpose product yield advantages of higher is the high quality raw material of ethylene preparing by steam cracker, propylene.
The maximum characteristics of hydrocracking process technology are can be directly not had high-quality petrochemical materialss such as the cleaning automotive fuel such as clean diesel, high-quality rocket engine fuel of sulphur, low aromatic hydrocarbons, high hexadecane value and light naphthar, heavy naphtha, tail oil by inferior raw material production.But also it is big to have a production handiness, characteristics such as liquid product yield height.Hydrocracking technology can be divided into three kinds by work flow: one-stage serial hydrocracking technical process, single-stage hydrocracking technical process and two-stage hydrocracking technical process.From work flow, what succeed in developing also widespread use at first is two-stage hydrocracking technology.First section is adopted different catalyzer with second section, wherein first section main task is that stock oil is carried out the hydrogenation pre-treatment, with organic compound hydrogenolysis such as the metal in the stock oil, sulphur, nitrogen, alkene and aromatic hydrogenation are saturated, its purpose is to be the stock oil that second section preparation do not contain or lack sulfur-bearing and nitrogen, avoids the acid sites of hydrocracking catalyst to poison.Second section main task is hydrocracking, and with low-sulfur, low nitrogen stock oil, i.e. last running in first section reactor effluent is converted into light ends.Owing to a little less than the anti-ammonia and hydrogen sulfide ability of two sections catalyzer, need first section effluent after the decrease temperature and pressure adopted stripping, go out being dissolved in the ammonia stripping that generates in the oil, first section, second section is adopted independently recycle hydrogen system separately simultaneously.
Existing two-stage method hydrocracking technology such as US4737167 disclose a kind of multiple single-stage hydrocracking technology, mainly be first section whole conversion that realize raw material, intermediate oil with first section generation enters the further hydrocracking of second reaction zone then, produces the lower product of cut.It all is converted into very light product with heavy raw oil, and chemical hydrogen consumption is very big, and does not produce this high-quality cracking of ethylene raw material of hydrocracking tail oil.US4940503 discloses a kind of two sections hydrocarbon conversion technologies and catalyzer, in first section, remove impurity such as sulphur and nitrogen, and through stripping, the liquid behind the stripping enters second section and carries out hydrocracking, this method needs stripping tower, and two reaction zones use recycle hydrogen system separately respectively.
CN01823056.3 discloses a kind of two-stage hydrocracking process, mainly emphasize the hydrotreatment/method for hydrogen cracking of hydrogen make-up gas logistics, this method stock oil all is converted into the product that boiling point is lower than stock oil, this method has considered that just hydrogen is second section energy-conservation use, use as if the hydrogen of the new hydrogen that only uses this device as two sections, then two sections the quantity that processes raw material is very limited, and can not produce this extraordinary industrial chemicals of hydrocracking tail oil.
US5904835 discloses a kind of parallel hydrocracking method, although this method is used two serial reaction districts, their charging is identical, is public fractionating system, this method can be understood as two cover hydroeracking unit parallel operations, can not mass production of chemical materials.
US2003/0221990A1, US2005/0103682A1 discloses a kind of boat coal round-robin multistage method for hydrogen cracking. and the method for hydrogen cracking of these two pieces of patent disclosures is at the low 3.45～6.9MPa of first section of pressure ratio and substantially not under the situation of sulfide hydrogen and ammonia, first section round-robin light-end products carried out cracking, to produce more gas and petroleum naphtha. because the working pressure in two-stage reaction district differs bigger, therefore need take two to overlap independently recycle hydrogen system, and two sections treatment zones use expensive noble metal catalyst usually, running cost is higher. and there is complex process in this method, shortcomings such as process cost height.
The present inventor finds, have hydrogen sulfide and considerably less ammonia in the presence of, adopts suitable hydrocracking catalyst, lighter intermediate oil can be very easy to cracking generation gas and petroleum naphtha, and its transformation efficiency is also higher.Based on this discovery, the contriver has proposed a kind of new method for hydrogen cracking, except can producing a large amount of petroleum naphthas, can also provide fine preparing ethylene by steam cracking raw material.
Summary of the invention
The technical problem to be solved in the present invention provides a kind of two-segment hydrocracking method of producing industrial chemicals, the inventive method can keep that two-segment hydrocracking method is strong to adaptability to raw material, in the good product quality, the greatly preparing hihg-quality industrial chemicals, especially fecund has the more petroleum naphtha and the hydrocracking tail oil of high added value.
Method for hydrogen cracking of the present invention comprises:
(1) heavy distillate and hydrogen mix the back by containing the one-stage hydrogenation processing reaction district of hydrocracking catalyst, and reaction effluent obtains hydrogen-rich gas and liquid product after separating;
(2) hydrogen-rich gas of step (1) enters the secondary hydrogenation processing reaction district of containing hydrocracking catalyst, and liquid product enters separation column to carry out fractionation and obtain gas, light naphthar, heavy naphtha, kerosene, diesel oil and tail oil cut;
(3) a kind of in the kerosene that obtains of step (2), the diesel oil distillate or all and the hydrogen-rich gas of step (1) enter secondary hydrogenation processing reaction district after mixing, further carry out hydrotreatment;
The raw material that enters the secondary hydrogenation treatment zone can also comprise the lightweight material oil inferior (as kerosene inferior and/or diesel oil distillate) in other source, one section low 0.1～2.0MPa of the pressure ratio of described secondary hydrogenation treatment zone;
(4) reaction effluent that obtains of step (3) is after separating, the hydrogen-rich gas stream Recycling, and liquid product enters separation column to be separated, and obtains the gas, light naphthar, heavy naphtha and the tail oil that increase than step (2) quantity.
The present invention adopts the two-stage method operating process, wherein handles heavy raw oil for first section, second section intermediate oil and other intermediate oil inferior of originating of handling one section generation.First section can be the single hop flow process, the combination catalyst of filling single-stage hydrocracking catalyzer or filling hydrocracking pretreatment catalyst and hydrocracking catalyst in the reactor; First section can also be the one-stage serial flow process, the first reactor charge hydrocracking pretreatment catalyst, the second reactor charge hydrocracking catalyst.Second section general two agent flow process of single hop that adopt.
Heavy distillate of the present invention comprises various hydrocarbon feeds.Typical raw material comprises any heavy oil or synthetic oil cut (boiling point is usually above 200 ℃), this class raw material comprises straight-run gas oil, decompressed wax oil, wax tailings, delayed coking wax oil, gas oil viscosity reduction, vacuum residuum, long residuum, Fisher-Tropsch synthesis fuels or diasphaltene wet goods, also can be the coal synthetic oil, the coal tar wet goods.The lightweight material oil inferior in described other sources can be the straight run intermediate oil of crude oil such as cycloalkyl, cycloalkanes intermediate base, intermediate ring alkyl, catalytic cracking light cycle oil (LCO) etc., principal feature is that further difficulty of processing is big, paraffinicity is low, naphthenic hydrocarbon and aromaticity content height, wherein naphthenic hydrocarbon and aromatic hydrocarbons total amount reach more than the 85wt%.
As technical term commonly used, hydrotreatment mainly is meant hydrofining or hydrocracking in this application, is meant hydrocracking more.Typical hydrofining condition and hydrocracking condition comprise: reaction pressure 5.0～35.0MPa, preferred 6.0～19.0MPa; 200～480 ℃ of temperature of reaction, preferred 270～450 ℃; Volume space velocity 0.1～15.0h
-1, preferred 0.2～3.0h
-1Hydrogen to oil volume ratio 100: 1～2500: 1, preferred 400: 1～2000: 1; Wherein the working pressure of secondary hydrogenation treatment zone is lower slightly than one section reaction zone, approximately low 0.1～2.0MPa.
Each hydrotreatment district can have only a kind of catalyzer, or the combination of several catalyzer.The Hydrobon catalyst that uses form by the hydrogenation metal of carrier and institute's load.Weight with catalyzer is benchmark, generally includes group vib metal component in the periodic table of elements, counts 10%～35% as tungsten and/or molybdenum with oxide compound, is preferably 15%～30%; Group VIII metal such as nickel and/or cobalt count 1%～7% with oxide compound, are preferably 1.5%～6%.Carrier is inorganic refractory oxide such as aluminum oxide, amorphous silicon aluminium, silicon oxide, titanium oxide etc., wherein conventional Hydrobon catalyst can be existing various commercial catalysts, as Fushun Petrochemical Research Institute (FRIPP) develop 3936,3996, Hydrobon catalysts such as FF-16, FF-26, FF-36, the HC-K of Uop Inc., HC-P, the TK-555 of Topsor company, TK-565 catalyzer, the KF-847 of AKZO company, KF-848 or the like.
Hydrocracking catalyst generally includes cracking component, hydrogenation component and tackiness agent.As can being to comprise any suitable hydrocracking catalyst of prior art.The cracking component generally includes amorphous aluminum silicide phase and/or molecular sieve, as Y type or USY molecular sieve.Tackiness agent is generally aluminum oxide or silicon oxide.Hydrogenation component is metal, metal oxide or the metallic sulfide of VI family, VII family or VIII family, more preferably one or more in iron, chromium, molybdenum, tungsten, cobalt, nickel or its sulfide or the oxide compound.Weight with catalyzer is benchmark, hydrogenation component content be generally 5～40wt%.Specifically existing hydrocracking catalyst can be selected, also specific hydrocracking catalyst can be prepared as required.Commercial hydrocracking catalyst mainly contains: the HC-12 of Uop Inc., HC-14, HC-24, DHC-39 etc. and FRIPP develop 3905,3955, FC-12, FC-16, FC-24,3971,3976, FC-26, ZHC-02, FC-28 etc., and CHEVRON company ICR126, the ICR210 etc. that develop.
Compared with prior art, method for hydrogen cracking of the present invention has following advantage:
(1) technical process is simple relatively, and total system only is provided with a circulating hydrogen compressor, has reduced cost of investment and process cost.Utilizing one section hydrogen-rich gas that obtains directly to enter the second-stage reaction district participates in reaction and as quenching hydrogen, has reduced the load of circulating hydrogen compressor significantly; And hydrocracking catalyst used in the present invention is non-precious metal catalyst, but not expensive noble metal catalyst also greatly reduces process cost.
(2) be circulated to two sections treatment zones by the intermediate oil that fractionation is obtained and carry out cracking, increased productive rate light, heavy naphtha; Mix refining part external source intermediate oil inferior and then widened the raw material sources of hydroeracking unit, and improved the utilization ratio of two sections treatment zone hydrocracking catalysts, and the heavy naphtha that obtains virtue potential content obviously improves; And one section hydrocracking tail oil BMCI value that obtains is lower, is suitable as very much the raw material of downstream preparing ethylene by steam cracking, and therefore method for hydrogen cracking of the present invention can be realized the greatly preparing hihg-quality industrial chemicals.
Description of drawings
Fig. 1 is a principle process flow diagram of the present invention.
Embodiment
Figure 1 shows that a process flow diagram of the present invention, wherein first section is adopted the one-stage serial flow process, first section and second section shared separation column. as shown in Figure 1, the stock oil 1 of preheating with enter hydrocracking pretreatment reaction device 4 after recycle hydrogen 3 mixes, the hydrogenation effluent 5 that obtains with continue to enter hydrocracking reactor 6 after cold hydrogen mixes, obtain hydrocracking effluent 7, hydrocracking effluent 7 obtains hydrogen-rich gas 9 and liquid stream 10 in separator 8 separation, hydrogen-rich gas 9 directly enters secondary hydrogenation cracking case 18, the liquid stream 23 that liquid stream 10 that separation obtains and secondary hydrogenation cracking obtain is mixed into separation column 11, carries out fractionation and obtain gas products 12 in separation column 11, light naphthar 13, heavy naphtha 14, intermediate oil (comprising kerosene and diesel oil distillate) 15 and tail oil 16; Wherein intermediate oil 15 partly or entirely with after the lightweight material oil 17 in hydrogen-rich gas 9 and other source mixes enters secondary hydrogenation cracking case 18, obtain secondary hydrogenation cracking effluent 19, effluent 19 separates in separator 20 and obtains hydrogen-rich gas 21 and liquid stream 23, wherein hydrogen-rich gas 21 mixes with new hydrogen 2 and recycles behind circulating hydrogen compressor 22, and the liquid stream 23 that obtains enters and carries out fractionation in the separation column 11.
Certainly, protection scope of the present invention is not limited only to schematic flow sheet shown in Figure 1.For example, intermediate oil 15 also can straight-forward fractional distillation obtain kerosene(oil)fraction and diesel oil distillate, and the secondary hydrogenation cracking case 18 that partly or entirely is circulated to of kerosene(oil)fraction or diesel oil distillate carries out cracking; The raw material that perhaps enters secondary hydrogenation cracking case 18 includes only the middle runnings of separation column, and does not comprise the lightweight material oil in other source.Though flow process recited above is not included in the schematic flow sheet shown in Figure 1, all be the embodiment of technical solution of the present invention.
Below by embodiment technical scheme of the present invention and effect are described.
Embodiment 1-5 adopts exemplary flow shown in Figure 1, raw materials used oil properties sees Table 1, catalyst system therefor is Fushun Petrochemical Research Institute's development, FC-26, FC-24 and 3976 catalyzer that FF-26 hydrocracking pretreatment catalyst that Gong Quan company in Shandong produces and Fushun Petrochemical Research Institute produce.The composition and the character of catalyzer see Table 2, and processing condition and the product property of embodiment 1-5 are listed in table 3.The boiling range scope of each cut is respectively among the embodiment: light naphthar＜65 ℃, 65～177 ℃ of heavy naphtha, 177～260 ℃ of kerosene, 260～350 ℃ of diesel oil, tail oil＞350 ℃.
The result of embodiment 1-5 shows, adopt method for hydrogen cracking of the present invention, faulty wax oil stock oil and lightweight material oil inferior can be carried out hydrocracking simultaneously, and maximum is produced the industrial chemicals of high added values such as light naphthar, heavy naphtha and hydrogenation tail oil.
Table 1 stock oil character
The composition of table 2 catalyzer and character
Table 3 processing condition and product property
*Stock oil is the intermediate oil that obtains of separation column and the mixing oil of other lightweight material oil inferior of originating, and the quantity of lightweight material oil inferior of wherein mixing refining is in one section heavy feed stock weight of oil.
Claims (9)
1. a method for hydrogen cracking of producing industrial chemicals comprises the steps:
(1) heavy distillate and hydrogen mix the back by containing the one-stage hydrogenation processing reaction district of hydrocracking catalyst, and reaction effluent obtains hydrogen-rich gas and liquid product after separating;
(2) hydrogen-rich gas of step (1) enters the secondary hydrogenation processing reaction district of containing hydrocracking catalyst, and liquid product enters separation column to carry out fractionation and obtain gas, light naphthar, heavy naphtha, kerosene, diesel oil and tail oil cut;
(3) a kind of in the kerosene that obtains of step (2), the diesel oil distillate or all and the hydrogen-rich gas of step (1) enter secondary hydrogenation processing reaction district after mixing, further carry out hydrotreatment; One section low 0.1～2.0MPa of the pressure ratio of described secondary hydrogenation treatment zone;
(4) reaction effluent that obtains of step (3) is after separating, and hydrogen-rich gas stream is mixed Recycling afterwards with new hydrogen, and liquid product enters separation column to be separated, and obtains gas, light naphthar, heavy naphtha and tail oil than the increase of step (2) quantity.
2. according to the described method for hydrogen cracking of claim 1, it is characterized in that at least one bed in described hydrotreatment district contains hydrocracking catalyst.
3. according to the described method for hydrogen cracking of claim 1, it is characterized in that the hydroprocessing condition in step (1) and the step (3) is: reaction pressure 5.0～35.0MPa, 200～480 ℃ of temperature of reaction, volume space velocity 0.1～15.0h
-1, hydrogen to oil volume ratio 100: 1～2500: 1.
4. according to the described method for hydrogen cracking of claim 3, it is characterized in that the hydroprocessing condition in step (1), the step (3) is reaction pressure 6.0～19.0MPa, 270～450 ℃ of temperature of reaction, volume space velocity 0.2～3.0h
-1With hydrogen to oil volume ratio 400: 1～2000: 1.
5. according to the described method for hydrogen cracking of claim 1, it is characterized in that the boiling point of the heavy distillate described in the step (1) is higher than 200 ℃.
6. according to the described method for hydrogen cracking of claim 5, it is characterized in that described heavy distillate is selected from straight-run gas oil, decompressed wax oil, wax tailings, delayed coking wax oil, gas oil viscosity reduction, vacuum residuum, long residuum, Fisher-Tropsch synthesis fuels, deasphalted oil, coal synthetic oil or coal tar.
7. according to the described method for hydrogen cracking of claim 1, the raw material that it is characterized in that entering in the described step (3) secondary hydrogenation processing reaction district also comprises the lightweight material oil inferior in other source.
8. according to the described method for hydrogen cracking of claim 7, it is characterized in that being in the described lightweight material oil inferior cycloalkyl, cycloalkanes intermediate base, intermediate ring alkyl straight run intermediate oil or catalytic cracking light cycle oil.
9. according to the described method for hydrogen cracking of claim 8, it is characterized in that naphthenic hydrocarbon and aromatic hydrocarbons total amount reach more than the 85wt% in the described lightweight material oil inferior.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN200610134153A CN101173189B (en) | 2006-11-01 | 2006-11-01 | Two-stage hydrogenation cracking method for producing industrial chemicals |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN200610134153A CN101173189B (en) | 2006-11-01 | 2006-11-01 | Two-stage hydrogenation cracking method for producing industrial chemicals |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101173189A CN101173189A (en) | 2008-05-07 |
| CN101173189B true CN101173189B (en) | 2010-05-12 |
Family
ID=39421947
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN200610134153A Active CN101173189B (en) | 2006-11-01 | 2006-11-01 | Two-stage hydrogenation cracking method for producing industrial chemicals |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN101173189B (en) |
Families Citing this family (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102465008B (en) * | 2010-11-04 | 2015-01-14 | 中国石油化工股份有限公司 | Sulfuration method of catalyst for hydrocracking technology |
| CN104560173B (en) * | 2013-10-29 | 2016-11-16 | 中国石油化工股份有限公司 | A kind of heavy oil hydrogenation conversion method |
| CN104611026B (en) * | 2013-11-05 | 2016-11-16 | 中国石油化工股份有限公司 | A kind of low energy consumption produces the two-segment hydrocracking method of high-quality industrial chemicals |
| CN109988648B (en) * | 2017-12-29 | 2021-07-09 | 中国石油化工股份有限公司 | Hydrocracking process for flexibly producing diesel oil |
| CN109988610B (en) * | 2017-12-29 | 2021-05-04 | 中国石油化工股份有限公司 | Flexible two-stage hydrocracking method |
| CN109988617B (en) * | 2017-12-29 | 2021-07-09 | 中国石油化工股份有限公司 | Flexible two-stage hydrocracking process |
| CN110835550B (en) * | 2018-08-15 | 2021-12-17 | 中国石油化工股份有限公司 | Hydrocracking method for producing chemical raw materials |
| CN111100708B (en) * | 2018-10-29 | 2021-12-17 | 中国石油化工股份有限公司 | Hydrocracking method for producing chemical raw materials |
| CN110862837A (en) * | 2019-12-25 | 2020-03-06 | 陕西延长石油（集团）有限责任公司 | System and method for grading, processing and utilizing full-fraction coal tar |
| CN114437801B (en) * | 2020-10-19 | 2023-05-30 | 中国石油化工股份有限公司 | Two-stage hydrocracking method |
| CN112391201B (en) * | 2020-10-22 | 2022-01-07 | 中国科学院大连化学物理研究所 | Method for mixing ethylene cracking tar with naphthenic base heavy oil or residual oil thereof |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1260376A (en) * | 1999-03-08 | 2000-07-19 | 中国石化集团洛阳石油化工工程公司 | Converting and combining method for hydrogenation of hydrocarbon |
| WO2003080769A1 (en) * | 2002-03-21 | 2003-10-02 | Chevron U.S.A. Inc. | New hydrocracking process for the production of high quality distillates from heavy gas oils |
| US20030221990A1 (en) * | 2002-06-04 | 2003-12-04 | Yoon H. Alex | Multi-stage hydrocracker with kerosene recycle |
-
2006
- 2006-11-01 CN CN200610134153A patent/CN101173189B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1260376A (en) * | 1999-03-08 | 2000-07-19 | 中国石化集团洛阳石油化工工程公司 | Converting and combining method for hydrogenation of hydrocarbon |
| WO2003080769A1 (en) * | 2002-03-21 | 2003-10-02 | Chevron U.S.A. Inc. | New hydrocracking process for the production of high quality distillates from heavy gas oils |
| US20030221990A1 (en) * | 2002-06-04 | 2003-12-04 | Yoon H. Alex | Multi-stage hydrocracker with kerosene recycle |
Also Published As
| Publication number | Publication date |
|---|---|
| CN101173189A (en) | 2008-05-07 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101173189B (en) | Two-stage hydrogenation cracking method for producing industrial chemicals | |
| CN112143522B (en) | Hydrogenation method and system for production chemical material | |
| CN101376839B (en) | Diesel fraction deep hydrogenation method | |
| CN104611029B (en) | A kind of catalytic cracking diesel oil hydrogenating conversion process | |
| CN101067089B (en) | Shale oil producing process | |
| CN1876767B (en) | Coal tar hydrocracking method | |
| CN103773464B (en) | Hydrocracking method of productive high-quality jet fuel | |
| CN101724454A (en) | Hydrocracking method for producing high-octane petrol | |
| JP2008524386A (en) | High conversion rate hydrotreatment | |
| CN103773452B (en) | A kind of method for hydrogen cracking of high-output qulified industrial chemicals | |
| PL189544B1 (en) | Integrated hydroconversion process with reverse hydrogen flow | |
| CN110938466A (en) | Wax oil hydrocracking method | |
| CN104611050B (en) | A kind of catalytic cracking diesel oil method for transformation | |
| CN103059960B (en) | Flexible hydrocracking method | |
| CN101280221A (en) | Hydrogenation conversion method for poor ignition quality fuel distillate | |
| CN103773450B (en) | A kind of method for hydrogen cracking processing inferior raw material | |
| CN107557064B (en) | Coal tar combined bed hydrogenation method and system for coal tar combined bed hydrogenation | |
| CN103805247B (en) | A kind of combined technical method processing poor ignition quality fuel | |
| CN1175090C (en) | Method for producing the clean diean diesel oil with low sulfur and low arene | |
| CN103773473A (en) | Two-stage hydrocracking method used for producing high-quality jet fuel | |
| CN103805248A (en) | Method for producing clean fuel oil from ethylene tar | |
| CN110835550B (en) | Hydrocracking method for producing chemical raw materials | |
| CN103773462A (en) | Two-stage hydrocracking method used for producing high-quality chemical raw materials | |
| CN103773497A (en) | Method for increasing yield of clean fuel oil | |
| CN103773463A (en) | Two-stage hydrocracking method |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |