CN1115375C - Improved coking process with two-channel feed system - Google Patents
Improved coking process with two-channel feed system Download PDFInfo
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- CN1115375C CN1115375C CN 98117810 CN98117810A CN1115375C CN 1115375 C CN1115375 C CN 1115375C CN 98117810 CN98117810 CN 98117810 CN 98117810 A CN98117810 A CN 98117810A CN 1115375 C CN1115375 C CN 1115375C
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Abstract
The present invention relates to an improved coking process with two-channel feed systems, which adopts a main feeding system and an auxiliary feeding system, and the two systems share one fractionating tower. When a heating furnace tube of the auxiliary feeding system cokes, a part of the main feeding system enters the sharing fractionating tower so as to maintain normal operation; when the saturation of raw material in the main feeding system is larger than 40 wt%, a part of the heavy fraction oil of the fractionating tower circulates to the main feeding system so as to be regulated. The process provided by the present invention can simultaneously produce two different levels of petroleum coke: common coke and superior quality coke.
Description
The invention belongs to a kind of improved delay coking process, more particularly, is a kind of coking process with two-channel feed system.
Delayed coking is the comparatively ideal technology of residual oil deep processing, it has characteristics such as reduced investment, flow process are simple, technology maturation, bottoms conversion height, it not only can increase substantially refinery's yield of light oil, its byproduct refinery coke still is the important source material of aluminium metallurgy, production Graphite Electrodes and other carbon products, and the residual oil more than 50% all transforms by delayed coking abroad.
For the work of bringing into play delayed coking better in order to improve the economic benefit of refinery, CN101416B discloses a kind of slag oil delay coking process with two-channel feed system, this invention is the conventional delayed coking unit of two covers of a shared separation column, the raw material of one cover delayed coking unit is the common promptly main feed system of vacuum residuum, raw material directly enters a process furnace heating after heat exchange, enter the coke drum of producing common Jiao then and carry out pyrogenic reaction, reacted coking oil gas is gone into shared separation column by the coke drum jacking.The purpose product of another set of delayed coking unit is high-quality petroleum needle coke (being called for short high-quality Jiao), it is secondary feed system, its raw material is for being selected from thermal cracking residue, fluid catalytic cracking decant oil, the mixture of one or more in ethylene bottom oil and the furfural extract oil, raw material enters shared separation column bottom after heat exchange, with the radiation section heating that enters another process furnace behind the heavy distillate mixed heat transfer in the separation column, enter production high-quality Jiao's coke drum again, the coking oil gas that reaction generates enters the separation column shared with main feed system, therefore main feed system does not have the heavy distillate circulation, and leads, the heavy distillate of secondary feed system reactant all circulates in secondary feed system.
The flow process of CN101416B is seen accompanying drawing 1, and its advantage is:
1, because the heavy distillate of major and minor feed system reactant all enters secondary feed system, therefore can enlarge the raw material sources of producing high-quality petroleum coke;
2, when secondary feed system lacks raw material, the also available common vacuum residuum of secondary feed system is done raw material, this moment is owing to have only secondary feed system that the heavy distillate circulation is arranged, and main feed system does not have the heavy distillate circulation, the recycle ratio of whole device will reduce, and help improving the liquid product yield of device.
But this invention also has following shortcoming:
1, when secondary feed system is produced high-quality petroleum coke, the coking raw material temperature of coming out from process furnace is not a constant, but between 430～510 ℃, change, the alternating temperature operation makes the temperature of coke drum and separation column and heat change thereupon like this, therefore often there is coke powder to bring separation column into and enter secondary feed system process furnace and make the easy coking of secondary charging process furnace with heavy distillate, behind secondary charging furnace coking, secondary charging can not enter separation column, quite a few heat can not be taken separation column out of by secondary charging in the separation column, the thermal equilibrium of separation column can't be kept, thereby main feed system also can't be operated;
2, in delayed coking, reaction is mainly carried out in coke drum, and the reaction of carrying out in coke drum is broadly divided into the thermal condensation reaction of the heat cracking reaction and the aromatic hydrocarbons of hydro carbons, and the condensation reaction of aromatic hydrocarbons is thermopositive reaction.When the low raw material of some aromaticity content is handled in delayed coking, the reaction of carrying out in coke drum is based on the heat cracking reaction of hydro carbons, because reaction needs to absorb a large amount of heats, therefore coke drum is difficult to remain under the temperature of requirement and operates, when the coke drum temperature is lower than the requirement temperature, pyrogenic reaction can not be carried out fully, and can produce soft Jiao this moment, not only make the decoking operation be difficult to carry out, and influence coke quality.
The objective of the invention is to provide on the basis of existing technology a kind of improved coking process with two-channel feed system, promptly behind the furnace coking of secondary feed system, the thermal equilibrium of shared separation column is unlikely to be damaged, and main feed system still can be kept normal running; When saturated part of raw material of main feed system weighed % greater than 40, decoking operation and coke quality still can not be affected.
Technology provided by the invention comprises main charging, secondary charging two-channel feed system, four coke drums and a shared separation column, when the process furnace generation tube coking of secondary feed system, the part of main charging enters the separation column bottom, heavy distillate at the bottom of the separation column enter surge tank with remaining main charging after the radiation section preheating of main feed system process furnace, in coke drum, produce common Jiao; When saturated part of raw material of main feed system weighs % greater than 40, at the bottom of the separation column part of heavy distillate enter surge tank with remaining main charging after the radiation section preheating of main feed system process furnace, in coke drum, produce common Jiao, still production high-quality of secondary feed system Jiao; Process furnace generation tube coking at secondary feed system, simultaneously under saturated part of situation of the raw material of main feed system greater than 40 heavy %, the part of main charging enters separation column, heavy distillate at the bottom of the separation column enter surge tank with remaining main charging after the radiation section preheating of main feed system process furnace, in coke drum, produce common Jiao.
Technology provided by the invention is so concrete enforcement:
Main feed system:
The process furnace convection zone that main charging enters this system heats the back enters process furnace by surge tank radiation section, be heated to 495～505 ℃ of coke drums that enter this system to produce common Jiao, coking oil gas enters the separation column separation and obtains coking gas, coker gasoline, coker gas oil, wax tailings simultaneously.
When saturated part of raw material of main feed system weighed % greater than 40, a part of coking heavy distillate of separation column bottom enters surge tank to be mixed with main charging, and the recycle ratio of main feed system can be regulated as required.
Secondary feed system:
Secondary charging enters separation column after entering the process furnace convection zone heating of this system, after the part coking heavy distillate of separation column bottom mixes, enter the radiation section of process furnace, the coke drum that enters this system after the heating is with production high-quality Jiao, and coking oil gas enters the separation column separation and obtains coking gas, coker gasoline, coker gas oil, wax tailings simultaneously.
When the process furnace generation tube coking of secondary feed system, 1/5～1/4 of main charging total amount enters separation column when temperature is 100～120 ℃, with coking oil gas heat exchange to 370～390 ℃, after entering surge tank and remaining main charging mixing, send into the radiation section of main feed system process furnace, be heated to 495～505 ℃ and enter main feed system coke drum, to produce common Jiao, coking oil gas then enters the separation column product separation.
Process furnace generation tube coking at secondary feed system, simultaneously under saturated part of situation of the raw material of main feed system greater than 40 heavy %, 1/5～1/4 of main charging total amount enters separation column when temperature is 100～120 ℃, ℃ enter surge tank with coking oil gas heat exchange to 370～390, after remaining main charging mixes, send into the process furnace radiation section of main feed system.Be heated to 495～505 ℃ and enter coke drum to produce common Jiao, coking oil gas then enters the separation column product separation.
The invention has the advantages that: after the secondary feed system heating furnace tube coking in the two-channel feed system, the part of main charging can enter shared separation column, and the thermal equilibrium of separation column can be kept normally, makes the main feed system still can quiet run; And when saturated part of the raw material of main feed system during greater than 40 heavy %, the heavy distillate of a shared separation column part capable of circulation is to main charging and regulated.Can produce the refinery coke of two kinds of different stages simultaneously with technology provided by the invention: common Jiao and high-quality Jiao.
Accompanying drawing 1 is the coking process schematic flow sheet with two-channel feed system of prior art CN101416B.
Accompanying drawing 2 is improved coking process schematic flow sheets with two-channel feed system provided by the invention.
Each numbering is described as follows in the accompanying drawing:
1,2,3,4 all represent coke drum, 5 is separation column, and 6 is surge tank, and 7,8 is process furnace, and 9,10,11,12,13,14,15,16,17,18 all represent pipeline.
The embodiment of technology provided by the present invention is described below in conjunction with accompanying drawing 2.
Main feed system:
Enter the convection zone of process furnace 8 from the main charging of pipeline 12, enter surge tank 6 after the heating, enter the radiation section of process furnace 8 through pipeline 16, be heated to 495～505 ℃ and enter coke drum 1 or 2 to produce common Jiao, coking oil gas enters separation column 5 through pipeline 17 simultaneously, separates to obtain coking gas, coker gasoline, coker gas oil, wax tailings.
When saturated part of the raw material of main feed system during greater than 40 heavy %, a part of coking heavy distillate of separation column 5 bottoms enters surge tank 6 and mixes with main charging through pipeline 9,10 successively, and the recycle ratio of main feed system can be regulated as required.
Secondary feed system:
Enter the convection zone of process furnace 7 through pipeline 14 from the secondary charging of pipeline 11, heating is after pipeline 18 enters separation column 5, after the part coking heavy distillate of separation column 5 bottoms mixes, enter the radiation section of process furnace 7 through pipeline 9, enter coke drum 3 or 4 after the heating with production high-quality Jiao, coking oil gas enters separation column 5 through pipeline 17 simultaneously, separates to obtain coking gas, coker gasoline, coker gas oil, wax tailings.
When the tube coking of secondary feed system process furnace 7,1/5～1/4 of main charging total amount enters separation column 5 through pipeline 13,14,15 successively when temperature is 100～120 ℃, with coking oil gas heat exchange to 370～390 ℃, enter surge tank 6 through pipeline 9,10 successively, after remaining main charging mixes, send into the radiation section of main charging process furnace 8.Be heated to 495～505 ℃ and enter coke drum 1 or common Jiao of 2 productions, coking oil gas then enters separation column 5 through pipeline 17.
Tube coking takes place in the process furnace 7 at secondary feed system, simultaneously under saturated part of situation of the raw material of main feed system greater than 40 heavy %, 1/5～1/4 of main charging total amount enters separation column 5 through pipeline 13,14,15 successively when temperature is 100～120 ℃, with coking oil gas heat exchange to 370～390 ℃, enter surge tank 6 through pipeline 9,10 successively, after remaining main charging mixes, send into the radiation section of main charging process furnace 8.Be heated to 495～505 ℃ and enter coke drum 1 or common Jiao of 2 productions, coking oil gas then enters separation column 5 through pipeline 17.
Claims (5)
1, a kind of coking process with two-channel feed system, comprise main charging, secondary charging two-channel feed system, four coke drums and a shared separation column, when it is characterized in that the process furnace generation tube coking when secondary feed system, the part of main charging enters the separation column bottom, heavy distillate at the bottom of the separation column enter surge tank with remaining main charging after the radiation section of main feed system process furnace is heated to 495～505 ℃, in coke drum, produce common Jiao.
2, according to the technology of claim 1, the main feeding temperature that it is characterized in that entering separation column is 100～120 ℃, and its amount is 1/5～1/4 of a main charging total amount.
3, a kind of coking process with two-channel feed system, comprise main charging, secondary charging two-channel feed system, four coke drums and a shared separation column, it is characterized in that when saturated part of raw material of main feed system weighs % greater than 40, at the bottom of the separation column part of heavy distillate enter surge tank with remaining main charging after the radiation section of main feed system process furnace is heated to 495～505 ℃, in coke drum, produce common Jiao, still production high-quality of secondary feed system Jiao.
4, a kind of coking process with two-channel feed system, comprise main charging, secondary charging two-channel feed system, four coke drums and a shared separation column, it is characterized in that process furnace generation tube coking at secondary feed system, simultaneously under saturated part of situation of the raw material of main feed system greater than 40 heavy %, the part of main charging enters separation column, heavy distillate at the bottom of the separation column enter surge tank with remaining main charging after the radiation section of main feed system process furnace is heated to 495～505 ℃, in coke drum, produce common Jiao.
5, according to the technology of claim 4, the main feeding temperature that it is characterized in that entering separation column is 100～120 ℃, and its amount is 1/5～1/4 of a main charging total amount.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 98117810 CN1115375C (en) | 1998-08-27 | 1998-08-27 | Improved coking process with two-channel feed system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 98117810 CN1115375C (en) | 1998-08-27 | 1998-08-27 | Improved coking process with two-channel feed system |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1246513A CN1246513A (en) | 2000-03-08 |
| CN1115375C true CN1115375C (en) | 2003-07-23 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 98117810 Expired - Lifetime CN1115375C (en) | 1998-08-27 | 1998-08-27 | Improved coking process with two-channel feed system |
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| Country | Link |
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| CN (1) | CN1115375C (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2015016804A1 (en) * | 2012-11-01 | 2015-02-05 | Fluor Technologies Corporation | Multiple drum coking system |
| US9852389B2 (en) | 2012-11-01 | 2017-12-26 | Fluor Technologies Corporation | Systems for improving cost effectiveness of coking systems |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115873631A (en) * | 2021-08-27 | 2023-03-31 | 中国石油化工股份有限公司 | Method and apparatus for delayed coking |
-
1998
- 1998-08-27 CN CN 98117810 patent/CN1115375C/en not_active Expired - Lifetime
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2015016804A1 (en) * | 2012-11-01 | 2015-02-05 | Fluor Technologies Corporation | Multiple drum coking system |
| US9852389B2 (en) | 2012-11-01 | 2017-12-26 | Fluor Technologies Corporation | Systems for improving cost effectiveness of coking systems |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1246513A (en) | 2000-03-08 |
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