CN1200076C - Delayed coking method for lowering coke volatile component - Google Patents
Delayed coking method for lowering coke volatile component Download PDFInfo
- Publication number
- CN1200076C CN1200076C CN 02120777 CN02120777A CN1200076C CN 1200076 C CN1200076 C CN 1200076C CN 02120777 CN02120777 CN 02120777 CN 02120777 A CN02120777 A CN 02120777A CN 1200076 C CN1200076 C CN 1200076C
- Authority
- CN
- China
- Prior art keywords
- coking
- coke
- raw material
- oil
- gas oil
- 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 - Lifetime
Links
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Coke Industry (AREA)
Abstract
The present invention relates to a delayed coking method for lowering coke volatile components. Conventional coking stock and a few coking raw materials are respectively heated to 420 to 505 DEG C and 490 to 525 DEG C and enter a coke tower, and coke generated in reaction stays in the coke tower. Coking oil gas is separated so as to obtain coking gas, coking gasoline, coking diesel oil and coking gas oil, the coking raw materials replace conventional coking stock as coking feeding for some time in a coking period, and the coking raw materials enter the coke tower for reaction after heated by a coking heater. The method reduces a volatile component of raw coke in the tower to 3 to 12 m% via increasing the temperature in the coke tower.
Description
Technical field
The invention belongs to a kind of under the situation that does not have hydrogen the thermal non-catalytic cracking technology of hydrocarbon ils, more particularly, be a kind of delayed coking method that reduces coke volatile component.
Background technology
Because investment and process cost are low, can change into products such as costly liquid product and extraordinary refinery coke to vacuum residuum inferior or sump oil, delayed coking still is the main residual oil processing technology in refinery, is subjected to people and generally payes attention to.At present, domestic coker generally faces technical problem at device maximization, long period, Optimizing operation, raising coke quality, raising liquid yield to obtain aspects such as optimum economic benefit.The coke volatile component control techniques is one of them, and coke volatile component is one of main quality index of coke.In China's oil chemical industry standard ordinary coke (the green coke green coke) quality index (SH0527-92), volatilization is divided into 12～20%, and first grade is 12%, is higher than abroad 4～10%, influence China's coke product and exports and economic benefit.At present, each refinery coker coke volatile component of China is generally 12～16%, and minority device volatile matter reaches more than 20%.The big liquid yield that influences coker of volatile matter for the coke used of steel-making electrode, also influences loss of calcination and electrode cost, the serious electrode quality that also influences.Feedstock property, operational condition and coke drum heat insulation effect have determined the coke volatile component size, at the certain raw materials such as vacuum residuum of processing, refinery coker generally adopts control furnace outlet temperature to reduce the coke volatilization, because the furnace outlet temperature is restricted by tube coking and operational cycle thereof, generally be controlled at 495 ℃～500 ℃, the leeway of adjusting is little, and therefore, coke volatile component is difficult to guarantee sometimes.
USP4,547,284 disclose a kind of coke production method, and particularly with through pretreated raw material production needle coke method, this method is heat-treated to reduce the volatile matter of coke with cracked gas not the coke in off-line (off-stream) coke drum.This method is after an operational cycle finishes to change tower off-line coke drum to be heat-treated.This method needs one to overlap not cracked gas heating, cooling, the recycle system in addition, and during actually operating, this recycle system and coking operation itself is difficult to lucky distribution.
USP5,645,712 disclose a kind of delayed coking method that improves liquid product yield, be in the operation cycle ratio that reduces coking system, hydrocarbon diluent with the non-coking after a kind of heating improves the coke drum service temperature, and liquid product yield is increased, and coking yield descends.This thinner can add in the logistics of furnace outlet, also can directly add in the coke drum, and thinner separates heating with coking raw material, and the thinner cut is light to small part proportion gas oil, and this method is separated heating with thinner and coking raw material and operated simultaneously.This method also needs a cover thinner heating system, has increased facility investment and process cost.
Summary of the invention
The objective of the invention is defective, propose a kind of delayed coking method that reduces coke volatile component at prior art.
Method provided by the invention comprises: conventional coking raw material, less pyrogenic raw material are entered coke drum after being heated to 420 ℃～505 ℃, 490 ℃～525 ℃ respectively, the coke that reaction generates is stayed in the coke drum, separate coking oil gas and obtain cooking gas, coker gasoline, coker gas oil, coker gas oil, less pyrogenic raw material replaces conventional coking raw material as the coking charging in for some time of a coking cycle, is heated to 490 ℃～525 ℃ through coking heater and enters the coke drum reaction.
Temperature makes the green coke volatile matter in the tower be reduced to 3～12m% to this method in the coke drum by improving.
Description of drawings
Accompanying drawing is the delayed coking method synoptic diagram of reduction coke volatile component provided by the invention.
Embodiment
Method provided by the invention is: conventional coking raw material, less pyrogenic raw material are entered coke drum after being heated to 420 ℃～505 ℃, 490 ℃～525 ℃ respectively, the coke that reaction generates is stayed in the coke drum, separate coking oil gas and obtain cooking gas, coker gasoline, coker gas oil, coker gas oil, less pyrogenic raw material replaces conventional coking raw material as the coking charging in for some time of a coking cycle, is heated to 490 ℃～525 ℃ through coking heater and enters the coke drum reaction.
Described conventional coking raw material is selected from vacuum residuum, long residuum, visbreaking residue, fluid catalytic cracking decant oil, straight run gas oil or its mixture; Less pyrogenic raw material is coking distillate, straight run gas oil or its mixture, and wherein coking distillate is coker gas oil and/or coker gas oil, and straight run gas oil is normal pressure straight run gas oil and/or decompression straight run gas oil.
The ratio of less pyrogenic raw material and conventional coking raw material is 40m%～150m%, preferably 100m%.100m% is meant that conventional coking raw material in the operation is fully by less pyrogenic raw material substitution, the flow of this raw material is identical with the flow of conventional coking raw material, be meant that less than 100m% conventional coking raw material part in the operation is by less pyrogenic raw material substitution, be meant conventional coking raw material in the operation fully by less pyrogenic raw material substitution greater than 100m%, the flow of this raw material is greater than the flow of conventional coking raw material.Handoff procedure can be to switch in a step to finish, and also program is switched gradually in time.
The position that less pyrogenic raw material switches into coking system is coking raw material oil surge tank inlet or source line, for switching, can also be enter the mouth any position between the outlet of raw material surge tank of coking heater convection zone inlet, radiation section inlet or process furnace convection zone less than 100% raw material.
In coking, some coke drums fill burnt to suitable need height after, change the tower operation, conventional coking raw material substitutes less pyrogenic raw material and advances another coke drum, the origin operation coke drum carries out cold Jiao and decoking operation, the decoking mode is a hydraulic decoking, and the pressure of hydraulic decoking is 10.0MPa～30.0MPa.To change tower be a coking operation cycle to each coke drum to being full of coke from feed switched, and a coking cycle is 12～48 hours.A coking cycle divides two time periods, and previous time period is advanced conventional coking raw material, and by recycle ratio 0～0.4 operation, one time period of back is advanced less pyrogenic raw material, by recycle ratio 0～1.0 operation.
For some time of a coking cycle refers to 5～50% of a coking cycle, is for some time before one-period finishes.Replace the independent reacting by heating of conventional coking raw material in above-mentioned for some time with less pyrogenic raw material, utilize the conventional relatively coking raw material of less pyrogenic raw material to be difficult for the characteristics of coking, improve its temperature of reaction, less pyrogenic raw material provides high potential temperature heat for coke drum, the further thermal treatment of sedimentary coke in the STRENGTH ON COKE tower descends the volatile matter of coke.With the suitable condition of conventional coking coke volatile component under, the furnace outlet temperature was reduced to 440 ℃～485 ℃ when said process allowed the conventional coking raw material of processing, had delayed coking heater coking tendency.
In order to prevent the coking of high-temperature oil gas pipeline, on coke drum top exit gas pipeline, annotate chill oil, chill oil is coker gas oil, coker gas oil or its mixture.The oil gas of coke cat head temperature after the chill oil cooling reaches 410 ℃～440 ℃, has delayed coke drum outlet gas pipeline coking tendency.
Said process also is applicable to fluid catalytic cracking decant oil produces needle coke as conventional coking raw material.
Method provided by the invention is not only applicable to a stove two tower flow processs, is applicable to two stoves, four towers or three stoves, six tower flow processs yet, and the coke that coking is produced is common Jiao, makes steel with high grade coke or needle coke.
Below in conjunction with accompanying drawing method provided by the present invention is further detailed, but does not therefore limit the present invention.
Accompanying drawing is the delayed coking method synoptic diagram of reduction coke volatile component provided by the invention, and this figure is a stove two tower flow processs, is an operational cycle by 24 hours.
In preceding 20 hours an of operational cycle, device advances conventional coking raw material, this raw material enters surge tank 2 through pipeline 1 earlier, enter the bottom and the heat exchange of coking oil gas part of coking fractional distillation column 11 then through pipeline 3, with turning oil after pipeline 4 enters coking heater 5 heating, enter coke drum 7 or 9 respectively through pipeline 6 or 8, pyrogenic reaction takes place in conventional coking raw material and turning oil in coke drum, the coke that generates is stayed in the coke drum, coking oil gas enters coking fractional distillation column 11 through pipeline 10, isolated cooking gas, coker gasoline, coker gas oil, coker gas oil is respectively through pipeline 12,13,21,22 derive, and coking recycle oil returns coking system.This moment, process furnace radiation section temperature out was 420 ℃～505 ℃, was 0.2 operation by recycle ratio.After the operational cycle in 4 hours, stop conventional coking raw material motion device, the straight run gas oil that will reduce pressure is introduced surge tank 2 through pipeline 14, conventional coking raw material is switched to the operation of decompression straight run gas oil, decompression straight run gas oil coking raw material flow process routinely is heated to 490 ℃～525 ℃ and enters coke drum, by recycle ratio 0.15 operation, separate coking oil gas.
The present invention utilizes the conventional relatively coking raw material of less pyrogenic raw material to be difficult for the characteristics of coking, improve its temperature of reaction, less pyrogenic raw material provides high potential temperature heat for coke drum, and the further thermal treatment of sedimentary coke makes the volatile matter of coke be reduced to 3～12m% in the STRENGTH ON COKE tower.
The following examples will give further instruction to present method, but therefore not limit present method.Embodiment, the used conventional coking raw material of Comparative Examples are vacuum residuum, and its character is as shown in table 1.
Comparative Examples
In the accompanying drawings, vacuum residuum enters surge tank 2 through pipeline 1 earlier, enter the bottom and the heat exchange of coking oil gas part of coking fractional distillation column 11 then through pipeline 3, with turning oil (recycle ratio is 04) respectively after pipeline 4 enters coking heater 5 and is heated to 495 ℃, pyrogenic reaction in entering coke drum 7, pipeline 6 takes place, the coke that generates is stayed in the coke drum, the coke material level rises to certain height in coke drum, change the tower operation and enter the next operational cycle, conventional coking raw material is switched to coke drum 9, and the coke drum 7 that is full of coke carries out cold Jiao and decoking operation.Coking oil gas enters coking fractional distillation column 11 through pipeline 10, and isolated cooking gas, coker gasoline, coker gas oil, coker gas oil are derived through pipeline 12,13,21,22 respectively, and coking recycle oil returns coking system.
Coke product character sees Table 2, and as seen, the volatilization of coke is divided into 13.5m% from table 2.
Embodiment
In the accompanying drawings, for an operational cycle 24 hours coking, in preceding 20 hours of operational cycle, device advances vacuum residuum, and process furnace radiation section temperature out is 495 ℃, after the operational cycle in 4 hours, stop conventional coking raw material motion device, change into decompression straight run gas oil into, the ratio of decompression straight run gas oil and vacuum residuum is 100m%, decompression straight run gas oil coking raw material flow process routinely is heated to 505 ℃ and enters coke drum, separates coking oil gas.
Coke product character sees Table 2, and as seen, the volatilization of coke is divided into 5.2m% from table 2, reduces by 8.3 percentage points than the coking yield in the Comparative Examples.
Table 1
| Material name | Vacuum residuum | Decompression straight run gas oil |
| Proportion (15 ℃/4 ℃), g/cm 3 | 0.9732 | 0.8932 |
| Carbon residue, m% | 13.4 | 0.12 |
| Ash content, m% | 0.05 | 0.01 |
| Sulphur content, m% | 1.42 | 1.1 |
| Kinematic viscosity (100 ℃), mm 2/s | 835.5 | 6.4 |
Table 2
| Comparative Examples | Embodiment | |
| Coke | ||
| Volatile matter, m% | 13.5 | 5.2 |
| Ash content, m% | 0.18 | 0.18 |
| Sulphur content, m% | 1.9 | 1.8 |
Claims (9)
1, a kind of delayed coking method that reduces coke volatile component, it is characterized in that conventional coking raw material, less pyrogenic raw material is heated to 420 ℃～505 ℃ respectively, enter coke drum after 490 ℃～525 ℃, the coke that reaction generates is stayed in the coke drum, separate coking oil gas and obtain cooking gas, coker gasoline, coker gas oil, coker gas oil, less pyrogenic raw material before coking cycle finishes, account for this coking cycle 5～50% during this period of time in the conventional coking raw material of replacement as the coking charging, recycle ratio during less pyrogenic raw material coking is 0～1.0, enters the coke drum reaction after the coking heater heating.
2,, it is characterized in that described conventional coking raw material is selected from vacuum residuum, long residuum, visbreaking residue, fluid catalytic cracking decant oil, straight run gas oil or its mixture according to the method for claim 1.
3, according to the method for claim 1, it is characterized in that described less pyrogenic raw material is coking distillate, straight run gas oil or its mixture, wherein coking distillate is coker gas oil and/or coker gas oil, and straight run gas oil is normal pressure straight run gas oil and/or decompression straight run gas oil.
4, according to claim 1,2 or 3 method, the ratio that it is characterized in that described less pyrogenic raw material and conventional coking raw material is 40m%～150m%.
5, according to the method for claim 1, it is characterized in that a described coking operation cycle be meant each coke drum from feed switched to being full of the time that coke changes tower, a coking cycle is 12～48 hours.
6,, it is characterized in that the coke that coking is produced is common Jiao, makes steel with high grade coke or needle coke according to the method for claim 1.
7, according to the method for claim 1, the recycle ratio when it is characterized in that conventional coking raw material coking is 0～0.4.
8, according to the method for claim 1, it is characterized in that the decoking mode is a hydraulic decoking, the pressure of hydraulic decoking is 10.0MPa～30.0MPa.
9, according to the method for claim 1, it is characterized in that on coke drum top exit gas pipeline, annotating chill oil, chill oil is coker gas oil, coker gas oil or its mixture.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 02120777 CN1200076C (en) | 2002-05-31 | 2002-05-31 | Delayed coking method for lowering coke volatile component |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 02120777 CN1200076C (en) | 2002-05-31 | 2002-05-31 | Delayed coking method for lowering coke volatile component |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1461794A CN1461794A (en) | 2003-12-17 |
| CN1200076C true CN1200076C (en) | 2005-05-04 |
Family
ID=29742561
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 02120777 Expired - Lifetime CN1200076C (en) | 2002-05-31 | 2002-05-31 | Delayed coking method for lowering coke volatile component |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1200076C (en) |
-
2002
- 2002-05-31 CN CN 02120777 patent/CN1200076C/en not_active Expired - Lifetime
Also Published As
| Publication number | Publication date |
|---|---|
| CN1461794A (en) | 2003-12-17 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US4404092A (en) | Delayed coking process | |
| AU708406B2 (en) | Method for increasing yield of liquid products in a delayed coking process | |
| CN101597518A (en) | A kind of improved delay coking process | |
| CN1261526C (en) | High acid value hydrocarbon oil delayed coking method | |
| JPH06104834B2 (en) | Girade caulking method | |
| CN1200076C (en) | Delayed coking method for lowering coke volatile component | |
| CN109777458B (en) | Preparation method of high-quality needle coke | |
| CN1206318C (en) | Delayed coking method capable of reducing coked gas oil | |
| CN102051214A (en) | Coked wax oil thermal cracking combined process | |
| CN102268287B (en) | Delayed coking method of advanced deacidification of high acid raw oil | |
| CN1323131C (en) | Delayed coking method for increasing coke strength | |
| CN1276963C (en) | High-yield chemical light oil delayed coking method | |
| CN1465658A (en) | Method for simutaneously raising treatment quantity and diesel recovery ratio of delay coking apparatus | |
| RU2058366C1 (en) | Method for production of petroleum coke | |
| CN217651150U (en) | Oil gas recovery processing system for delayed coking | |
| RU2256687C1 (en) | Method of retarding of petroleum residue coking | |
| CN1238470C (en) | Improved delayed coking process for raising yield of gasoline and diesel oil | |
| CN1740274A (en) | Direct delayed coking process of heavy raw oil | |
| CN106675613B (en) | A kind of processing method of phenol tar | |
| CN106924984B (en) | Method for controlling liquid level and reaction severity of tower bottom of fractionating tower | |
| CN1286947C (en) | Dalayed coking method of ungraded materials | |
| CN1396236A (en) | Delay coking process able to flexibly regulate recirculating ratio | |
| US11920099B2 (en) | Extruder systems and processes for production of petroleum coke | |
| RU2786846C1 (en) | Method for producing petroleum needle coke | |
| CN111321003A (en) | Process for producing needle coke |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CX01 | Expiry of patent term | ||
| CX01 | Expiry of patent term |
Granted publication date: 20050504 |