CN1011416B - Residual Oil Coking Process with Two-way Feed System - Google Patents
Residual Oil Coking Process with Two-way Feed SystemInfo
- Publication number
- CN1011416B CN1011416B CN 87102308 CN87102308A CN1011416B CN 1011416 B CN1011416 B CN 1011416B CN 87102308 CN87102308 CN 87102308 CN 87102308 A CN87102308 A CN 87102308A CN 1011416 B CN1011416 B CN 1011416B
- Authority
- CN
- China
- Prior art keywords
- oil
- feed system
- coking
- separation column
- heavy fraction
- 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.)
- Expired
Links
- 238000004939 coking Methods 0.000 title claims abstract description 40
- 238000000034 method Methods 0.000 title claims abstract description 39
- 239000000571 coke Substances 0.000 claims abstract description 35
- 238000004519 manufacturing process Methods 0.000 claims abstract description 22
- 239000002994 raw material Substances 0.000 claims description 24
- 238000000926 separation method Methods 0.000 claims description 21
- 238000006243 chemical reaction Methods 0.000 claims description 9
- 230000005855 radiation Effects 0.000 claims description 8
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical group [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 7
- 238000005194 fractionation Methods 0.000 claims description 4
- 239000000203 mixture Substances 0.000 claims description 4
- 230000001698 pyrogenic effect Effects 0.000 claims description 4
- 239000002893 slag Substances 0.000 claims 1
- 230000003111 delayed effect Effects 0.000 abstract description 16
- 238000010924 continuous production Methods 0.000 abstract description 3
- 239000003921 oil Substances 0.000 description 77
- 239000007789 gas Substances 0.000 description 17
- 239000002283 diesel fuel Substances 0.000 description 11
- 239000003502 gasoline Substances 0.000 description 11
- 239000007788 liquid Substances 0.000 description 11
- 238000010438 heat treatment Methods 0.000 description 10
- 238000005516 engineering process Methods 0.000 description 7
- 239000000047 product Substances 0.000 description 7
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 5
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 4
- 239000005864 Sulphur Substances 0.000 description 4
- 238000004227 thermal cracking Methods 0.000 description 4
- 238000005235 decoking Methods 0.000 description 3
- 239000011331 needle coke Substances 0.000 description 3
- 238000010792 warming Methods 0.000 description 3
- 239000001993 wax Substances 0.000 description 3
- PAYRUJLWNCNPSJ-UHFFFAOYSA-N Aniline Chemical compound NC1=CC=CC=C1 PAYRUJLWNCNPSJ-UHFFFAOYSA-N 0.000 description 2
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical group C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 2
- 239000005977 Ethylene Substances 0.000 description 2
- 241000282326 Felis catus Species 0.000 description 2
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 2
- 238000004231 fluid catalytic cracking Methods 0.000 description 2
- HYBBIBNJHNGZAN-UHFFFAOYSA-N furfural Chemical compound O=CC1=CC=CO1 HYBBIBNJHNGZAN-UHFFFAOYSA-N 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 229910052759 nickel Inorganic materials 0.000 description 2
- 229910052720 vanadium Inorganic materials 0.000 description 2
- LEONUFNNVUYDNQ-UHFFFAOYSA-N vanadium atom Chemical compound [V] LEONUFNNVUYDNQ-UHFFFAOYSA-N 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 238000003723 Smelting Methods 0.000 description 1
- 239000010692 aromatic oil Substances 0.000 description 1
- 238000007630 basic procedure Methods 0.000 description 1
- 238000001354 calcination Methods 0.000 description 1
- 238000004523 catalytic cracking Methods 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 239000011280 coal tar Substances 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 239000013078 crystal Substances 0.000 description 1
- 230000006837 decompression Effects 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000007701 flash-distillation Methods 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- 238000005087 graphitization Methods 0.000 description 1
- 229910001385 heavy metal Inorganic materials 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 239000000852 hydrogen donor Substances 0.000 description 1
- 238000005984 hydrogenation reaction Methods 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000012263 liquid product Substances 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 238000002203 pretreatment Methods 0.000 description 1
- 238000003672 processing method Methods 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Coke Industry (AREA)
Abstract
The present invention belongs to an improved method of delayed coking process. It features that the heavy fraction oil circulation and non-circulation combined process is used and the two systems of main feeding and secondary feeding are used. The tower bottom heavy distillate oil of the shared fractionating tower circulates in the auxiliary feeding system, and when wax oil is produced more, the circulation ratio is 0.1-0.3; when the middle distillate oil is produced more, the circulation ratio is 0.4-1.0.
The present invention has the advantages of flexible production of high quality coke, wax oil or middle fraction oil, and continuous production of high quality coke.
Description
The invention belongs to modified process of delayed coking technology.
Delay coking process is widespread use in refining of petroleum.This technology is to make the residual oil thermal conversion become the liquid and the coke of gas, different fractions, even low value residual oil is converted into the liquid product of high value, and produces some useful byproduct-gas and coke simultaneously.
The major equipment of delay coking process is process furnace, coke drum, separation column and mechanical facilities such as corresponding decoking, accumulating, its basic procedure: stock oil is after interchanger and the preheating of process furnace convection zone, be introduced at the bottom of the separation column, with coking oil gas heat exchange in separation column from the coke cat head, on the one hand the lightweight oil fractionation in the raw material is come out, heated raw material simultaneously again.Stock oil at the bottom of the separation column with pump into the process furnace radiation section after heavy distillate mixes, it is temperature required to be heated to pyrogenic reaction, enters coke drum and carries out pyrogenic reaction, the char build-up of generation switches to another coke drum and continues coking in coke drum after general 24 hours.After the coking oil gas that generates enters separation column bottom and stock oil heat exchange from the effusion of coke cat head, obtain gas, gasoline, diesel oil and wax oil caterpillar through fractionation, the heavy fraction oil that is difficult for gasification (is seen How DelaYedCoking Works with circulating after stock oil mixes, Hydrocarbon Processing, July 1971, PP87).
Because the ultra high power smelting technology of metallurgical industry is developed, and is growing to the demand of high-quality needle coke, therefore utilize delayed coking production high-quality Jiao's new technology constantly to occur.United States Patent (USP) 2775549 and 2922755 is described in detail and is produced the manufacture method of electrode with high-quality Jiao.United States Patent (USP) 3472761 proposes a cover delayed coking-thermally splitting machinery and produces the processing method of two kinds of grade refinery cokes, promptly produces common Jiao with conventional delayed coking, and the wax oil of generation is made the thermally splitting raw material, and thermal cracking residue is for delayed coking production high-quality Jiao.
United States Patent (USP) 3759822 and 4066532 has been introduced with ethylene residue and thermal cracking residue mixing, coal tar and fluid catalytic cracking decant oil and has been mixed the technology of making the burnt raw material of high-quality; United States Patent (USP) 4130475 and 4177133 proposes with long residuum and makes the method for high-quality Jiao raw material with the distilled oil of viscosity breaking flash distillation; United States Patent (USP) 4176046 and European patent 83143 introduction usefulness hydrogenation clarified oils (HydrotreatedDecant Oil) and hydrogen supply agent (Hydrogen Donor) are as production high-quality Jiao's raw material.The improvement of these technology and raising mainly are to select proper raw material oil or stock oil is carried out pre-treatment, make it to contain more aromatic hydrocarbons, being fit to wanting of production high-quality Jiao, but fail to enlarge high-quality Jiao's raw material sources.In fact, high-quality Jiao's raw material is the needs that can not satisfy the treatment capacity of delayed coking unit in the refinery, in the time of can only leaning on the way of storage and production high-quality Jiao, the time and produce common Jiao's stage production.
In order to improve liquid yield, the Recycle design of delayed coking also there have been many improvement, United States Patent (USP) 4455219 has been introduced and has been sneaked into a part of coker gas oil fraction in raw material, to reduce coking yield, increases liquid yield.In United States Patent (USP) 4492625 and 4501654, propose the raw material separated into two parts: a part circulates at the bottom of entering separation column routinely; Another part directly enters the process furnace radiation section, can reduce recycle ratio (being turning oil/stock oil) like this, improves liquid yield.In United States Patent (USP) 4518487, propose further to improve feeding manner, promptly replace heavy distillate to circulate fully with the coking solar oil, can increase liquid yield 5%.
The objective of the invention is to propose a kind ofly can improve liquid yield, again can production high-quality Jiao, and can be under the under-supply situation of the burnt stock oil of high-quality long-term continuous production high-quality Jiao's method.
Major equipment of the present invention is basic identical with conventional delayed coking, comprises two process furnace all the people present coke drums and a shared separation column.The invention is characterized in and adopted different feeding manners and Recycle design, promptly adopt to comprise the oil circulation and association system of the major and minor charging of round-robin not of heavy fraction.
Main feed system: raw material is directly sent into a process furnace heating after heat exchange, enter the coke drum of producing common Jiao then and carry out pyrogenic reaction, and reacted coking oil gas is gone into separation column by the coke drum jacking.
Secondary feed system: raw material enters the separation column bottom after heat exchange, mix the back by entering another process furnace radiation section heating at the bottom of the separation column with the heavy fraction oil in the separation column, enter production high-quality Jiao's coke drum again, the coking oil gas that reaction generates also enters the separation column shared with main feed system.Therefore not have heavy fraction oil circulation for main feed system, and the heavy fraction oil of major and minor feed system reactant all circulates in secondary feed system.
When secondary feed system production high-quality of the present invention is burnt, stock oil heats through 430～510 ℃ of alternating temperatures at the process furnace radiation section with the oily back of mixing of the heavy fraction at the bottom of the separation column, and under 490～510 ℃ of temperature, kept 5～8 hours, make coke crystal growth generation high-quality Jiao in the coke drum.On the delayed coking unit of routine, the alternating temperature operation makes the heat of separation column and temperature change thereupon like this, causes operation unstable when low temperature easily, and petrol-feed pump and diesel oil pump vaccuum phenomenon take place.The present invention can be remedied and be avoided by the main feed system of not alternating temperature operation.
Not having the burnt raw material of high-quality or not needing in production high-quality Jiao's the refinery, improve treatment capacity if desired and increase liquid yield, major and minor feed system then of the present invention is a raw material with vacuum residuum all, changes 0.1～0.3 partial circulating into than operation, can produce wax oil more; Under the insufficient situation of capacity to reprocess such as catalytic cracking, thermally splitting, can change the operation of 0.4～1.0 recycle ratio into, can reach the effect of many production middle distillate oil.
Accompanying drawing is a schema of the present invention.1,2 is process furnace among the figure; 3,4 is coke drum; 5 is separation column.Press production high-quality Jiao below in conjunction with accompanying drawing, voluminous wax oil, full part of oily three various objectives are described in detail in the middle of the fecund.
1. the burnt flow process of production high-quality
Main feed system: feedstock oil is entered the convection section of heating furnace 1 by pipeline 6, heat exchanger 7, enter surge tank 8 after being warming up to 300～500 ℃, again at the bottom of the tank after the radiant section that pipeline 9 enters heating furnace 1 is warming up to 490～510 ℃, a tower that enters in the coke drum 3 through pipeline 10 carries out pyrogenetic reaction, its operating condition (by 600,000 ton/years of devices): flow is 50～60 tons/hour, 490～510 ℃ of temperature, pressure 98～245KPa fills burnt 16～28 hours time. The ordinary coke that reaction generates is deposited in the coke drum, and coking oil gas enters fractionating column 5 through pipeline 11 and is fractionated into gas, gasoline, diesel oil and wax oil, and a part of heavy distillate is condensate in Fractionator Bottom to be mixed with secondary feed system feedstock oil.
Secondary feed system: raw material enters the convection section of heating furnace 2 through pipeline 12, entering fractionating column 5 bottoms after being warming up to 250～300 ℃ mixes with heavy distillate, at the bottom of tower, extract the radiant section that enters heating furnace 2 through pipeline 13 out again, a tower that enters in the coke drum 4 after 430～510 ℃ alternating temperature heating carries out pyrogenetic reaction, its flow be the 50-60 ton/hour, pressure 98～245KPa fills burnt 24～48 hours time. The high-quality coke deposits that generates is in coke drum, and coking oil gas is fractionated into gas, gasoline, diesel oil and wax oil through pipe together through 11 oil gas that enter fractionating column 5 and main feed system, and a part of heavy distillate also with after native system feedstock oil mixes recycles.
Described feedstock oil, main feed system is that proportion 0.90～0.98, carbon residue are 7～18% decompression residuum, secondary feed system comprises the high aromatic oil material such as thermal cracking residue, fluid catalytic cracking decant oil, ethylene residue and furfural extract oil or the mixed material of several oil plants wherein, its proportion is 0.85～1.2, aromatic hydrocarbons/gum level is 3～5, sulfur content is less than 0.5%, and heavy metal vanadium and nickel are all less than 10PPm; Heavy fraction oil recycle ratio is 0.2～0.7.
Fill defocused coke drum routinely the hydraulic decoking method of delay coking process carry out decoking. High-quality Jiao that the coke drum of secondary feed system generates is commodity Jiao of high-quality, the commercial needle coke that claims again through 1300 ℃ of calcinings after volatile matter is down to below 0.5%. This class Jiao has the advantages such as high density, high-crystallinity, high graphitization degree, low impurity, low thermal coefficient of expansion.
2. when producing greater than 350 ℃ wax oil more, be with production high-quality Jiao's difference:
(1) raw material of secondary feed system also is a vacuum residuum; (2) process furnace 2 does not need the alternating temperature heating, and Heating temperature is 490～510 ℃; (3) coke of coke drum 4 generations of secondary feed system is common Jiao; (4) must take out wax oil more, improve fractionator bottom temperature to greatest extent and reach 390-400 ℃; (5) the heavy distillate recycle ratio is 0.1～0.3.Can improve treatment capacity like this, produce wax oil more or increase liquid yield 4～5%() coking stock oil.
3. when producing 140～350 ℃ of intermediate oils, its raw material, method are identical with voluminous wax oil more, and difference is to go out less wax oil, make fractionator bottom temperature reduce to 340～390 ℃, recycle ratio increases to 0.4～1.0, and the intermediate oil yield can reach 40～45% like this, and diesel oil/gasoline is 2～2.5.
Advantage of the present invention:
1. when the burnt stock oil of production high-quality is not enough (as 7～150,000 tons/year), also available large-scale plant (as 600,000 tons/year) is continuous production for a long time.
2. the heavy distillate owing to main feed system circulates at production high-quality Jiao's secondary feed system, thereby enlarges high-quality Jiao's raw material.
3. recycle ratio of the present invention can be as small as the conventional delayed coking recycle ratio of 0.1(only can reduce to 0.25), thus more liquid yield increased, improve treatment capacity, and do not have the too high danger that causes coking of fractionator bottom temperature.
4. the present invention has bigger handiness.According to raw material oil condition and required purpose product, can produce needle coke and common Jiao simultaneously, also can produce wax oil or intermediate oil more.For example recycle ratio increases to 0.4～1.0, and the intermediate oil yield can reach 40～45%.
Further specifically describe characteristics of the present invention below with embodiment:
Embodiment 1
Purpose production high-quality Jiao of this example.Used stock oil, main feed system are greater than 500 ℃ of vacuum residuum, and secondary feed system is greater than 350 ℃ of thermal cracking residues, and main inlet amount/secondary inlet amount is 54.2/16.7, recycle ratio 0.53.The main character of stock oil, device operational condition and product yield, high-quality Jiao's performance sees Table 1.
Find out that by table 1 secondary feed system adopts 430～510 ℃ of alternating temperature heating, can obtain 8.6% high-quality Jiao, common Jiao of 8.6%.
Embodiment 2
This example purpose is the wax oils of producing more.Used stock oil, major and minor feed system are greater than 500 ℃ of vacuum residuum, and main charging/secondary inlet amount is 59.6/41.7, recycle ratio 0.18.The main character of stock oil, device operational condition and product situation see Table 2.Found out that by table 2 liquid yield of the present invention is 69.0%, wherein the wax oil yield is 25.4%; And the liquid yield of conventional delayed coking is 65.1%, and wherein the wax oil yield is 20.5%.
Embodiment 3
Many production of purpose middle distillate oil of this example.Used stock oil is greater than 500 ℃ of vacuum residuum, and main inlet amount/secondary inlet amount is 59.6/23.8, and recycle ratio is 0.43, and other operational conditions are with example 2.Main character, the product yield of stock oil see Table 3.
Found out that by table 3 gasoline yield of the present invention is 19.1%, diesel yield 40.2% diesel oil/gasoline is 2.105.Conventional delayed coking under the similarity condition only can obtain gasoline 17.1%, and diesel oil 31.5%, diesel oil/gasoline are 1.842.Simultaneously, gas of the present invention and common Jiao's productive rate also decreases than conventional delayed coking.
Table 1
The secondary charging of main charging
Stock oil
Proportion (20 ℃), gram per centimeter
30.9244 0.9180
Sulphur, heavy % 0.2 0.15
Carbon residue, heavy % 7.97 3.30
Operational condition
The furnace outlet temperature, ℃ 500 ℃ 430～510 ℃
The coke drum top hole pressure, KPa 147 147
Fill the burnt time, hours 24 36
Product yield, heavy %
Coking gas 7.7
Gasoline 17.3
Diesel oil 53.0
Wax oil 4.8
Common burnt 8.6
High-quality Jiao 8.6
The burnt quality of high-quality
Thermal expansivity (greying, room temperature 1.525
～500℃），10
-6/℃
True density, gram per centimeter
32.155
Sulphur, heavy % 0.31
Ash content, heavy % 0.09
Vanadium, PPm 0.2
Nickel, PPm 0.2
Table 2
The conventional delayed coking of the secondary charging of main charging
Stock oil
Proportion (20 ℃), gram per centimeter
30.9752 0.9752 0.9752
Sulphur, heavy % 0.34 0.34 0.34
Carbon residue, heavy % 16.6 16.6 16.6
Operational condition
The furnace outlet temperature, ℃ 500 500 500
The coke drum top hole pressure, KPa 147 147 147
Fill the burnt time, hours 24 24 24
Product yield, heavy %
Coking gas 8.6 9.8
Gasoline 15.2 16.4
Diesel oil 28.4 28.2
Wax oil 25.4 20.5
Common burnt 22.4 25.1
The wax oil quality
Proportion (20 ℃), gram per centimeter
30.9016 0.8933
Viscosity (100 ℃), centistoke 4.68 3.56
Condensation point, ℃ 34 27
Carbon residue, heavy % 0.46 0.21
Aniline point, ℃ 79.2 77.3
Table 3
The conventional delayed coking of the secondary charging of main charging
Stock oil
Proportion (20 ℃), gram per centimeter
30.9715 0.9715 0.9715
Sulphur, heavy % 1.72 1.72 1.72
Carbon residue, heavy % 14.37 14.37 14.37
Product yield, heavy %
Coking gas 6.7 7.9
Gasoline 19.1 17.1
Diesel oil 40.2 31.5
Wax oil 11.5 20.2
Common burnt 22.5 23.3
Claims (7)
1, a kind of slag oil delay coking process that comprises process furnace, coke drum, fractionating tower equipment improves one's methods, it is characterized in that comprising major and minor charging association system, it is oil circulation that main feed system does not have heavy fraction, and the heavy fraction oil that major and minor feed system produces all circulates described main feed system in secondary feed system;
A, stock oil are preheated to 300～350 ℃ through process furnace 1 convection zone;
The advanced surge tank 8 of the stock oil of b, preheating reenters process furnace 1 radiation section and is heated to coking temperature;
C, the stock oil that is heated are gone into coke drum 4, and coking under the coking condition of 490～510 ℃ of temperature, pressure 98～245KPa generates common Jiao and gas-phase product;
D, gas-phase product enter separation column 5 fractionation shared with secondary feed system;
Heavy fraction oil mixes with the stock oil of secondary feed system at the bottom of e, the separation column;
Described secondary feed system;
A, stock oil go into shared separation column 5 bottoms of major and minor feed system and mix with heavy fraction oil in the separation column through process furnace 2 convection zone preheatings are laggard;
B, mixture enter process furnace 2 radiation sections and are heated to coking temperature;
C, the mixture that is heated enter coke drum 4, carry out pyrogenic reaction under the coking condition of 430～510 ℃ of temperature, pressure 98～245KPa, generate high-quality burnt or common Jiao and gas-phase product;
D, gas-phase product enter with the shared separation column 5 of main feed system and carry out fractionation;
E, separation column 5 bottom heavy fraction oil mixed with stock oil in (a) step.
2, in accordance with the method for claim 1, when it is characterized in that secondary feed system coke drum 4 generates high-quality Jiao, raw materials mixed oil and turning oil heat through 430～510 ℃ of alternating temperatures at the process furnace radiation section, keep 5～8 hours at 490～510 ℃.
3, in accordance with the method for claim 1, it is common when burnt to it is characterized in that secondary feed system coke drum 4 generates, and raw materials mixed oil and turning oil heat 490～510 ℃ at process furnace 2 radiation sections.
The raw material of the major and minor feed system when 4, in accordance with the method for claim 1, it is characterized in that producing wax oil is the vacuum residuum of proportion 0.90～0.98, carbon residue 7～18% more.
5, according to claim 1 or 4 described methods, the oil circulation ratio of heavy fraction when it is characterized in that producing wax oil is 0.1～0.3 more.
The raw material of the major and minor charging when 6, in accordance with the method for claim 1, it is characterized in that many production middle distillate oil is the vacuum residuum of proportion 0.90～0.98, carbon residue 7～18%.
7, according to claim 1 or 6 described methods, the oil circulation ratio of heavy fraction when it is characterized in that many production middle distillate oil is 0.4～1.0.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 87102308 CN1011416B (en) | 1987-03-28 | 1987-03-28 | Residual Oil Coking Process with Two-way Feed System |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 87102308 CN1011416B (en) | 1987-03-28 | 1987-03-28 | Residual Oil Coking Process with Two-way Feed System |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN87102308A CN87102308A (en) | 1988-10-12 |
| CN1011416B true CN1011416B (en) | 1991-01-30 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 87102308 Expired CN1011416B (en) | 1987-03-28 | 1987-03-28 | Residual Oil Coking Process with Two-way Feed System |
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Families Citing this family (5)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN101256400B (en) * | 2008-04-09 | 2010-06-02 | 清华大学 | A control method of delayed coking furnace |
| CN103113906A (en) * | 2013-01-08 | 2013-05-22 | 何巨堂 | Coking delaying method of easy-coking oil product |
| CN105925303A (en) * | 2016-06-13 | 2016-09-07 | 安庆市泰发能源科技有限公司 | Aromatizing production line reactor airspeed regulating device |
| 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 |
| JP7311508B2 (en) * | 2017-11-14 | 2023-07-19 | 中国石油化工股▲ふん▼有限公司 | Coking system and coking method |
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- 1987-03-28 CN CN 87102308 patent/CN1011416B/en not_active Expired
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| CN87102308A (en) | 1988-10-12 |
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