CN105623720B - Method for preparing raw material for needle-like coke - Google Patents
Method for preparing raw material for needle-like coke Download PDFInfo
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- CN105623720B CN105623720B CN201410601630.4A CN201410601630A CN105623720B CN 105623720 B CN105623720 B CN 105623720B CN 201410601630 A CN201410601630 A CN 201410601630A CN 105623720 B CN105623720 B CN 105623720B
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Abstract
The invention discloses a method for preparing a raw material for needle-like coke. The method comprises the steps of injecting a raw-material mixture heated by a radiation section of a heating furnace into coking towers for a delayed coking reaction, and carrying out fractionating on oil gas generated from the delayed coking reaction, so as to obtain a wax oil component, wherein the raw-material mixture contains catalytic cracking oil slurry and delayed coking stock, during the delayed coking reaction, cooling oil and/or cooling water are injected into the tops of the coking towers through pipelines, steam is injected into the bottoms of the coking towers, the pipelines for injecting the cooling oil and/or cooling water extend into the coking towers, and the cooling oil and/or cooling water contain desulfurization and denitrification catalysts. By the method disclosed by the invention, high-quality raw materials for the needle-like coke can be prepared, and the source of raw materials of the needle-like coke can be enlarged.
Description
Technical field
The present invention relates to a kind of method for preparing needle-shape coke raw material.
Background technology
Needle coke is production high power, the main raw material(s) of ultra high power graphite electrode.High-quality needle coke price is higher, can
As electric furnace steel making ultra high power graphite electrode, ultracapacitor used for electric vehicle, communication battery li-ion electrode and quilt
Extensively apply.In needle coke production, the influence factor of most critical is feedstock property, and the better needle coke for obtaining of feedstock property is produced
Product higher grade.In the general raw material for requiring production needle coke, arene content reaches 30%-50%, and colloid, asphalitine are less than
1%th, ash is less than 0.5% less than 100ug/g, sulfur content.A large amount of aromatic components that catalytic cracked oil pulp is rich in are production needle-like
Burnt ideal composition.As the property of the current majority catalytic cracked oil pulps of the restriction of raw material can not meet above-mentioned requirements, belong to bad
Matter slurry oil, impurity is more, colloid and asphalt content high, and these components and impurity can have a strong impact on the preparation process of needle coke, make
The needle coke Quality Down of production will not even generate needle coke.If said components and impurity separated, catalysis inferior is split
Carburetion slurry is then preferable needle-shape coke raw material.At present, account for the most slurry oil inferior of catalytic cracked oil pulp yield to be mainly used in adjusting
Close fuel oil or incorporation subtracts slag as the raw material of delayed coking, substantial amounts of aromatic component becomes fuel oil ingredient in above process
With ordinary coke, this is undoubtedly greatly waste.How existing process is utilized, make catalytic cracked oil pulp inferior meet needle coke former
The requirement of material is problem demanding prompt solution.
CN101724420B discloses one kind and processes catalytic cracked oil pulp and conventional coking raw material using delay coking process
The method of production needle-shape coke raw material.Slurry oil is fed from coke drum middle and upper part in the method, and conventional coking raw material is from coke drum bottom
Charging, slurry oil contacts with high-temperature oil gas in the coke drum, and removing is unfavorable for the component that needle coke is produced, by coking fractional distillation column
Side line obtain wax tailings as needle-shape coke raw material.In the method as slurry oil is without heating furnace radiant section, temperature compared with
Low and slurry oil is all fed from middle and upper part, and the time of staying is shorter, and this causes part colloid, asphalitine to be not sufficiently reacted, will
It is carried in wax tailings by oil gas；If the sulfur content on the other hand in raw material slurry oil is higher, the sulfur content in wax tailings is very
It is difficult to meet requirement, therefore the application of the method is considerably limited.Additionally, the main reactor of delayed coking is coke drum,
Raw material is converted into oil gas and coke in the coke drum, in conventional delayed coking technique a large amount of aromatic components have little time from coke drum from
Open and translate into coke, reduce the yield of pin Jiao's raw material.
CN1872963A discloses a kind of preprocessing method of raw materials for producing needle coke, raw oil elder generation Jing vacuum distillations removing
Wherein undesirable components, remaining ideal composition are contacted with hydrogen, hydrogenation catalyst, and hydrogenation reaction logistics is isolated to production
The raw material of needle coke.The method needs individually filtration, vacuum distillation apparatus, invests larger, and obtained by the method
Still contain a certain amount of colloid in needle-shape coke raw material, the quality of needle coke can be affected to produce high-grade needle coke product more
It is difficult.
The content of the invention
Present invention aim at providing a kind of new method for preparing needle-shape coke raw material, can be made by the method for the present invention
The needle-shape coke raw material of standby high-quality, and the raw material sources of needle coke can be extended.
The present invention provides a kind of method for preparing needle-shape coke raw material, and the method includes to heat through heating furnace radiant section
Delayed coking reaction is carried out in mixed material injection coke drum, and the oil gas that delayed coking reaction is produced is carried out into fractional distillation, obtained
Wax oil component；Wherein, the mixed material contains catalytic cracked oil pulp and delayed coking raw material, in delayed coking reaction process
In, cooling oil and/or cooling water are injected by pipeline in the coke drum top, steam is injected in coke drum bottom, inject cold
But the pipeline of oil and/or cooling water is stretched in coke drum, and is catalyzed containing desulfurization, denitrogenation in the cooling oil and/or cooling water
Agent.
In the preparation method of the present invention, at the top of the coke drum by pipeline injection cooling oil and/or cold
But water, and suitable control stretches into the length of pipeline of injection cooling oil and/or cooling water in coke drum, can reduce on coke drum
Portion's temperature is advantageously reduced beneficial to the reaction for producing the aromatic component of needle coke in coke drum.
Cooling oil and/or cooling water are injected by pipeline at the top of the coke drum, coke drum top temperature can be reduced
Degree, so as to advantageously reduce beneficial to the reaction for producing the aromatic component of needle coke in coke drum.
In the preparation method of the present invention, cooling oil and/or cooling water are injected in the form of water column by pipeline
So that cooling oil and/or cooling water will not be directly carried in main oil gas piping in the form of fine droplet.
In the preparation method of the present invention, by steam being injected in coke drum bottom, can effectively keep green coke
Easily there is the time of staying of secondary response component in duct and reduction.
In the preparation method of the present invention, the colloid, asphalitine in coking raw material and catalytic cracked oil pulp passes through one
The cracking of series and condensation reaction, are removed in the form of generating distillate and coke, and metal impurities also serve as the group of coke
Get removing, sulfur, nitrogen are because be reduced under desulfurization, denitrification catalyst existence condition.
In addition, in the preparation method of the present invention, as asphalitine, colloid and metal can enter in coke drum
Removing is gone, and sulfur, nitrogen can also be reduced.Therefore, preparation method of the invention is particularly well-suited to the poor catalysis of property
Cracking slurry oil is (for example：More than 4 weight %, (preferably 4-15 weight %, ash are more than 0.2 weight % (preferably 0.2- to asphalitine
1 weight %), sulfur content be more than 0.8 weight % (preferably 0.8-3 weight %)).Further, since the preparation method energy of the present invention
Enough it is applied to the poor catalytic cracked oil pulp of property, the raw material sources thus, it is possible to extend needle coke.
Other features and advantages of the present invention will be described in detail in subsequent specific embodiment part.
Description of the drawings
Accompanying drawing is, for providing a further understanding of the present invention, and to constitute the part of description, with following tool
Body embodiment is used for explaining the present invention together, but is not construed as limiting the invention.In the accompanying drawings：
Fig. 1 is the schematic diagram for implementing the equipment of the method for preparing needle-shape coke raw material of present invention offer.
Specific embodiment
Hereinafter the specific embodiment of the present invention is described in detail.It should be appreciated that described herein concrete
Embodiment is merely to illustrate and explains the present invention, is not limited to the present invention.
The method for preparing needle-shape coke raw material of the invention, its method include to heat through heating furnace radiant section
Delayed coking reaction is carried out in mixed material injection coke drum, and the oil gas that delayed coking reaction is produced is carried out into fractional distillation, obtained
Wax oil component；Wherein, the mixed material contains catalytic cracked oil pulp and delayed coking raw material, in delayed coking reaction process
In, cooling oil and/or cooling water are injected by pipeline in the coke drum top, steam is injected in coke drum bottom, inject cold
But the pipeline of oil and/or cooling water is stretched in coke drum, and is catalyzed containing desulfurization, denitrogenation in the cooling oil and/or cooling water
Agent.
Preferably, inject cooling oil and/or the pipeline of cooling water is extended vertically in coke drum.
Preferably, length of the mixed material in coke drum feed entrance point apart from cylinder lower end accounts for whole barrel lenght
5/10～7/10.Here, the length of the cylinder refers to that cylinder is connected with bottom cone with coke drum upper cover connecting portion and cylinder
Vertical dimension between socket part；Length of the mixed material in coke drum feed entrance point apart from cylinder lower end refers to feed entrance point
To cylinder and the vertical dimension of bottom cone connecting portion.
Top of coke tower can adopt conventional end socket, for example, can be dome head or ellipsoidal head.Work as top of coke tower
During using dome head, the length of pipeline for stretching into injection cooling oil and/or cooling water in coke drum is the 1- of coke drum diameter
45%, preferably 20-35%.When top of coke tower uses ellipsoidal head, the length of pipeline of cooling oil and/or cooling water is injected
For the 1-22% of coke drum diameter, preferably 12-20%.
In the present invention, big oil will not be directly carried in order to ensure cooling oil and/or cooling water by pipeline injection
In gas pipeline, the opening diameter for injecting the pipeline of cooling oil and/or cooling water is preferably 10-50 millimeters, more preferably 20-
30 millimeters.
In the present invention, in order to further remain with the aromatic component beneficial to production needle coke, preferably in the coke drum
Top cooling oil and cooling water are injected by pipeline.In this case, cooling oil and cooling water can pass through pipeline respectively
Injection, it is also possible to injected by same pipeline as a mixture, preferably the two is respectively by pipeline injection.
When cooling oil being injected and during cooling water by pipeline at the top of the coke drum, the cooling oil and the cooling
The weight ratio of the injection rate of water can be 0.01-1：1, preferably 0.1-0.3：1.
Total consumption of the cooling oil and the cooling water can be 0.01- with the weight ratio of the consumption of the mixed material
0.25：1, preferably 0.01-0.10：1.For the cooling oil and total consumption of the cooling water, if only injecting described cold
But oil and be not injected into the cooling water, then total consumption list refers to the injection rate of the cooling oil；If only injecting the cooling
Water and be not injected into the cooling oil, then total consumption list refers to the injection rate of the cooling water；If while the injection cooling
Oily and described cooling water, then total consumption refer to the injection rate sum of the two.
In the present invention, to the desulfurization, the species of denitrification catalyst and consumption, there is no particular limitation, can be with routine
Consumption is using the conventional desulfurization in this area, denitrification catalyst.As such catalyst can for example be with nickel-molybdenum, molybdenum-cobalt,
The catalyst for active component such as nickel-cobalt, nickel-molybdenum-cobalt.
Preferably, on the basis of the consumption of the mixed material, the desulfurization, the consumption of denitrification catalyst are 100-
10000ppm (more preferably 500-2000ppm).That is, in the present invention, (weighed with the injection rate of the mixed material
Amount) on the basis of, the desulfurization, the injection rate of denitrification catalyst are preferably 100-10000ppm (more preferably 500-2000ppm).
In the present invention, the cooling oil can be various quench oils commonly used in the art.In the preferred case, institute
The petroleum distillate that cooling oil is that boiling range is 100-450 DEG C is stated, more preferably boiling range is 250-380 DEG C of petroleum distillate.
In the present invention, the cooling water can in fresh water, softened water, demineralized water, deaerated water and condensate extremely
Few one kind, preferably demineralized water.
In the present invention, the mixed material can be heated to 490-515 DEG C before the coke drum is injected, preferably
492-500℃。
In the present invention, in order to keep green coke duct and reduce the time of staying that secondary response component easily occurs, this method
Select to inject steam in coke drum bottom, while in order to reduce the impact after steam injection to catalyst, the injection rate of steam is needed
It is controlled.Steam can be 0.01-0.05 with the weight ratio of the consumption of mixed material:1, preferably 0.01-0.02:1.
Can be carried out by pipeline in coke drum bottom injection steam, the opening diameter of the pipeline is not particularly limited
It is fixed, can for example be 10-50 millimeters, preferably 20-30 millimeters.
As the present invention is to the less demanding of catalytic cracked oil pulp property, therefore obtain from catalytic cracking fractionating tower bottom of towe
Catalytic cracked oil pulp directly can be used, and without the need for carrying out other process before the use.As from catalytic cracking fractional distillation
The catalytic cracked oil pulp that tower bottom of towe is obtained, its fragrance point content are usually above 50 weight %.
The delayed coking raw material can be various conventional delayed coking raw material commonly used in the art, for example can be with
For in decompression residuum, reduced crude, visbroken resids, heavy deasphalted oil, viscous crude, topped crude, shale oil and liquefied coal coil
At least one.The crude oil that the viscous crude refers to asphalitine and gum level is higher and viscosity is larger.
In order that the mixed material can be heated in the range of said temperature before the coke drum is injected, preferably
The outlet temperature of the heating furnace radiant section is 490-515 DEG C；More preferably 492-500 DEG C
In the present invention, the condition of the delayed coking reaction includes：Coke pressure tower be 0.05-0.25MPa, coking week
Phase is 18-36h；It is preferred that coke pressure tower is 0.12-0.17MPa, coking cycle is 24-36h.In the present invention, pressure is referred to
Absolute pressure.
In the present invention, the scope of the feed weight ratio of the catalytic cracked oil pulp and the delayed coking raw material can be
Change in wide scope.It is preferred that the catalytic cracked oil pulp is 0.1 with the feed weight ratio of the delayed coking raw material：99.9～
99.9:0.1, more preferably 20:80～50:50.
Additionally, in the present invention, there is no particular limitation for the coke drum, can be various Jiao commonly used in the art
Charcoal tower.
In the present invention, the coke drum tower top oil gas by delayed coking reaction is produced carries out fractional distillation, obtains wax oil group
Point.The fractional distillation can be carried out in fractionating column, and the condition of the fractional distillation includes：100～145 DEG C of fractionator overhead temperature, point
Evaporate column overhead 0.13～0.17MPa of pressure, 310～360 DEG C of fractionating column column bottom temperature.
In the present invention, the wax oil component refers to boiling range in 350-450 DEG C or so of distillate.
In one embodiment, the group technology of the invention is implemented in equipment as shown in Figure 1, specifically,
The equipment mainly includes：Blender 3, delay coking heating furnace, delayed coker fractionator 7 and delayed coking coke drum 6.Postpone
Coking raw material oil 1 is mixed in blender 3 with catalytic cracked oil pulp 2, after being then extracted optionally with coker gas oil, coking
(do not mark in Fig. 1) into heating furnace convection section 4 after wax oil, the heat exchange of coking wax slop, be divided into two strands Jing after convection section heating and enter
Material (i.e. upper feeding and lower charging) into the bottom of coking fractional distillation column 7, fractionating column bottom from coke drum 6 high-temperature oil gas 12
The liquid phase stream formed after exchanging heat with raw oil upper feeding and coking wax slop 17 charging under fractionation column base with raw oil is mixed
Conjunction forms fractionating column base oil 8, and fractionating column base oil 8 is sent to heating furnace radiant section 5 after extracting out, and heated stove radiant section is heated to target
Injecting coke drum 6 by pipeline 9 after temperature carries out coking reaction, while injecting steam by pipeline 18；The top of coke drum 6 sets
Cooling oil supply pipeline 10 and/or cooling water supply pipeline 11 are equipped with, pass through cooling oil supply pipeline 10 during green coke
And/or the injection cooling oil of cooling water supply pipeline 11 and/or cooling water, wherein, containing de- in the cooling oil and/or cooling water
Sulfur, denitrification catalyst；The coke of generation is stayed in coke drum 6, and the high-temperature oil gas of generation are transported in fractionating column 7 by pipeline 12
Separated, obtained rich tail gas of coking plant 13, coker gasoline 14, coker gas oil 15 and wax tailings 16；Wax tailings 16 are needle-like
Burnt raw material.In the above-described embodiment, the recycle ratio (difference of Fractionator Bottom weight of oil and the upper and lower feed weight sum in fractionating column bottom
Value ratio again with the upper and lower feed weight sum in fractionating column bottom) can be 0.05-0.8:1, preferably 0.1-0.3:1.At this
In invention, wax tailings (i.e. described wax oil component) refer to boiling range in 350-450 DEG C or so of distillate；Coking wax slop is referred to
Heavy wax oil of the initial boiling point higher than 430 DEG C.
The invention will be further described by the following examples.
Embodiment 1
The present embodiment is used for the preparation method of the needle-shape coke raw material for illustrating present invention offer.
The present embodiment is using the flow process shown in Fig. 1.Coking raw material decompression residuum 1 (relevant parameter is as shown in table 1) and catalysis
Cracking slurry oil 2 (relevant parameter is as shown in table 1) presses 75 in blender 3:25 ratio is mixed, with coking bavin after extraction
Oil, coking stage casing oil, wax tailings, coking wax slop (do not mark heat exchange) into heating furnace convection section 4 after exchanging heat successively in figure
Preheating, is then divided into upper and lower two bursts of chargings into 7 bottom of fractionating column, fractionating column bottom from coke drum 6 high-temperature oil gas 12
The liquid phase stream formed after being exchanged heat with raw oil upper feeding, coking wax slop 17 is mixed with charging under raw oil in fractionation column base
Fractionating column base oil 8 is formed, fractionating column base oil 8 is sent to heating furnace radiant section 5 after extracting out, and recycle ratio is 0.2：1, heated stove radiation
Section 5 is reacted for the coke drum 6 of dome head and under 0.15MPa into tower top by pipeline 9 after being heated to 495 DEG C, together
When coke drum bottom by pipeline 18 inject steam；Length of the coke drum feed entrance point apart from cylinder lower end accounts for whole barrel lenght
1/2, meanwhile, tower top by pipeline 10 inject as cooling oil coking stage casing oil (be derived from fractionating column 7, boiling range be 250～
380 DEG C) and the demineralized water (temperature is 30 DEG C) as cooling water is injected by pipeline 11, while adding in the cooling oil of pipeline 10
Plus catalyst, pipeline 10 and pipeline 11 extend in coke drum, and the opening diameter of pipeline 10 and pipeline 11 is 20mm, 10 He of pipeline
Pipeline 11 stretches into the length in coke drum and is respectively the 30% of coke drum diameter, and cooling oil is 0.1 with the weight ratio of demineralized water：1,
The total injection of cooling oil and demineralized water is 0.05 with the weight ratio of mixed feeding injection rate：Containing de- in 1, also, cooling oil
Sulfur, denitrification catalyst (catalyst containing nickel-molybdenum-cobalt active component), on the basis of the injection rate of mixed feeding, with cooling oil
The injection rate of the catalyst of injection is 500ppm；Coke tower bottom steam is by pipeline 18 (opening diameter is injected for 20mm), steam
Injection rate and mixed feeding injection rate weight ratio be 0.02:1；Coke drum green coke cycle 24h, the coke of generation stay in coke
In tower, the high-temperature oil gas of generation are separated in fractionating column 7, and (separation condition is fractionation column pressure on top surface 0.15MPa, fractional distillation
332 DEG C of tower column bottom temperature, 126 DEG C of fractionator overhead temperature), obtain rich tail gas of coking plant 13, coker gasoline 14, coker gas oil 15 and Jiao
Change wax oil 16, wax tailings 16 are needle-shape coke raw material.The product slates for finally obtaining and the property of the needle-shape coke raw material of gained
Matter is as shown in table 2.
Comparative example 1
Method according to embodiment 1 is carried out, and does not except for the difference that inject cooling oil and cooling water in the coke drum 4, most
The product slates for obtaining afterwards and the property of the needle-shape coke raw material of gained are as shown in table 2.
Comparative example 2
Method according to embodiment 1 is carried out, and does not except for the difference that inject steam in the coke drum 4, the product for finally obtaining
The property of the needle-shape coke raw material of product distribution and gained is as shown in table 2.
Embodiment 2
The present embodiment is used for the preparation method of the needle-shape coke raw material for illustrating present invention offer.
Carried out using the method for embodiment 1, except for the difference that：Decompression residuum and catalytic cracked oil pulp in a mixer according to
70:30 ratio is mixed；Furnace outlet temperature is 496 DEG C；Coke pressure tower is 0.16MPa；Recycle ratio is 0.25：1；
Length of the coke drum feed entrance point apart from cylinder lower end accounts for the 3/5 of whole barrel lenght；Replaced with the same amount of cooling water
The cooling oil (in the same amount of cooling water containing with the same amount of desulfurization of the cooling oil, denitrification catalyst), and it is described
The injection rate of cooling water is identical with the total injection of cooling water and the cooling oil described in embodiment 1；Coke tower bottom steam leads to
Pipeline 18 (opening diameter is injected for 30mm) is crossed, the injection rate of steam is 0.01 with the weight ratio of mixed feeding injection rate:1.Most
The product slates for obtaining afterwards and the property of the needle-shape coke raw material of gained are as shown in table 2.
Embodiment 3
The present embodiment is used for the preparation method of the needle-shape coke raw material for illustrating present invention offer.
Using carrying out with the method for embodiment 1, except for the difference that：Decompression residuum and catalytic cracked oil pulp in a mixer according to
65:35 ratio is mixed；Furnace outlet temperature is 497 DEG C；Coke pressure tower is 0.17MPa；Recycle ratio is 0.3：1；
Length of the coke drum feed entrance point apart from cylinder lower end accounts for the 7/10 of whole barrel lenght；Replaced with the same amount of cooling oil
The cooling water, the injection rate of the cooling oil are identical with the total injection of cooling water and the cooling oil described in embodiment 1,
And on the basis of the injection rate of mixed feeding, the injection rate of the catalyst injected with cooling oil is 2000ppm.The product for finally obtaining
The property of the needle-shape coke raw material of product distribution and gained is as shown in table 2.
Embodiment 4
The present embodiment is used for the preparation method of the needle-shape coke raw material for illustrating present invention offer.
Method according to embodiment 1 is carried out, except for the difference that：Furnace outlet temperature is 498 DEG C；Coke pressure tower is
0.17MPa；Recycle ratio is 0.15：1.The product slates for finally obtaining and the property of the needle-shape coke raw material of gained are as shown in table 2.
Embodiment 5
The present embodiment is used for the preparation method of the needle-shape coke raw material for illustrating present invention offer.
Method according to embodiment 3 is carried out, except for the difference that：Furnace outlet temperature is 498 DEG C；Recycle ratio is 0.2：1.Most
The product slates for obtaining afterwards and the property of the needle-shape coke raw material of gained are as shown in table 2.
Embodiment 6
The present embodiment is used for the preparation method of the needle-shape coke raw material for illustrating present invention offer.
Method according to embodiment 3 is carried out, and except for the difference that pipeline 10 and pipeline 11 stretch into length in coke drum and be respectively Jiao
The 20% of charcoal tower diameter.The product slates for finally obtaining and the property of the needle-shape coke raw material of gained are as shown in table 3.
Embodiment 7
The present embodiment is used for the preparation method of the needle-shape coke raw material for illustrating present invention offer.
Method according to embodiment 3 is carried out, and except for the difference that top of coke tower uses ellipsoidal head, and pipeline 10 and pipeline 11
Stretch into length in coke drum and be respectively the 12% of coke drum diameter.The product slates for finally obtaining and the needle-shape coke raw material of gained
Property it is as shown in table 3.
Embodiment 8
The present embodiment is used for the preparation method of the needle-shape coke raw material for illustrating present invention offer.
Method according to embodiment 3 is carried out, and except for the difference that, top of coke tower uses ellipsoidal head, and pipeline 10 and pipeline
11 stretch into length in coke drum is respectively the 20% of coke drum diameter.The product slates for finally obtaining and the needle coke of gained are former
The property of material is as shown in table 3.
Embodiment 9
Method according to embodiment 3 is carried out, and except for the difference that pipeline 10 and pipeline 11 stretch into length in coke drum and be respectively Jiao
The 5% of charcoal tower diameter.The product slates for finally obtaining and the property of the needle-shape coke raw material of gained are as shown in table 3.
Embodiment 10
Method according to embodiment 1 is carried out, except for the difference that：Cooling oil is 0.3 with the weight ratio of demineralized water：1, cooling oil and
The total injection of demineralized water is 0.1 with the weight ratio of mixed feeding injection rate：1；The injection rate of coke tower bottom steam be mixed into
The weight ratio of material injection rate is 0.01:1.The product slates for finally obtaining and the property of the needle-shape coke raw material of gained such as 3 institute of table
Show.
Table 1
Table 2
Table 3
The preferred embodiment of the present invention described in detail above, but, the present invention is not limited in above-mentioned embodiment
Detail, the present invention range of the technology design in, various simple variants can be carried out to technical scheme, this
A little simple variants belong to protection scope of the present invention.
It is further to note that each particular technique feature described in above-mentioned specific embodiment, in not lance
In the case of shield, can be combined by any suitable means, in order to avoid unnecessary repetition, the present invention to it is various can
The compound mode of energy is no longer separately illustrated.
Additionally, combination in any between a variety of embodiments of the present invention, can also be carried out, as long as which is without prejudice to this
The thought of invention, which should equally be considered as content disclosed in this invention.
Claims (15)
1. a kind of method for preparing needle-shape coke raw material, it is characterised in that the method includes to heat through heating furnace radiant section
Delayed coking reaction is carried out in mixed material injection coke drum, and the oil gas that delayed coking reaction is produced is carried out into fractional distillation, obtained
Wax oil component；Wherein, the mixed material contains catalytic cracked oil pulp and delayed coking raw material, in delayed coking reaction process
In, cooling oil and/or cooling water are injected by pipeline in the coke drum top, steam is injected in coke drum bottom, inject cold
But the pipeline of oil and/or cooling water is stretched in coke drum, and is catalyzed containing desulfurization, denitrogenation in the cooling oil and/or cooling water
Agent.
2. method according to claim 1, wherein, when top of coke tower uses dome head, stretch into the note in coke drum
Enter 1-45% of the length of pipeline of cooling oil and/or cooling water for coke drum diameter.
3. method according to claim 1, wherein, when top of coke tower uses ellipsoidal head, injection cooling oil and/or
1-22% of the length of pipeline of cooling water for coke drum diameter.
4. method according to claim 1, wherein, in the mixed material, the catalytic cracked oil pulp and coking raw material
Weight ratio be 0.1:99.9～99.9:0.1.
5. method according to claim 1, wherein, the mixed material is in coke drum feed entrance point apart from cylinder lower end
Length accounts for the 5/10～7/10 of whole barrel lenght.
6. the method according to any one in claim 1-5, wherein, inject the pipeline of cooling oil and/or cooling water
Opening diameter is 10-50 millimeters.
7. method according to claim 1, wherein, cooling oil and cooling are injected by pipeline at the top of the coke drum
Water, and the cooling oil and the weight ratio of the cooling water are 0.01-1：1.
8. the method according to claim 1 or 7, wherein, total consumption of the cooling oil and the cooling water is mixed with described
The weight ratio for closing the consumption of raw material is 0.01-0.25：1.
9. method according to claim 1, wherein, on the basis of the consumption of the mixed material, the desulfurization, denitrogenation are urged
The consumption of agent is 100-10000 weight ppm.
10. the method according to claim 1 or 7, wherein, the cooling oil is boiling range for 100-450 DEG C of petroleum distillate.
11. methods according to claim 1 or 7, wherein, the cooling water is demineralized water and/or deaerated water.
12. methods according to claim 1, wherein, the mixed material was heated to before the coke drum is injected
490-515℃。
13. methods according to claim 1, wherein, the weight of the steam and mixed material consumption of coke drum bottom injection
Than for 0.01-0.05:1.
14. methods according to any one in claim 1,4 and 12, wherein, the delayed coking raw material is normal pressure slag
One kind in oil, decompression residuum, visbroken resids, heavy deasphalted oil, viscous crude, topped crude, shale oil and liquefied coal coil or
It is various.
15. methods according to any one in claim 1-7 and 12, wherein, the condition bag of the delayed coking reaction
Include：Coke pressure tower is 0.05-0.25MPa, coking cycle 18-36h.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410601630.4A CN105623720B (en) | 2014-10-31 | 2014-10-31 | Method for preparing raw material for needle-like coke |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
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| CN201410601630.4A CN105623720B (en) | 2014-10-31 | 2014-10-31 | Method for preparing raw material for needle-like coke |
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| CN1289819A (en) * | 1999-09-29 | 2001-04-04 | 中国石油化工集团公司 | Coking delay process for lowering foam layer in coke tower |
| CN101724421A (en) * | 2008-10-29 | 2010-06-09 | 中国石油化工股份有限公司 | Production method of needle coke |
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| US8007660B2 (en) * | 2008-06-03 | 2011-08-30 | Graftech International Holdings Inc. | Reduced puffing needle coke from decant oil |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN1289819A (en) * | 1999-09-29 | 2001-04-04 | 中国石油化工集团公司 | Coking delay process for lowering foam layer in coke tower |
| CN101724421A (en) * | 2008-10-29 | 2010-06-09 | 中国石油化工股份有限公司 | Production method of needle coke |
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