CN106635150B - Catalytic cracking delayed coking group technology prepares needle coke method - Google Patents
Catalytic cracking delayed coking group technology prepares needle coke method Download PDFInfo
- Publication number
- CN106635150B CN106635150B CN201510730061.8A CN201510730061A CN106635150B CN 106635150 B CN106635150 B CN 106635150B CN 201510730061 A CN201510730061 A CN 201510730061A CN 106635150 B CN106635150 B CN 106635150B
- Authority
- CN
- China
- Prior art keywords
- coking
- oil
- accordance
- section
- baffle plate
- 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
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Coke Industry (AREA)
Abstract
The invention discloses a kind of method that catalytic cracking delayed coking group technology prepares needle coke, methods described includes herein below：Catalytically cracked stock is reacted into catalytic cracking unit, and gas, light oil, intermediate oil and catalytic slurry are obtained after the Oil-gas Separation of generation；Intermediate oil and catalytic slurry enter coking tower, and gas, light oil and recycle oil are obtained after reacting the Oil-gas Separation of generation, and when coking heater starts two sections of heatings, intermediate oil is mixed into coking tower with recycle oil, until reaction time terminates.The inventive method is advantageous to the formation of large area wide area interphase, may advantageously facilitate " drawing burnt " effect of wide area interphase.
Description
Technical field
The present invention relates to a kind of method for preparing needle coke, and work is combined more particularly to a kind of catalytic cracking-delayed coking
The method that skill prepares needle coke.
Background technology
Needle coke has the characteristics that CTE is low, easy graphitization, is the preferred material for producing high power and ultra high power graphite electrode
Material.In the forming process of needle coke, feedstock oil needs to undergo the generation of mesophasespherule, grows up, melts and wait course, develops
For wide area interphase, line style texture structure is then formed in the presence of air-flow again, needle coke is made in final curing.At the beginning of coking
Phase, excessive disturbance is avoided the occurrence of inside system, to ensure that mesophasespherule slowly, is smoothly developed, the hair of interphase
Educate the properties of product that degree direct influence needle coke；In " drawing burnt " stage, system domestic demand constantly will have air-flow at the uniform velocity to escape, will
Wide area interphase pulls into linear structure.
CN103045301 discloses a kind of method that needle coke is prepared using catalytic cracked oil pulp as raw material, works as delayed coking
When unit capacity reaches the 60%~80% of its processing total amount, remaining cut after oil separates out gasoline will be generated and fully enter delay
For coking plant as burnt gas is drawn, obtained needle coke has high microsteping structure.
CN103184057 discloses a kind of method for preparing homogeneous petroleum needle coke.This method in initial reaction stage, raw material with
Lower temperature enter coking tower formed interphase liquid crystal, with the raising of furnace temp, raw material mix successively heavy distillate and
Intermediate oil enters coking tower together, finally make it that temperature reaches 510 DEG C in coking tower.
, it is necessary to provide mitigation, a stable environment for the formation of wide area interphase in needle coke preparation process, avoid
There is excessive disturbance in reaction system.On the contrary, in the pyrogenetic reaction middle and later periods, need constantly there is air-flow at the uniform velocity to escape inside system again
Go out, wide area interphase is pulled into line style texture structure.In addition, in " drawing burnt " stage, generally use systemic circulation is fed than mode, with
Guarantee has enough gas to be escaped from system, and the circulation oil mass of coking tower itself generation tend not to meet systemic circulation than
Demand.
The content of the invention
In view of the shortcomings of the prior art, the present invention provides a kind of method for preparing needle coke.Coking tower passes through in this method
Using upper feeding and lower feed combinations mode, in initial reaction stage, charging is effectively eliminated in wide area by upper feeding mode
Between mutually form the disturbance brought；In the later stage in the reaction, La Jiao and heat supply can be played dual parts of by lower feeding manner.For
The deficiency of delayed coking circulation oil mass is made up, catalytic cracking unit recycle oil is passed through delayed coking unit, it is ensured that is had enough
Air-flow " draw burnt ".
The present invention provides a kind of method that Integration of Resid Fcc And Delayed Coking prepares needle coke, and methods described includes
Herein below：
（1）Catalytically cracked stock reacts into catalytic cracking unit, and the oil gas of generation is discharged into from tower top urges
Change cracking fractionating system, gas, light oil, intermediate oil and catalytic slurry are obtained after separation；
（2）Step（1）The intermediate oil and catalytic slurry of generation are after coking heater is heated to 430~490 DEG C
Coking tower is entered by the enterprising material mouth of coking tower, the oil gas for reacting generation is discharged into coker fractionation system from tower top, separation
After obtain gas, light oil and recycle oil, described coking heater using one section of constant temperature-three sections of constant temperature of-two sections of heatings program
Warming temperature mode, wherein, one section of constant temperature is 430~490 DEG C of 10~25h of constant temperature, and two sections of heatings are with 1~5 DEG C/h speed liter
To 490 DEG C~510 DEG C；Three sections of constant temperature are 490~510 DEG C of 1~5h of constant temperature；
（3）When coking heater, which terminates one section of constant temperature, starts two sections of heatings, stopping is fed by enterprising material mouth, step
（1）The intermediate oil and step of generation（2）The recycle oil mixing of generation, enters after coking heater heats under coking tower
Material mouth enters coking tower, until reaction time terminates, the needle coke of generation is deposited on coking section bottom.
In the inventive method, described coking heater uses the temperature programming of one section of constant temperature-three sections of constant temperature of-two sections of heatings
Mode of operation, wherein, one section of constant temperature is 430~490 DEG C of 10~25h of constant temperature, and two sections of heatings rise to 490 with 1~5 DEG C/h speed
~510 DEG C；Three sections of constant temperature are 490~510 DEG C of 1~5h of constant temperature；When heating furnace is in one section of constant temperature, intermediate oil and catalysis
Slurry oil enters coking tower by the enterprising material mouth of coking tower；When heating furnace, which terminates one section of constant temperature, starts two sections of heatings, stop logical
Enter catalytic slurry, intermediate oil and recycle oil and coking tower is entered by lower charging aperture, until filling burnt end cycle.
In the inventive method, the coking tower includes cylinder, upper cover and low head, and the cylinder is from top to bottom set successively
Coking section and packing section to be put, is provided with baffle plate between coking section and packing section, the baffle plate is the baffle plate with sieve aperture, coking section,
Baffle plate is fixedly connected with packing section by flange, enterprising material mouth is set on the cylinder of the coking section, under the low head setting
Charging aperture, lower charging aperture connect with packing section.
In the coking tower, the packing section is highly 1/20~1/2, preferably the 1/20~1/5 of coking tower total height.
In the coking tower, the enterprising material mouth is located at the middle and upper part of the coking section of coking tower, apart from the bottom of towe of coking tower
Highly it is the 3/5~4/5 of total tower height.
In the coking tower, the baffle plate is the baffle plate with sieve aperture, and the baffle plate sieve aperture is shaped as square, rectangular
Shape, triangle, it is circular in one kind, it is preferably circular；Slot size is 0.1mm~10mm, preferably 1mm~5mm, and sieve aperture edge is kept off
Plate is radially distributed in concentric circles, and total percent opening of baffle plate is 5%~50%, can be uniform pore openings rate or non-homogeneous opens
Porosity, preferably non-uniform perforation, when for non-uniform perforation when, gradually increase from the center of circle along baffle plate radial direction screen-aperture
Big or sieve aperture quantity gradually increases.
In the coking tower, filling heatproof in the packing section, pressure-resistant, corrosion resistant inert filler, the filler can be with
For the one or more in stainless steel, ceramics, inertia silica, its shape can be Raschig ring, Pall ring or non-porous
Granulated filler, the main function of filler is to make to be not easy coking material along tower radial dispersion, avoids being not easy coking Concentration of matter
In tower central shaft area.
In the inventive method, step（1）Described catalytically cracked stock is Conventional catalytic cracking feedstock oil, including normal pressure
One or more of mixing in hydrogenated residue, decompression hydrogenated residue, low-sulfur straight-run gas oil, low-sulfur wax tailings etc..Catalytic cracking
Device can be more than a set of or a set of, and a reactor, a regenerator are comprised at least per covering device.Catalytic cracking unit is pressed
Operated according to this area normal condition：Reaction temperature is 480 DEG C~530 DEG C, and regeneration temperature is 650 DEG C~750 DEG C, oil ratio 2
~10（Mass ratio）, the MPa of pressure 0.1MPa~0.5.Catalyst used in catalytic cracking unit is conventional catalyst, including silicon
Al catalysts, silica-magneia cataslyst or X-type, Y types, ZSM-5 equimolecular sieve catalysts.
In the inventive method, step（1）The intermediate oil boiling range that described catalytic cracking fractionating system is isolated is 350
DEG C~500 DEG C, preferably 375 DEG C~490 DEG C, than intermediate oil weight cut be catalytic slurry, it is desirable to intermediate oil with
S ≯ 0.5% of catalytic slurry（Quality meter）.
In the inventive method, step（2）Described in intermediate oil and catalytic slurry is filtered removes the ash that wherein contains
In ash content ≯ 0.1% into coking heater, contained in the intermediate oil and catalytic slurry after filtering after point（Quality meter）.
In the inventive method, described coking heater uses the temperature programming of one section of constant temperature-three sections of constant temperature of-two sections of heatings
Mode of operation, wherein, one section of constant temperature is 440~480 DEG C of 12~18h of constant temperature；Two sections of heatings are risen to 1~5 DEG C/h speed
490~510 DEG C；Three sections of constant temperature are 495 DEG C~505 DEG C constant temperature 2h~4h.
In the inventive method, the operation temperature of the coking tower is 410 DEG C~505 DEG C, operating pressure be 0.5 MPa~
2MPa, it can be constant voltage operation or become press operation.
In the inventive method, the lower gating location at described coking tower bottom is the position of Conventional delayed coking charging aperture.
In the inventive method, step（2）The recycle oil that described coker fractionation system is isolated is>200 DEG C of distillates, it is excellent
Choosing>350 DEG C of distillates.
In the inventive method, step（3）Described recycle oil inlet amount is the 0.1~2 of intermediate oil inlet amount（Quality
Than）.
Compared with prior art, coking tower of the present invention and prepare the method for needle coke and have the following advantages that：
1st, at pyrogenetic reaction initial stage, intermediate oil and catalytic slurry enter coking tower using upper feeding mode, avoided
Cause system disturbance excessive due to the entrance of fresh feed, for the generation of mesophasespherule, grow up and melt and provide one
Individual mitigation, stable developing environment, are advantageous to the formation of large area wide area interphase；In the pyrogenetic reaction middle and later periods, from lower charging
Mouth is passed through intermediate oil and recycle oil, due to being both not easy coking, while system viscosity is reduced, with carrying for temperature
Height escapes in gaseous form, the linear velocity of the system internal gas flow of considerably increasing in axial direction, may advantageously facilitate among wide area
" drawing burnt " effect of phase.
2nd, the not no return mechanism in the form of recycle oil of the intermediate oil of catalytic cracking unit, the side passed through using one way
Formula, the burning load of catalytic cracking regenerator is greatly reduced, for maintenance system heat balance, catalytic cracking can be taken former
Expect the mode of oil residue, be advantageous to improve the economic benefit of catalytic cracking unit.
3rd, coking tower packing section and baffle plate play good peptizaiton to bottom feed, to air-flow along tower in the radial direction
It is scattered play facilitation, also cause being uniformly distributed for system temperature improved, greatly improve coke texture structure and
Performance.In the decoking stage, the flange of coking section, baffle plate and packing section junction is dismantled, removes baffle plate and packing section, is then carried out
Normal de-coking operations.For the coke adhered on filler, it can be burnt up in air atmosphere, not interfering with the circulation of filler makes
With.
Brief description of the drawings
Fig. 1 is the schematic flow sheet that Integration of Resid Fcc And Delayed Coking of the present invention prepares needle coke.
Fig. 2 is coking tower structural representation of the present invention.
Fig. 3~Fig. 5 is the optical texture photo that needle coke sample is prepared using the inventive method.
Embodiment
The process and effect of the present invention is further illustrated with reference to embodiment.Catalytically cracked stock 1 splits by catalysis
2 reactions are put in makeup, and the oil gas 3 of generation enters catalytic cracking fractionating system 4, isolates gas 5, light oil 6, the and of intermediate oil 7
Catalytic slurry 8；Wherein, intermediate oil 7 and catalytic slurry 8 filter by filter 11 and 9 respectively, are mixed after removing ash content
Oil 10 enters coking tower 14A/B after coking heater is heated to 430 DEG C~490 DEG C of one section of constant temperature stage from enterprising material mouth,
The oil gas 15 of generation separates by coker fractionation system 16, obtains gas 17, light oil 18 and recycle oil 19；When coking heater enters
When entering two sections of temperature rise periods, intermediate oil switches to circuit 13 from 12, is mixed with coking recycle oil 19, through coking heater plus
Enter coking tower from lower charging aperture after heat, until filling burnt end cycle.
As shown in Fig. 2 in the inventive method, the coking tower includes cylinder 1, upper cover 2 and low head 3, the cylinder 1
Coking section 4 and packing section 5 are from top to bottom set gradually, baffle plate 9 is provided between coking section 4 and packing section 5, the baffle plate 9 is band
There is the baffle plate of sieve aperture, coking section 4, baffle plate 9 and packing section 5 are fixedly connected by flange 10, are set on the cylinder of the coking section 4
Enterprising material mouth 8, the low head 3 set lower charging aperture 7, and lower charging aperture 7 connects with packing section 5.
Embodiment 1
Using coking tower of the present invention and the combined technical method for preparing needle coke, wherein the enterprising material mouth of coking tower away from
Highly it is the 4/5 of total tower height from bottom of towe, the height of bottom of towe packing section is the 1/10 of total tower height.
The fundamental property of catalytically cracked stock is shown in Table 1, and the process conditions of catalytic cracking unit are shown in Table 2, and catalyst uses
The trade mark is RICC-1 catalyst.Catalytic cracking production enters fractionating system, isolates gas, light oil, intermediate oil and urges
Carburetion is starched, wherein, intermediate oil and catalytic slurry pass through filtration treatment, and content of ashes is down to less than 0.1%.In addition, centre evaporates
It is 382 DEG C~459 DEG C to divide oily boiling range；Delayed coking generation recycle oil be>355 DEG C of cuts.
The fundamental property of the catalytically cracked stock of table 1
The process conditions of the catalytic cracking unit of table 2
Coking heater is controlled using alternating temperature, 440 DEG C of holding 16h of initial temperature, is then warming up to 4 DEG C/h speed
505 DEG C of holding 3h.When furnace outlet temperature is 440 DEG C of constant temperature, the intermediate oil of catalytic cracking unit generation and catalysis
Slurry oil enters coking tower from enterprising material mouth；When heating furnace is in the temperature programming stage, stopping is passed through catalytic slurry, midbarrel
Oil and the recycle oil of coking plant generation enter coking tower from lower charging aperture, until 505 DEG C of constant temperature terminate, wherein, recycle oil enters
Doses is 0.5 times of intermediate oil inlet amount.In whole course of reaction, temperature range is 425 DEG C~498 in coking tower
DEG C, constant pressure is 0.8MPa.The optical texture for the needle coke sample prepared is as shown in Figure 3.
Embodiment 2
Embodiment prepares needle coke using the inventive method, and the difference with embodiment 1 is, delayed coker operation bar
Part is different.
Coking heater is controlled using alternating temperature, 450 DEG C of holding 13h of initial temperature, is then warming up to 3 DEG C/h speed
505 DEG C of holding 2h.When furnace outlet temperature is 450 DEG C of constant temperature, the intermediate oil of catalytic cracking unit generation and catalysis
Slurry oil enters coking tower from enterprising material mouth；When heating furnace is in the temperature programming stage, stopping is passed through catalytic slurry, midbarrel
Oil and the recycle oil of coking plant generation enter coking tower from lower charging aperture, until 505 DEG C of constant temperature terminate, wherein, recycle oil enters
Doses is 1 times of intermediate oil inlet amount.In whole course of reaction, temperature range is 433 DEG C~497 DEG C in coking tower,
Constant pressure is 1.1MPa.The optical texture for the needle coke sample prepared is as shown in Figure 4.
Embodiment 3
Embodiment prepares needle coke using the inventive method, and the difference with embodiment 1 is, delayed coker operation bar
Part is different.
Coking heater is controlled using alternating temperature, 440 DEG C of holding 16h of initial temperature, is then warming up to 4 DEG C/h speed
500 DEG C of holding 2h.When furnace outlet temperature is 440 DEG C of constant temperature, the intermediate oil of catalytic cracking unit generation and catalysis
Slurry oil enters coking tower from enterprising material mouth；When heating furnace is in the temperature programming stage, stopping is passed through catalytic slurry, midbarrel
Oil and the recycle oil of coking plant generation enter coking tower from lower charging aperture, until 500 DEG C of constant temperature terminate, wherein, recycle oil enters
Doses is 1 times of intermediate oil inlet amount.In whole course of reaction, temperature range is 433 DEG C~497 DEG C in coking tower,
Initial pressure is 1.1MPa, and when furnace outlet temperature rises to 500 DEG C of constant temperature, pressure is down to 0.5MPa in 1h.Prepare
Needle coke sample optical texture it is as shown in Figure 5.
Claims (22)
1. a kind of method that Integration of Resid Fcc And Delayed Coking prepares needle coke, methods described includes herein below：
（1）Catalytically cracked stock reacts into catalytic cracking unit, and the oil gas of generation is discharged into catalysis from tower top and split
Change fractionating system, gas, light oil, intermediate oil and catalytic slurry are obtained after separation；
（2）Step（1）The intermediate oil and catalytic slurry of generation pass through after coking heater is heated to 430~490 DEG C
The enterprising material mouth of coking tower enters coking tower, and the oil gas for reacting generation is discharged into coker fractionation system from tower top, after separation
To gas, light oil and recycle oil, described coking heater uses the temperature programming of one section of constant temperature-three sections of constant temperature of-two sections of heatings
Mode of operation, wherein, one section of constant temperature is 430~490 DEG C of 10~25h of constant temperature, and two sections of heatings rise to 490 with 1~5 DEG C/h speed
DEG C~510 DEG C；Three sections of constant temperature are 490~510 DEG C of 1~5h of constant temperature；
（3）When coking heater, which terminates one section of constant temperature, starts two sections of heatings, stopping is fed by enterprising material mouth, step（1）It is raw
Into intermediate oil and step（2）The recycle oil mixing of generation, from the lower charging aperture of coking tower after coking heater heats
Into coking tower, until terminating reaction time, the needle coke of generation is deposited on coking section bottom.
2. in accordance with the method for claim 1, it is characterised in that：The coking tower includes cylinder, upper cover and low head, institute
State cylinder and from top to bottom set gradually coking section and packing section, baffle plate is provided between coking section and packing section, the baffle plate is band
There is the baffle plate of sieve aperture, coking section, baffle plate and packing section are fixedly connected by flange, and upper feeding is set on the cylinder of the coking section
Mouthful, the low head sets lower charging aperture, and lower charging aperture connects with packing section.
3. in accordance with the method for claim 2, it is characterised in that：The packing section highly for coking tower total height 1/20~
1/2。
4. in accordance with the method for claim 2, it is characterised in that：The packing section highly for coking tower total height 1/20~
1/5。
5. in accordance with the method for claim 2, it is characterised in that：On the enterprising material mouth is located in the coking section of coking tower
Portion, the bottom of towe apart from coking tower are highly the 3/5~4/5 of total tower height.
6. in accordance with the method for claim 2, it is characterised in that：The baffle plate is the baffle plate with sieve aperture, the baffle plate sieve
Hole is shaped as square, rectangle, one kind in triangle or circle.
7. in accordance with the method for claim 2, it is characterised in that：The baffle plate is the baffle plate with sieve aperture, the baffle plate sieve
Hole is shaped as circle.
8. according to the method described in claim 6 or 7, it is characterised in that：The slot size is 0.1mm~10mm.
9. according to the method described in claim 6 or 7, it is characterised in that：The slot size is 1mm~5mm.
10. according to the method described in claim 6 or 7, it is characterised in that：The sieve aperture is radially distributed along baffle plate in concentric circles,
Total percent opening of baffle plate is 5%~50%.
11. according to the method described in claim 6 or 7, it is characterised in that：The baffle plate is using uniform pore openings rate or non-homogeneous opens
Porosity, when for non-uniform perforation when, from the center of circle along baffle plate radial direction screen-aperture gradually increase or sieve aperture quantity by
It is cumulative more.
12. in accordance with the method for claim 2, it is characterised in that：It is filling heatproof in the packing section, pressure-resistant, corrosion resistant
Inert filler, the filler are the one or more in stainless steel, ceramics, inertia silica, and its shape is Raschig ring, Bauer
Ring.
13. in accordance with the method for claim 1, it is characterised in that：Step（1）Described catalytically cracked stock is urged to be conventional
Change one kind in cracked stock oil, including atmospheric hydrogenation residual oil, decompression hydrogenated residue, low-sulfur straight-run gas oil, low-sulfur wax tailings
Or several mixing.
14. in accordance with the method for claim 1, it is characterised in that：Step（1）Described catalytic cracking unit for it is a set of with
On, a reactor, a regenerator are comprised at least per covering device.
15. in accordance with the method for claim 1, it is characterised in that：Step（1）Described catalytic cracking unit operating condition：
Reaction temperature is 480 DEG C~530 DEG C, and regeneration temperature is 650 DEG C~750 DEG C, and oil ratio is 2~10, pressure 0.1MPa~0.5
MPa。
16. in accordance with the method for claim 1, it is characterised in that：Step（1）Described catalytic cracking fractionating system is isolated
Intermediate oil boiling range be 350 DEG C~500 DEG C, than intermediate oil weight cut be catalytic slurry, it is desirable to intermediate oil
With S ≯ 0.5% of catalytic slurry.
17. in accordance with the method for claim 1, it is characterised in that：Step（2）Described in intermediate oil and catalytic slurry warp
Filter off except, into coking heater, containing after the ash content that wherein contains in the intermediate oil and catalytic slurry after filtering
Ash content ≯ 0.1%.
18. in accordance with the method for claim 1, it is characterised in that：Described coking heater is risen using one section of-two sections of constant temperature
The temperature programmed work mode of warm-three sections of constant temperature, wherein, one section of constant temperature is 440~480 DEG C of 12~18h of constant temperature；Two sections of heatings
490~510 DEG C are risen to 1~5 DEG C/h speed；Three sections of constant temperature are 495 DEG C~505 DEG C constant temperature 2h~4h.
19. in accordance with the method for claim 1, it is characterised in that：The operation temperature of the coking tower is 410 DEG C~505 DEG C,
Operating pressure is 0.5 MPa~2MPa, constant voltage operation or change press operation.
20. in accordance with the method for claim 1, it is characterised in that：Step（2）What described coker fractionation system was isolated follows
Ring oil is>200 DEG C of distillates.
21. in accordance with the method for claim 1, it is characterised in that：Step（2）What described coker fractionation system was isolated follows
Ring oil is>350 DEG C of distillates.
22. in accordance with the method for claim 1, it is characterised in that：Step（3）Described recycle oil inlet amount is midbarrel
The 0.1~2 of oily inlet amount.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510730061.8A CN106635150B (en) | 2015-11-02 | 2015-11-02 | Catalytic cracking delayed coking group technology prepares needle coke method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510730061.8A CN106635150B (en) | 2015-11-02 | 2015-11-02 | Catalytic cracking delayed coking group technology prepares needle coke method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN106635150A CN106635150A (en) | 2017-05-10 |
| CN106635150B true CN106635150B (en) | 2018-02-09 |
Family
ID=58810534
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201510730061.8A Active CN106635150B (en) | 2015-11-02 | 2015-11-02 | Catalytic cracking delayed coking group technology prepares needle coke method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN106635150B (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109777458B (en) * | 2017-11-14 | 2021-04-06 | 中国石油化工股份有限公司 | Preparation method of high-quality needle coke |
Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5286371A (en) * | 1992-07-14 | 1994-02-15 | Amoco Corporation | Process for producing needle coke |
| CN101302434A (en) * | 2008-06-20 | 2008-11-12 | 中国石油大学(华东) | Process for preparing needle coke |
| CN101724420A (en) * | 2008-10-28 | 2010-06-09 | 中国石油化工股份有限公司 | Production method of needle coke raw material |
| CN103045301A (en) * | 2011-10-17 | 2013-04-17 | 中国石油化工股份有限公司 | Method for producing needle coke by catalytic cracking-delayed coking combination process |
| CN203820708U (en) * | 2014-04-17 | 2014-09-10 | 程志宇 | Filler tower for deeply processing coal tar and coproducing coal-based needle coke |
| CN104560155A (en) * | 2013-10-23 | 2015-04-29 | 中国石油化工股份有限公司 | Coking method |
| CN104560152A (en) * | 2013-10-23 | 2015-04-29 | 中国石油化工股份有限公司 | Coking process for production of needle coke |
| CN104560104A (en) * | 2013-10-23 | 2015-04-29 | 中国石油化工股份有限公司 | Method for producing needle coke |
-
2015
- 2015-11-02 CN CN201510730061.8A patent/CN106635150B/en active Active
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5286371A (en) * | 1992-07-14 | 1994-02-15 | Amoco Corporation | Process for producing needle coke |
| CN101302434A (en) * | 2008-06-20 | 2008-11-12 | 中国石油大学(华东) | Process for preparing needle coke |
| CN101724420A (en) * | 2008-10-28 | 2010-06-09 | 中国石油化工股份有限公司 | Production method of needle coke raw material |
| CN103045301A (en) * | 2011-10-17 | 2013-04-17 | 中国石油化工股份有限公司 | Method for producing needle coke by catalytic cracking-delayed coking combination process |
| CN104560155A (en) * | 2013-10-23 | 2015-04-29 | 中国石油化工股份有限公司 | Coking method |
| CN104560152A (en) * | 2013-10-23 | 2015-04-29 | 中国石油化工股份有限公司 | Coking process for production of needle coke |
| CN104560104A (en) * | 2013-10-23 | 2015-04-29 | 中国石油化工股份有限公司 | Method for producing needle coke |
| CN203820708U (en) * | 2014-04-17 | 2014-09-10 | 程志宇 | Filler tower for deeply processing coal tar and coproducing coal-based needle coke |
Also Published As
| Publication number | Publication date |
|---|---|
| CN106635150A (en) | 2017-05-10 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| WO2012161272A1 (en) | Monocyclic aromatic hydrocarbon production method and monocyclic aromatic hydrocarbon production plant | |
| CN106753551B (en) | A method of producing high-knock rating gasoline using catalytic cracking diesel oil | |
| CN101463274B (en) | Improved hydrocarbon oil hydrotreating and catalytic cracking combined technique | |
| CN107603671B (en) | A kind of system and method for adding hydrogen to produce mesophase pitch and oil product based on middle coalite tar | |
| CN106635157B (en) | A kind of lightening method of inferior feedstock oil | |
| CN1923971A (en) | Catalytic conversion method capable of increasing propylene yield | |
| CN102533332A (en) | Method for comprehensively using all fractions produced through hydrogenation combined with delayed coking on coal tar | |
| CN103184057A (en) | Production method of homogeneous petroleum needle coke | |
| CN106635149B (en) | A kind of preparation method of needle coke | |
| CN106635143B (en) | A kind of method for preparing needle coke | |
| CN106635150B (en) | Catalytic cracking delayed coking group technology prepares needle coke method | |
| CN108264934B (en) | Suspension bed hydrogenation process for treating heavy oil | |
| RU2408653C1 (en) | Procedure for processing oil residues | |
| CN1926219A (en) | Down-flow fluidization catalytic cracking device and method | |
| CN108070403A (en) | A kind of method for producing jet fuel | |
| CN108238837A (en) | Method for producing low-carbon olefin by catalytic cracking | |
| CN85104806A (en) | Fluid catalytic cracking process and device | |
| CN101928587A (en) | Catalytic conversion method of hydrocarbon oil | |
| CN102268291B (en) | Catalytic cracking technology and device for reducing olefins in gasoline | |
| CN109929592A (en) | A kind for the treatment of process and system of ethylene bottom oil | |
| CN102086413B (en) | Hydrocarbon oil catalytic conversion method | |
| CN105733631A (en) | Needle coke preparation method and device | |
| CN106635101B (en) | Delayed coking tower and method for preparing needle coke | |
| CN102311796B (en) | Suspension bed hydrogenation process method | |
| US5324418A (en) | FCC process using high cat:oil ratios |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |