CN1206318C - Delayed coking method capable of reducing coked gas oil - Google Patents
Delayed coking method capable of reducing coked gas oil Download PDFInfo
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- CN1206318C CN1206318C CN 02116913 CN02116913A CN1206318C CN 1206318 C CN1206318 C CN 1206318C CN 02116913 CN02116913 CN 02116913 CN 02116913 A CN02116913 A CN 02116913A CN 1206318 C CN1206318 C CN 1206318C
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Abstract
The present invention relates to a delayed coking method which can reduce coked gas oil. Conventional coking stock and coking gas oil 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. The coking gas oil is separated so as to obtain coking gas, coking gasoline, coking diesel oil and coking gas oil, wherein the coking gas oil replaces conventional coking stock as coking feeding in a coking cycle for some time, is heated by a coking heating furnace and enters the coke tower for reaction. The method singly carries out high temperature drastic cracking to the coking gas oil, so the yield of the coking gas oil is reduced to 0 to 20 m%, the yield of the coking diesel oil is increased by 2 to 15%, the volatile component of the coke is reduced to 4 to 12 m%, and the method delays the coking tendency of the coking heating furnace.
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 the coker gas oil yield.
Background technology
Because the investment and the process cost of delayed coking are low, can change into products such as costly liquid and 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, a large amount of research and industrial application work have been done at liquid yield that improves the delay coking process process and reduction ordinary coke yield aspects both at home and abroad, groundwork is recently to improve liquid product yield by the circulation that reduces coker operations, recycle ratio reduces to 0.05～0.15 usually, even utilize single-pass operation to realize the maximization of liquid product yield, in order to prevent because of reducing the situation that recycle ratio causes coke quality to descend and furnace tubing coking tendency strengthens, coking system is introduced the hydrocarbon thinner of non-coking, the subject matter of above-mentioned work is that the part that liquid product yield improves mainly is the increase of heavy gas oil fraction, because impurity such as this heavy gas oil sulphur nitrogen are alkali nitrogen content height particularly, coke powder, bituminous matter and carbon residue are big, cut is quite heavy, to such an extent as to bring very big difficulty to make the post-treatment process become uneconomical for following process process such as hydrofining or catalytic cracking etc., place to go that poor like this heavy gas oil is most economical or delayed coking, in fact, the coker gas oil of tradition delay coking process is owing to derive from vacuum residuum, particularly the alkali nitrogen content is very high for impurity such as its sulphur nitrogen, it is the imperfect raw material of catalytic cracking, and its catalytic cracking diesel oil cetane value only 28～32, combustionproperty is poor.Therefore, coker gas oil is digested in coking, the coker gas oil that as far as possible has more high hexadecane value (reaching 48～55) is a technological process meaningful and likely.Secular delayed coking process practice is known, the operation cycle ratio that improves coking can reduce the coker gas oil yield, but, because the heat and the temperature limitation that provided by coking heater, with easier pyrogenic conventional coking raw material such as vacuum residuum coker gas oil by the process furnace radiating furnace tube, there are not enough heats and temperature and the residence time to carry out drastic cracking, coke drum subsequently can't make the further cracking of coker gas oil because temperature of reaction descends, so systemic circulation is difficult to drop to lower level than the coker gas oil yield of operating.
CN1246512A discloses a kind of thermocracking process of heavy oil, this patent adopts establishes a process furnace and a reactor in addition with coker gas oil heating carrying out thermally splitting, reaction oil gas advances former coking fractional distillation column fractionation again, and uncracked gas oil wherein returns coking system again.This method need be established a process furnace and a reactor in addition, because this reactor is not a coke drum, the thermally splitting temperature of employing is lower, has the unconverted coker gas oil of part to return coking system, corresponding reduction unit capacity.
CN1176287A discloses a kind of delay coking process of high-yield diesel oil, and this patent adopts to be returned coking heater with pump again with coker gas oil part (350 ℃～420 ℃) and heat to advance coke drum again and carry out pyrogenic reaction with coking raw material and turning oil.This technology for above-mentioned reasons, the further cracked degree of this part coker gas oil is limited and go out the heavy coker gas oil of a part.
Summary of the invention
The objective of the invention is defective, propose a kind ofly separately coker gas oil to be carried out the delayed coking method that reacting by heating reduces coker gas oil separately at prior art.
Method provided by the invention comprises: enter coke drum after conventional coking raw material, coker gas oil are 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 (hereinafter to be referred as CGO), wherein CGO 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.
The present invention utilizes the CGO raw material to be difficult for the characteristics of coking, improves its temperature of reaction, makes its independent drastic cracking, the CGO yield is reduced to 0～20m%, the coker gas oil yield improves 2～15 percentage points, and coke volatile component is reduced to 4m%～12m%, has also delayed coking heater coking tendency.
Description of drawings
Fig. 1 is the delayed coking method synoptic diagram of minimizing coker gas oil provided by the invention, and this figure is a stove two tower flow processs.
Fig. 2 is the delayed coking method synoptic diagram of minimizing coker gas oil provided by the invention, and this figure is two stove four-column process flows.
Embodiment
Method provided by the invention is: enter coke drum after conventional coking raw material, coker gas oil are 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, wherein coker gas oil 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.
In coking, some coke drums fill burnt to suitable need height after, change tower and operate, change conventional coking raw material and advance another coke drum, the origin operation coke drum carries out cold Jiao and decoking operation, and 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.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 CGO, utilize the conventional relatively coking raw material of CGO to be difficult for the characteristics of coking, improve its temperature of reaction, increase its depth of conversion, reach the purpose that reduces CGO.Simultaneously, CGO provides high potential temperature heat for coke drum, and the further thermal treatment of sedimentary Jiao 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, CGO or its mixture.The oil gas of coke cat head temperature after the chill oil cooling reaches 410 ℃～440 ℃, has delayed coking heater coking tendency.
The coke that coking is produced is common Jiao, makes steel with high grade coke or needle coke.Said process also is applicable to fluid catalytic cracking decant oil produces needle coke as conventional coking raw material.
With three kinds of embodiments the present invention is further described below, but the present invention is not limited to this two kinds of embodiments.
Embodiment one:
Present embodiment is a stove two tower flow processs.Conventional coking raw material advances coking heater through the laggard coking fractional distillation column of heat exchange and coking recycle oil by recycle ratio 0.2 (being the mass ratio of turning oil and conventional coking raw material) and is heated to 490 ℃ and advances coke drum, because the pyrogenic reaction aggregate performance is heat absorption, conventional coking raw material and coking recycle oil rely in coke drum and absorb self heat generation pyrogenic reaction, the coke that generates is stayed in the coke drum, the coking oil gas that generates advances coking fractional distillation column and isolates cooking gas, coker gasoline, coker gas oil, CGO, it is low 30 ℃～80 ℃ than its temperature in to reach overhead oil temperature degree in this coke drum, the coke drum outer wall is established thermal insulation layer and is avoided heat radiation, the operation coke drum fill burnt to suitable need height after, change the tower operation, change conventional coking raw material and advance second coke drum, the origin operation coke drum carries out cold Jiao and decoking operation, 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 24 hours.At this after date 4 hours in week, replace conventional coking raw material as the coking charging CGO that generates, advance the coke drum reaction through being heated to 520 ℃, the coking oil gas that generates advances coking fractional distillation column and isolates cooking gas, coker gasoline, coker gas oil and a small amount of CGO, and turning oil and CGO are by 0.15 time reactive system of recycle ratio.Like this in one-period 24 hours, in the processing conventional coking raw material while suitable substantially, improved the coker gas oil yield with conventional coking, reduce even eliminated CGO.Lower because of processing conventional coking raw material outlet of still temperature in addition, slowed down the tube coking tendency.One-period finishes, and CGO is switched to conventional coking raw material again, repeats said process.Switch CGO in for some time as the coking charging, need to annotate chill oil on the coke cat head gas pipeline, control oil gas temperature is less than 425 ℃, and chill oil is 90 ℃ CGO.Cao Zuo coker in a manner described, the coke volatile component of coke drum descends, and hardness strengthens, and needs the hydraulic pressure of 18MPa that coke is removed.
Embodiment two:
Present embodiment is two stove four-column process flows.This flow process can have following scheme:
Scheme 1, one cover one stove two towers advance conventional coking raw material, and an another set of stove two towers advance CGO;
Scheme 3, one cover one stove two towers advance conventional coking raw material, and an another set of stove two towers advance conventional coking raw material for the previous period a coking cycle, advance CGO in back for some time.
Be that example is narrated only below with scheme 1.
Conventional coking raw material comes along a coking heater with a certain amount of turning oil and is heated to 420 ℃～505 ℃ of coking temperatures and advances a corresponding coke drum after going separation column bottom and the direct heat exchange of pyrogenic reaction oil gas part behind raw material surge tank and interchanger and the process furnace convection zone, pyrogenic reaction takes place in coke drum, the coke of producing is stayed in the coke drum, coking oil gas goes separation column to carry out fractionation with a certain amount of turning oil by the coke overhead line, this turning oil returns coking system, cooking gas, coker gasoline, coker gas oil, CGO is told by separation column, CGO gets to another process furnace convection zone by pump and radiation section is heated to 490 ℃～525 ℃, be added to another coke drum and carry out the drastic cracking reaction, the oil gas of generation also goes same separation column to fractionate out cooking gas, coker gasoline, coker gas oil.The a small amount of coke that generates is stayed in the coke drum, because CGO green coke amount is few, the furnace tubing coking tendency of heating CGO reduces this furnace operation cycle stretch-out.Like this for the coking system of two stoves, four towers, when keeping a certain amount of conventional coking raw material continuously feeding, can not go out CGO, promptly eliminated CGO, had more coker gas oil.
Embodiment three:
Present embodiment is three stoves, six tower flow processs.Similar with embodiment two, present embodiment can have the scheme of various combinations.One of them scheme is only described below.
Adopting two stoves, four towers wherein is 0～0.4 to advance conventional coking raw material and operate by normal flow by recycle ratio, an another set of stove two towers are 0～1.0 operation by CGO feed cycle ratio, to be conventional coking raw material after going separation column bottom and the direct heat exchange of pyrogenic reaction oil gas part behind raw material surge tank and interchanger and the process furnace convection zone with a certain amount of turning oil come along advances two corresponding coke drums respectively after two coking heaters are heated to 420 ℃～505 ℃ of coking temperatures, pyrogenic reaction takes place in coke drum, the coke of producing is stayed in the coke drum, coking oil gas goes separation column to carry out fractionation with a certain amount of turning oil by the coke overhead line, this turning oil returns coking system, cooking gas, coker gasoline, coker gas oil, CGO is told by separation column, wherein CGO gets to another process furnace convection current by pump and radiation section is heated to 490 ℃～525 ℃, be added to another coke drum and carry out the drastic cracking reaction, the oil gas of generation also goes same separation column to fractionate out cooking gas, coker gasoline, coker gas oil.The a small amount of coke that generates is stayed in the coke drum, because CGO green coke amount is few, the furnace tubing coking tendency of heating CGO reduces this furnace operation cycle stretch-out.Like this for the coking system of three stoves, six towers, when keeping a certain amount of conventional coking raw material continuously feeding, can not go out CGO, promptly eliminated CGO, had more coker gas oil.
Below in conjunction with accompanying drawing method provided by the present invention is further detailed.
Fig. 1 is the delayed coking method synoptic diagram of minimizing CGO 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, CGO 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 CGO that this device one-period for some time is produced introduces surge tank 2 through pipeline 14, conventional coking raw material is switched to the CGO operation, CGO 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.
Drastic cracking finally makes CGO install basic cracking at this and falls CGO because its temperature further improves, and has improved the coker gas oil yield simultaneously, has also reduced coke volatile component.Owing to adopted low recycle ratio in preceding 20 hours, strengthen inlet amount, although do not advance conventional coking raw material in back 4 hours, the amount of finish of one-period is suitable with conventional coking.Specifically, the yield of CGO can be reduced to 0～20m%, and the coker gas oil yield improves 2～15 percentage points, and coke volatile component is reduced to 4m%～12m%.
Fig. 2 is the delayed coking method synoptic diagram of minimizing CGO provided by the invention, and this figure is two stove four-column process flows.
Conventional coking 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 and is heated to 420 ℃～505 ℃, 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, CGO is respectively through pipeline 12,13,21,22 derive, and coking recycle oil returns coking system.
CGO is after pipeline 14 enters coking heater 15 and is heated to 490 ℃～525 ℃, enter coke drum 17 or 19 respectively through pipeline 16 or 18, pyrogenic reaction takes place in CGO in coke drum, the coke that generates is stayed in the coke drum, coking oil gas enters coking fractional distillation column 11 through pipeline 20, isolated cooking gas, coker gasoline, coker gas oil, CGO derive through pipeline 12,13,21,22 respectively, and coking recycle oil returns coking system.
In addition, in above-mentioned two stove four-column process flows, also can be therein a cover one stove two towers (process furnace 5, coke drum 7,9) advance conventional coking raw material, by the operation of recycle ratio 0.2 normal way, an another set of stove two towers (process furnace 15, coke drum 17,19) advance conventional coking raw material preceding 18 hours of one-period 24 hours, by the operation of recycle ratio 0.2 normal way, back 6 hours of this cycle, the CGO that device is produced is after pipeline 23 is squeezed into process furnace 15 and is heated to 490 ℃～525 ℃, enter coke drum 17 or 19, CGO is drastic cracking in coke drum, the cooking gas of generation, coker gasoline, coker gas oil and a small amount of CGO isolate through separation column 11.Under like this can the assurance device amount of finish constant substantially condition, reduce even eliminate CGO, improved the coker gas oil yield, reduced the volatile matter of coke in the coke drum 17,19.During actually operating, raw material and CGO depend on device amount of finish and the requirement of CGO yield switching time.
The invention has the advantages that: the yield of CGO can be reduced to 0～20m%, and the coker gas oil yield improves 2～15 percentage points, and coke volatile component is reduced to 4m%～12m%.
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 1
In Fig. 1, 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 0.4) 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, CGO derive through pipeline 12,13,21,22 respectively, and coking recycle oil returns coking system.
Operational condition, product distribute and portioned product character sees Table 2, and as seen, the yield of coker gasoline, coker gas oil, CGO is respectively 13.7m%, 33.2m%, 20.4m% from table 2, and the volatilization of coke is divided into 14m%.
Embodiment 1
In Fig. 1, 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 the CGO that one-period into produced in preceding 20 hours into, CGO coking raw material flow process routinely is heated to 505 ℃ and enters coke drum, separates coking oil gas.
Operational condition, product distribute and portioned product character sees Table 2, from table 2 as seen, the yield of coker gasoline, coker gas oil is respectively 16.9m%, 44.3m%, exceed 3.2,11.1 percentage points than the coker gasoline in the Comparative Examples 1, coker gas oil yield respectively, the yield of CGO is 3.4m%, reduce by 17 percentage points than the CGO yield in the Comparative Examples 1, though the CGO cracking generates a spot of coke, the coke total recovery descends to some extent; The volatilization of coke is divided into 8m%, reduces by 6 percentage points than the coking yield in the Comparative Examples 1.
Comparative Examples 2
In Fig. 2, 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 0.4) respectively through pipeline 4,14 enter coking heater 5,15 be heated to 495 ℃ after, respectively through pipeline 6,16 enter coke drum 7 respectively, pyrogenic reaction takes place in 17, 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 respectively, 19, be full of the coke drum 7 of coke, 17 carry out cold Jiao and decoking operation.Coking oil gas enters coking fractional distillation column 11 through pipeline 10,20 respectively, and isolated cooking gas, coker gasoline, coker gas oil, CGO derive through pipeline 12,13,21,22 respectively, and coking recycle oil returns coking system.
Operational condition, product distribute and portioned product character sees Table 3, and as seen, the yield of coker gasoline, coker gas oil, CGO is respectively 13.7m%, 33.2m%, 20.4m% from table 3.
In Fig. 2, after vacuum residuum advances process furnace 5 and is heated to 495 ℃, enter pyrogenic reactions take place in coke drum 7 or 9; And after CGO advances process furnace 15 and be heated to 505 ℃, enter pyrogenic reactions take place in coke drum 17 or 19.
Operational condition, product distribute and portioned product character sees Table 3, from table 3 as seen, the yield of coker gasoline, coker gas oil is respectively 16.9m%, 43.8m%, exceed 3.2,10.6 percentage points than the coker gasoline in the Comparative Examples 1, coker gas oil yield respectively, the yield of CGO is 3.4m%, reduce by 17 percentage points than the CGO yield in the Comparative Examples 1, though the CGO cracking generates a spot of coke, the coke total recovery descends to some extent.
Table 1
| Material name | Vacuum residuum |
| Proportion (15 ℃/4 ℃), g/cm 3 | 0.9862 |
| Carbon residue, m% | 13.7 |
| Ash content, m% | 0.06 |
| Sulphur content, m% | 1.48 |
| Kinematic viscosity (100 ℃), mm 2/s | 856.3 |
Table 2
| Comparative Examples 1 | Embodiment 1 | ||
| Operational condition | |||
| The one-period time, h | 24 | 20 (preceding time periods) | 4 (back time periods) |
| The furnace outlet temperature, ℃ | 495 | 495 | 505 |
| Recycle ratio | 0.40 | 0.10 | 0.35 |
| The coke tower top pressure, MPa | 1.7 | 1.7 | 1.7 |
| The coke tower top temperature, ℃ | 425 | 422 | 440 |
| Product distributes, m% | |||
| Cooking gas | 7.9 | 10.8 | |
| Coker gasoline | 13.7 | 16.9 | |
| Coker gas oil | 33.2 | 44.3 | |
| CGO | 20.4 | 3.4 | |
| Coke | 24.8 | 24.6 | |
| CGO character | |||
| Proportion (15 ℃/4 ℃), g/cm 3 | 0.9203 | 0.9123 | |
| 95% boiling range, ℃ | 471 | 458 | |
| Coke volatile component, m% | 14 | 8 | |
Table 3
| Comparative Examples 2 | | ||
| Operational condition | |||
| The major equipment | |||
| Process furnace | |||
| 5，15 | 5 | 15 | |
| | 7，9/17，19 | 7/9 | 17/19 |
| The furnace outlet temperature, ℃ | 495 | 495 | 505 |
| Recycle ratio | 0.40 | 0.10 | - |
| The coke tower top pressure, MPa | 1.7 | 1.7 | 1.7 |
| The coke tower top temperature, ℃ | 425 | 422 | 450 |
| Product distributes, m% | |||
| Cooking gas | 7.9 | 10.9 | |
| Coker gasoline | 13.7 | 16.9 | |
| Coker gas oil | 33.2 | 43.8 | |
| CGO | 20.4 | 3.4 | |
| Coke | 24.8 | 25.0 | |
| CGO character | |||
| Proportion (15 ℃/4 ℃), g/cm 3 | 0.9203 | 0.9123 | |
| 95% boiling range, ℃ | 471 | 458 | |
Claims (7)
1, a kind of delayed coking method that reduces coker gas oil, it is characterized in that conventional coking raw material, coker gas oil 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, wherein coker gas oil 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 the coker gas oil 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 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.
4,, 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.
5, 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.
6, 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.
7, 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.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 02116913 CN1206318C (en) | 2002-04-26 | 2002-04-26 | Delayed coking method capable of reducing coked gas oil |
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| CN 02116913 CN1206318C (en) | 2002-04-26 | 2002-04-26 | Delayed coking method capable of reducing coked gas oil |
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| CN1206318C true CN1206318C (en) | 2005-06-15 |
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| CN102041013B (en) * | 2009-10-16 | 2013-07-24 | 中国石油化工股份有限公司 | Method for producing needle coke raw material by using delayed coking process |
| CN103102986B (en) * | 2011-11-10 | 2015-05-13 | 中国石油化工股份有限公司 | Combined process of hydrotreatment and delayed coking for residual oil |
| CN104046383B (en) * | 2013-03-17 | 2016-01-13 | 中国石油化工股份有限公司 | A kind of processing method of delayed coking and device |
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