CN104046384A - Delayed coking process and device - Google Patents
Delayed coking process and device Download PDFInfo
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- CN104046384A CN104046384A CN201310084695.1A CN201310084695A CN104046384A CN 104046384 A CN104046384 A CN 104046384A CN 201310084695 A CN201310084695 A CN 201310084695A CN 104046384 A CN104046384 A CN 104046384A
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Abstract
The invention relates to a delayed coking process and a device. The process comprises the following steps: flash evaporation is carried out on high-temperature oil gas coming from a coke tower top; a liquid phase flow obtained after flash evaporation is divided through gravity or rotational flow sedimentation into a flow containing much coke powder and a flow containing less coke powder; a gas phase flow obtained after flash evaporation enters a fractionating tower to separate coker rich gas, coker gasoline, coker diesel and coker gas oil; the flow containing less coke powder or an oil mixture composed of the flow containing less coke powder and coking distillate oil is used as a backflow of flash evaporation; and after heated by a convection section and a radiation section of a heating furnace, raw oil or an oil mixture of the raw oil and oil at the bottom of the fractionating tower is mixed with the flow containing much coke powder, and the mixture enters a coke tower to react. By the method and the device provided by the invention, quality of a coking product can be raised; influence of coke powder on downstream processes is reduced; yield of a liquid product can be raised; and operational cycle of the device can be prolonged.
Description
Technical field
The present invention relates to a kind of coking delay process and device that improves liquid product yield.
Background technology
Along with the trend aggravation of world's crude resources heaviness, in poor quality, and the minimizing of heavy fuel oil (HFO) consumption and the increase of light-end products demand, heavy oil deep processing technology has become the emphasis of world today petroleum refining industry development.At present, the major technique of the raising heavy oil conversion degree of depth, increase light-end products output remains the techniques such as coking, residual oil catalytic cracking and residual hydrocracking.Delayed coking is as a kind of heat processing technique of degree of depth thermally splitting, can be dry gas, liquefied gas, coker gasoline, coker gas oil, wax tailings and coke by heavy oil conversion, it has the advantages such as adaptability to raw material is strong, economic benefit is obvious, is one of most important heavy oil conversion technology.Conventionally the liquid product yield using the yield sum of coker gasoline, coker gas oil and wax tailings as delayed coking, liquid product yield is the most important technico-economical comparison of coking.
The technological process of conventional delayed coking is: fresh feed enters separation column after the preheating of process furnace convection zone, high-temperature-coked oil gas heat exchange at separation column bottom and coke drum, Fractionator Bottom oil enters process furnace radiation section after extracting out, being heated to coking temperature enters coke drum and carries out coking reaction, the coke generating is stayed in coke drum, and the high-temperature oil gas of generation enters separation column from top of coke tower and isolates rich tail gas of coking plant, coker gasoline, coker gas oil and wax tailings.In conventional delay coking process, rich tail gas of coking plant and liquid product can carry a certain amount of coke powder, bring disadvantageous effect to safety, the stable operation of the downstream processes such as hydrogenation, sour water processing, catalysis, and this is the problem that conventional delay coking process exists.In conventional delay coking process, the coking rate of furnace tubing is very fast, serious all the more with the furnace outlet temperature this trend that raises, not only shortened the cycle of operation of process furnace, also limited by improving furnace outlet temperature and improved liquid and receive, this is another problem that conventional delay coking process exists.In current actual device, in order to guarantee the long-term operation of process furnace, furnace outlet temperature is many at 492-498 ℃, and temperature out is less at more than 500 ℃ devices.In conventional delay coking process, the charging of process furnace is by coking oil gas and fresh feed, weighs the liquid phase stream forming after wax tailings heat exchange, the so-called recycle ratio of one of important operational condition in coking process, just refer to the mass ratio of non-fresh feed to fresh feed in this liquid phase stream, the recycle ratio design load of current domestic conventional coking process is many between 0.2～0.4.In conventional delay coking process, along with recycle ratio reduces, the quality of wax tailings and turning oil obviously declines, not only increased the operation easier of the techniques such as downstream hydrogenation, catalysis, and can further shorten the cycle of operation of coking heater, guarantee if the long-term operation of process furnace and reduce furnace outlet temperature, can offset to a certain extent again the Beneficial Effect that recycle ratio declines and brings, this is another problem that conventional delay coking process exists.
In order to realize the flexible of coker recycle ratio, CN1189540C proposed a kind of can flexible recycle ratio the delay coking process of operation, in this technique, coking raw material enters coking heater separately or after mixing with coking recycle oil, be heated to enter coke drum after coking temperature and carry out coking reaction, the coke generating is stayed in coke drum, the high-temperature oil gas generating enters coking fractional distillation column, coking fractional distillation column bottom is extracted coking recycle oil out, coking recycle oil is after heat exchange is cooling, a part is returned coking fractional distillation column bottom as backflow, a part is mixed with coking raw material or/and a part goes out device as product.Have at present the coker of part refinery to adopt this flow process, this technique exists and the similar problem of conventional coking flow process.
(< < refining of petroleum and the chemical industry > > such as Ding Zongyu, the 38th volume, the 8th phase in 1988) developed a kind of coking process of zero recycle ratio, in the method, fresh feed oil does not enter separation column and the direct heat exchange of high-temperature-coked oil gas, but by interchanger and coke chemicals heat exchange, after process furnace, enter coke drum again and carry out pyrogenic reaction, the heavy wax tailings obtaining by separation column is discharged from Fractionator Bottom as coke chemicals.USP4,518,487, USP4,549,934, USP4, the zero recycle ratio coking process of the exploitation such as 661,241 disclosed delay coking process and Ding Zongyu is similar.This technique exists and the similar problem of conventional coking flow process.
Patent CN1212369C discloses a kind of new coking process method.Its core is by the washing oil on the top using a small amount of wax slop as cyclonic separator, and oil at the bottom of cyclonic separator is mixed to the low recycle ratio that the mode that enters again process furnace radiation section realizes coker operates with fresh feed.Also there is the problem that furnace tubing coking rate is very fast, affect the process furnace cycle of operation in this technique, particularly the recycle ratio of this processing method is limited to 0.05-0.1:1, when raw material fluctuates larger, especially when work condition abnormality need increase while circulating recently setting device, cannot operation be adjusted accordingly by recycle ratio restriction, thereby the limitation of this technique practical application is larger.
The high-temperature oil gas that CN200810012208.X proposes coker to produce, through coke powder tank decoking powder, is extracted light constituent simultaneously, and heavy constituent enters vacuum distillation apparatus, isolates wax oil cut, and the vacuum residuum of gained is as coking charging.In CN200810012208.X, decoking powder tank removes coke powder by inert solid fillers, when coke powder content is slightly large, coke powder and the viscous oil of filling surface greatly decline packing efficiency on the one hand, heavy constituent at the bottom of decoking powder tank still contains a certain amount of coke powder on the other hand, and this part heavy constituent is sent to vacuum fractionation tower continuation fractionation, affected the separating effect of vacuum fractionation tower, the liquid distillate that separation obtains is also easily containing coke powder.
Summary of the invention
In order to overcome the deficiencies in the prior art, the invention provides a kind of processing method of delayed coking, the method can improve liquid product yield simultaneously and improve coke chemicals quality.The present invention also provides a kind of device of implementing above-mentioned processing method.
A processing method for delayed coking, comprising: the high-temperature oil gas from top of coke tower is carried out to flash distillation, and the liquid phase stream after flash distillation is divided into containing the more logistics of coke powder with containing the less logistics of coke powder by gravity or rotational flow settlement; Gas gas-phase objects diffluence separation column after flash distillation is separated into rich tail gas of coking plant, coker gasoline, coker gas oil and wax tailings; The described backflow as flash distillation containing the less logistics of coke powder or the described mixing oil containing the less logistics of coke powder and coking distillate composition; The mixing oil of stock oil or stock oil and Fractionator Bottom oil, after process furnace convection zone and radiation section heating, mixes containing the more logistics of coke powder with described, then enters coke drum reaction; 410～440 ℃ of the service temperatures of flash distillation, the mass ratio of described flash distillation backflow and fresh feed is 0.05～0.15:1; Described is 0.01～0.05:1 containing the more logistics of coke powder and the mass ratio of fresh feed; Recycle ratio is 0.05～0.8:1.
In the present invention, recycle ratio refers in the charging of coke drum, non-fresh feed oil part and fresh feed oil mass ratio partly.
Described coking distillate is selected from one or more in coker gasoline, coker gas oil, coking stage casing oil, wax tailings and Fractionator Bottom oil, is preferably Fractionator Bottom oil.
The temperature of flash distillation is preferably 410 ℃～425 ℃.
In preferred situation, Fractionator Bottom oil is extracted out, a part is extracted oily backflow separation column out; A part extract out oil with described containing the less logistics of coke powder jointly as the backflow of flash distillation; All the other extract oil out as a part for product and/or furnace charge.
The operating parameters of gravity settling is relevant with stock oil character and coker operations condition.Those skilled in the art know the process of gravity settling.By simple experiment, those skilled in the art can easily determine corresponding operating parameters.The charging residence time of gravity settling is generally 1～10h, preferably 1～5h.Containing the more logistics of coke powder outlet operated by rotary motion at liquid phase bottommost, containing the less logistics outlet operated by rotary motion of coke powder on liquid phase top the position near liquid level, opening for feed position arranges should guarantee that the upper and lower liquid phase of opening for feed all has enough height.
Existing gravity settling equipment all can be the present invention and adopts.Gravity settling equipment preferably adopts slurry tank.At the bottom of flashing tower, oil enters slurry tank, and at the bottom of slurry tank, oil enters coke drum reaction after mixing with furnace outlet logistics, sedimentation tank deck oily independent or with coking distillate jointly as the backflow of flash distillation.At the bottom of described slurry tank, oil is 0.01～0.05:1 with the mass ratio of fresh feed.
Process furnace radiation section temperature out is 490～510 ℃, preferably 495～508 ℃.Top of coke tower pressure is generally 0.1～0.3MPa.
Coking raw material oil is generally the heavy oil that initial boiling point is greater than 350 ℃, can be selected from one or more in long residuum, vacuum residuum, visbroken resids, heavy deasphalted oil, catalytically cracked oil, viscous crude, topped crude, shale oil and liquefied coal coil.The so-called head that pulls out refers to that the pre-treatment step of crude oil before atmospheric and vacuum distillation, topped crude are exactly the cut of crude oil after light constituent is extracted in flash distillation.In China, viscous crude refers to that viscosity under reservoir temperature is greater than the crude oil of 50mPa.s.
The present invention also provides a kind of delayed coking unit, sets up flashing tower and settling vessel between coke drum and separation column; Flashing tower is provided with oil gas entrance, and flash distillation tower top is provided with oil gas vent and reflux inlet, is provided with oil export at the bottom of tower at the bottom of flashing tower; Settling vessel is provided with opening for feed, and settling vessel top is provided with top oil export, and settling vessel bottom is provided with end oil export; Top of coke tower oil gas vent pipeline and flashing tower oil gas source line are connected, and flashing tower oil gas vent pipeline and fractionating tower oil gas source line are connected, and at the bottom of flashing tower tower, oil export pipeline and settling vessel feeding hole pipeline are connected; Settling vessel top oil export pipeline and flashing tower reflux inlet pipeline are connected, and the pipeline that at the bottom of settling vessel, oil export pipeline and process furnace radiation section enter coke drum is connected; Fractionator Bottom oil export and process furnace convection zone entrance are connected; The outlet of process furnace convection zone is connected with process furnace radiation section entrance.
Each technical characterictic in the present invention, without prejudice to the object of the invention and can arbitrary combination not conflicting in the situation that, it belongs to scope disclosed by the invention equally.
In conventional delay coking process, the rich tail gas of coking plant obtaining by separation column separation, liquid distillate and turning oil can carry a certain amount of coke powder, have a strong impact on safety, the stable operation of downstream process and coking heater.At fluctuation or by enforcement, improve furnace outlet temperature, reduce recycle ratio and improve liquid and bring drill to an end while doing, above-mentioned phenomenon is further obvious.Although improved delay coking process can promote the raising that liquid is received by the low recycle ratio operation of delayed coking.But when liquid is received raising, the Quality Down trend of rich tail gas of coking plant, sideline product and the turning oil being caused by coke powder and unreacted heavy constituent also clearly, can affect equally cycle of operation of coker and downstream process and operational stability, safety, similar with common process, this has limited by improving furnace outlet temperature and has further improved liquid and receive.The improvement technique particularly having can only be confined to the operation of low recycle ratio, cannot adjusting operation when raw material fluctuation or work condition abnormality need increase recycle ratio and guarantee safety in production, and cause technique to have certain limitation.
The first STRENGTH ON COKE tower top of the present invention high-temperature oil gas is carried out flash distillation, most of coke powder is wherein removed, and then made it enter separation column, can obviously improve the quality of rich tail gas of coking plant, sideline product and turning oil.Existing coking process, be rich in the turning oil of coke powder all by the radiation section of process furnace, and most of coke powder does not enter separation column and process furnace radiation section in the present invention, specifically, the present invention is divided into flash distillation liquid phase stream containing the more logistics of coke powder with containing the less logistics of coke powder by sedimentation, containing the less logistics of coke powder separately or with coking distillate jointly as the backflow of flash distillation; Containing the more logistics of coke powder, do not enter the radiation section of process furnace, but after mixing with the logistics of furnace outlet, enter coke drum reaction, avoided the disadvantageous effect to process furnace, can be at the lower operation process furnace of conventional or higher temperature (being greater than 500 ℃ to 510 ℃), not only can improve liquid and receive, and can extend the cycle of operation of process furnace.
Accompanying drawing explanation
Accompanying drawing 1 is the block diagram of a kind of preferred implementation of the present invention.
Accompanying drawing 2 is block diagrams of a kind of embodiment of conventional delayed coking.
Accompanying drawing 3 is block diagrams of a kind of embodiment of Adjustable Recirculating Ratio flow process.
Embodiment
Below in conjunction with accompanying drawing, further set forth the present invention, accompanying drawing is only a kind of preferred implementation of the present invention, is not construed as limiting the invention.
After the fresh coking raw material part Fractionator Bottom oil oily and from pipeline 23 of pipeline 1 mixes, successively by process furnace convection zone 2, radiation section 4, furnace outlet logistics 19 mixes with oil 18 at the bottom of slurry tank, then entering coke drum 5 reacts, the coke generating is stayed in coke drum, top of coke tower oil gas 6 enters flashing tower 7, the withdrawing oil counter current contact entering with flashing tower jacking, withdrawing oil is that flashing tower temperature is by backflow fuel-flow control from the sedimentation tank deck oil of pipeline 20 with from the mixing oil of the Fractionator Bottom oil of pipeline 22; By flash distillation, the coke powder in high-temperature oil gas and part heavy constituent are separated, and withdrawing oil purifies oil gas by the remaining coke powder in washing flash distillation tower top oil gas.Flash distillation tower top oil gas 8 after purification is gone to separation column 3, and at the bottom of flashing tower, oil 16 is gone to slurry tank 17; High-temperature oil gas in flashing tower 7 seals in slurry tank 17, can slurry tank liquid level be arranged higher than slurry tank opening for feed more than 2 meters, general 2～3 meters, certainly those skilled in the art also can adopt other technique means, these technique means belong to prior art, and the present invention repeats no more this; By gravity settling, coke powder is to enrichment at the bottom of slurry tank, and sedimentation tank deck oil 20 is gone to flash distillation tower top, with Fractionator Bottom oil from pipeline 22 jointly as the backflow of flashing tower.High-temperature oil gas 8 from flash distillation tower top enters separation column in separation column bottom, through separation column, be separated into rich tail gas of coking plant 12, coker gasoline 13, coker gas oil 14, wax tailings 15, Fractionator Bottom oil is divided into three parts after extracting out, a part is as refluxing by pipeline 21 backflow separation columns, a part is the part as flash distillation withdrawing oil by pipeline 22, and all the other go to process furnace by pipeline 23 together with after fresh feed mixing.
Embodiment 1
The present embodiment adopts the flow process of accompanying drawing 1, and the present embodiment explanation adopts the situation of 503 ℃ of higher recycle ratios 0.4, higher furnace outlet temperature.In actual condition, when recycle ratio is 0.4 time, the furnace outlet temperature of coker is generally no more than 500 ℃.
From the stock oil of pipeline 1 with after part Fractionator Bottom oil from pipeline 23 mixes, successively by process furnace convection zone 2, radiation section 4, after being warmed up to 503 ℃, entering coke drum 5 reacts, recycle ratio is in the charging of 0.4:1(coke drum, non-fresh feed oil part and fresh feed oil mass ratio partly); The coke generating is stayed in coke drum, the coking oil gas generating enters flashing tower, sedimentation tank deck oil mixes as withdrawing oil and injects flash distillation tower top with the part Fractionator Bottom oil of extracting out, and the mass ratio of withdrawing oil and fresh feed is 0.08:1,420 ℃ of flash distillation tower top oil gas temperature; Flash distillation tower top oil gas 8 after purification is gone to coking fractional distillation column, and at the bottom of flashing tower, oil 16 is gone to slurry tank, and slurry tank liquid level is higher than 2.5 meters of slurry tank opening for feeds, and the slurry tank charging residence time is 3h; At the bottom of slurry tank, oil 18 is gone to coke drum after mixing with furnace outlet logistics 19 from slurry tank is extracted out, and at the bottom of slurry tank, oil is 0.02:1 with the mass ratio of fresh feed; Finally by separation column separation, obtain rich gas, coker gasoline, coker gas oil, wax tailings, wherein, rich tail gas of coking plant, coker gasoline, coker gas oil and wax tailings go out device as product; Fractionator Bottom oil is divided into three parts after extracting out, and part conduct refluxes by pipeline 21 backflow separation columns, and a part is the part as the withdrawing oil of flash distillation by pipeline 22, and all the other go to process furnace by pipeline 23 together with after fresh feed mixing.Feedstock property is listed in table 1, and product distributes and lists in table 2, and wax tailings character is listed in table 3.Wax tailings is sent to wax oil backwash filter and filters, the backwashing period of backwash filter is listed in table 4.
Embodiment 2
The present embodiment adopts the flow process of accompanying drawing 1, process condition when the present embodiment explanation adopts the low recycle ratio of often taking in current actual production, lower furnace outlet temperature.
Adopt the vacuum residuum feed identical with embodiment 1.From the stock oil of pipeline 1 with after part Fractionator Bottom oil from pipeline 23 mixes, successively by process furnace convection zone 2, radiation section 4, after being warmed up to 496 ℃, entering coke drum 5 reacts, recycle ratio is in the charging of 0.1:1(coke drum, non-fresh feed oil part and fresh feed oil mass ratio partly); The coke generating is stayed in coke drum, the coking oil gas generating enters flashing tower, sedimentation tank deck oil mixes as withdrawing oil and injects flash distillation tower top with the part Fractionator Bottom oil of extracting out, and the mass ratio of withdrawing oil and fresh feed is 0.08:1,420 ℃ of flash distillation tower top oil gas temperature; Flash distillation tower top oil gas 8 after purification is gone to coking fractional distillation column, and at the bottom of flashing tower, oil 16 is gone to slurry tank, and slurry tank liquid level is higher than 2.5 meters of slurry tank opening for feeds, and the slurry tank charging residence time is 3h; At the bottom of slurry tank, oil 18 is gone to coke drum after mixing with furnace outlet logistics 19 from slurry tank is extracted out, and at the bottom of slurry tank, oil is 0.02:1 with the mass ratio of fresh feed; Finally by separation column separation, obtain rich gas, coker gasoline, coker gas oil, wax tailings, wherein, rich tail gas of coking plant, coker gasoline, coker gas oil and wax tailings go out device as product; Fractionator Bottom oil is divided into three parts after extracting out, and part conduct refluxes by pipeline 21 backflow separation columns, and a part is the part as the withdrawing oil of flash distillation by pipeline 22, and all the other go to process furnace by pipeline 23 together with after fresh feed mixing.Feedstock property is listed in table 1, and product distributes and lists in table 2, and wax tailings character is listed in table 3.Wax tailings is sent to wax oil backwash filter and filters, the backwashing period of backwash filter is listed in table 4.
Embodiment 3
The present embodiment adopts the flow process of accompanying drawing 1, and the present embodiment illustrates process condition when this processing method adopts low recycle ratio, higher furnace outlet temperature.
Adopt the vacuum residuum feed identical with embodiment 1.From the stock oil of pipeline 1 with after part Fractionator Bottom oil from pipeline 23 mixes, successively by process furnace convection zone 2, radiation section 4, after being warmed up to 503 ℃, entering coke drum 5 reacts, recycle ratio is in the charging of 0.1:1(coke drum, non-fresh feed oil part and fresh feed oil mass ratio partly); The coke generating is stayed in coke drum, the coking oil gas generating enters flashing tower, sedimentation tank deck oil mixes as withdrawing oil and injects flash distillation tower top with the part Fractionator Bottom oil of extracting out, and the mass ratio of withdrawing oil and fresh feed is 0.08:1,420 ℃ of flash distillation tower top oil gas temperature; Flash distillation tower top oil gas 8 after purification is gone to coking fractional distillation column, and at the bottom of flashing tower, oil 16 is gone to slurry tank, and slurry tank liquid level is higher than 2.5 meters of slurry tank opening for feeds, and the slurry tank charging residence time is 3h; At the bottom of slurry tank, oil 18 is gone to coke drum after mixing with furnace outlet logistics 19 from slurry tank is extracted out, and at the bottom of slurry tank, oil is 0.02:1 with the mass ratio of fresh feed; Finally by separation column separation, obtain rich gas, coker gasoline, coker gas oil, wax tailings, wherein, rich tail gas of coking plant, coker gasoline, coker gas oil and wax tailings go out device as product; Fractionator Bottom oil is divided into three parts after extracting out, and part conduct refluxes by pipeline 21 backflow separation columns, and a part is the part as the withdrawing oil of flash distillation by pipeline 22, and all the other go to process furnace by pipeline 23 together with after fresh feed mixing.Feedstock property is listed in table 1, and product distributes and lists in table 2, and wax tailings character is listed in table 3.Wax tailings is sent to wax oil backwash filter and filters, the backwashing period of backwash filter is listed in table 4.
Comparative example 1
This comparative example explanation adopt compared with systemic circulation than time conventional delay coking process situation.
Adopt the vacuum residuum feed identical with embodiment 1.General flow chart as shown in Figure 2, stock oil 1 is divided into two bursts of chargings and enters separation column 7 bottoms after 2 preheatings of process furnace convection zone, in separation column bottom from the high-temperature oil gas 6 and stock oil upper feeding of coke drum 5, the liquid phase stream forming after 12 heat exchange of coking wax slop mixes with stock oil in separation column bottom, Fractionator Bottom oil is sent to process furnace radiation section 3 after extracting out, in Fractionator Bottom oil, the mass ratio of turning oil and fresh vacuum residuum feed is 0.4:1, through process furnace radiation section 3, being heated to 498 ℃ enters coke drum 5 by pipeline 4 and reacts, the high-temperature oil gas that coking produces enters separation column 7 separation, obtain rich tail gas of coking plant 8, coker gasoline 9, coker gas oil 10 and wax tailings 11, wax tailings 11 is sent to wax oil backwash filter to be filtered.Feedstock property is listed in table 1, and product distributes and lists in table 2, and wax tailings character is listed in table 3.Wax tailings is sent to wax oil backwash filter and filters, the backwashing period of backwash filter is listed in table 4.
Comparative example 2
This comparative example explanation adopt partial circulating than time conventional delay coking process situation.
Adopt the vacuum residuum feed identical with embodiment 1.General flow chart as shown in Figure 2, stock oil 1 is divided into two bursts of chargings and enters separation column 7 bottoms after 2 preheatings of process furnace convection zone, in separation column bottom from the high-temperature oil gas 6 and stock oil upper feeding of coke drum 5, the liquid phase stream forming after 12 heat exchange of coking wax slop mixes with stock oil in separation column bottom, Fractionator Bottom oil is sent to process furnace radiation section 3 after extracting out, in Fractionator Bottom oil, the mass ratio of turning oil and fresh vacuum residuum feed is 0.1:1, through process furnace radiation section 3, being heated to 496 ℃ enters coke drum 5 by pipeline 4 and reacts, the high-temperature oil gas that coking produces enters separation column 7 separation, obtain rich tail gas of coking plant 8, coker gasoline 9, coker gas oil 10 and wax tailings 11, wax tailings 11 is sent to wax oil backwash filter to be filtered.Feedstock property is listed in table 1, and product distributes and lists in table 2, and wax tailings character is listed in table 3.Wax tailings is sent to wax oil backwash filter and filters, the backwashing period of backwash filter is listed in table 4.
Comparative example 3
This comparative example explanation adopt systemic circulation than time Adjustable Recirculating Ratio coking process situation.
Adopt the vacuum residuum feed identical with embodiment 1.General flow chart as shown in Figure 3, after stock oil 1 heat exchange, (in figure, do not express heat exchange) and enter surge tank 2 with after part Fractionator Bottom oil mixes, at the bottom of surge tank, oil is successively by process furnace convection zone 3, radiation section 4, after being warmed up to 498 ℃, entering coke drum 5 reacts, the oil gas 6 of top of coke tower enters separation column 7 bottoms and carries out separation, separation obtains rich tail gas of coking plant 8, coker gasoline 9, coker gas oil 10 and wax tailings 11, wax tailings 11 is sent to wax oil backwash filter and filters.Fractionator Bottom oil is extracted out, and a part of Fractionator Bottom oil mixes and is sent to surge tank with fresh feed 1 as turning oil, and all the other are divided into two strands and return to the washing oil of separation column bottom at the bottom of as tower.In surge tank, the mass ratio of turning oil and fresh vacuum residuum feed is 0.4:1.Feedstock property is listed in table 1, and product distributes and lists in table 2, and wax tailings character is listed in table 3.Wax tailings is sent to wax oil backwash filter and filters, the backwashing period of backwash filter is listed in table 4.
Comparative example 4
This comparative example explanation adopt partial circulating than time Adjustable Recirculating Ratio coking process situation.
Adopt the vacuum residuum feed identical with embodiment 1.General flow chart as shown in Figure 3, after stock oil 1 heat exchange, (in figure, do not express heat exchange) and enter surge tank 2 with after part Fractionator Bottom oil mixes, at the bottom of surge tank, oil is successively by process furnace convection zone 3, radiation section 4, after being warmed up to 496 ℃, entering coke drum 5 reacts, the oil gas 6 of top of coke tower enters separation column 7 bottoms and carries out separation, separation obtains rich tail gas of coking plant 8, coker gasoline 9, coker gas oil 10 and wax tailings 11, wax tailings 11 is sent to wax oil backwash filter and filters.Fractionator Bottom oil is extracted out, and a part of Fractionator Bottom oil mixes and is sent to surge tank with fresh feed 1 as turning oil, and all the other are divided into two strands and return to the washing oil of separation column bottom at the bottom of as tower.In surge tank, the mass ratio of turning oil and fresh vacuum residuum feed is 0.1:1.Feedstock property is listed in table 1, and product distributes and lists in table 2, and wax tailings character is listed in table 3.Wax tailings is sent to wax oil backwash filter and filters, the backwashing period of backwash filter is listed in table 4.
Table 1 postpones feedstock property
| Density (20 ℃), kg/m 3 | 972.1 |
| Carbon residue, % | 14.1 |
| Sulphur content, % | 2.20 |
| Stable hydrocarbon, % | 22.1 |
| Aromatic hydrocarbons, % | 35.5 |
| Colloid+bituminous matter, % | 42.4 |
Table 2 delayed coking product distributes
Table 3 wax tailings character
| Project name | Comparative example 1 | Comparative example 2 | Comparative example 3 | Comparative example 4 | Example 1 | Example 2 | Example 3 |
| Density (20 ℃), kg/m 3 | 896.5 | 899.3 | 896.6 | 899.5 | 895.8 | 898.5 | 897.5 |
| Sulphur content, m% | 0.73 | 0.85 | 0.73 | 0.86 | 0.75 | 0.84 | 0.78 |
| Nitrogen content, ug/g | 4579 | 5036 | 4588 | 5045 | 4573 | 5019 | 5008 |
| Carbon residue, m% | 0.37 | 0.81 | 0.36 | 0.80 | 0.36 | 0.76 | 0.73 |
The backwashing period of table 4 wax tailings backwash filter
| Project name | Comparative example 1 | Comparative example 2 | Comparative example 3 | Comparative example 4 | Example 1 | Example 2 | Example 3 |
| Backwashing period | 1.5h | 1h | 1.5h | 1h | 4.5h | 4.5h | 4.5h |
Claims (9)
1. a processing method for delayed coking, comprising: the high-temperature oil gas from top of coke tower is carried out to flash distillation, and the liquid phase stream after flash distillation is divided into containing the more logistics of coke powder with containing the less logistics of coke powder by gravity or rotational flow settlement; Gas gas-phase objects diffluence separation column after flash distillation is separated into rich tail gas of coking plant, coker gasoline, coker gas oil and wax tailings; The described backflow as flash distillation containing the less logistics of coke powder or the described mixing oil containing the less logistics of coke powder and coking distillate composition; The mixing oil of stock oil or stock oil and Fractionator Bottom oil, after process furnace convection zone and radiation section heating, mixes containing the more logistics of coke powder with described, then enters coke drum reaction; 410～440 ℃ of the service temperatures of flash distillation, the mass ratio of described flash distillation backflow and fresh feed is 0.05～0.15:1; Described is 0.01～0.05:1 containing the more logistics of coke powder and the mass ratio of fresh feed; Recycle ratio is 0.05～0.8:1.
2. in accordance with the method for claim 1, it is characterized in that, Fractionator Bottom oil is extracted out, and a part is extracted oily backflow separation column out; A part extract out oil with described containing the less logistics of coke powder jointly as the backflow of flash distillation; All the other extract oil out as a part for product and/or furnace charge.
3. in accordance with the method for claim 1, it is characterized in that, process furnace radiation section temperature out is 490～510 ℃.
4. in accordance with the method for claim 3, it is characterized in that, process furnace radiation section temperature out is for being greater than 500 ℃ to 510 ℃.
5. in accordance with the method for claim 1, it is characterized in that, the charging residence time of sedimentation is 1～10h.
6. in accordance with the method for claim 1, it is characterized in that, gravity settling equipment adopts slurry tank, and at the bottom of flashing tower, oil enters slurry tank, at the bottom of slurry tank, oil enters coke drum reaction after mixing with furnace outlet logistics, sedimentation tank deck oily independent or with coking distillate jointly as the backflow of flash distillation.
7. in accordance with the method for claim 1, it is characterized in that, described coking distillate is selected from one or more in coker gasoline, coker gas oil, coking stage casing oil, wax tailings and Fractionator Bottom oil.
8. in accordance with the method for claim 1, it is characterized in that, described stock oil is selected from one or more in long residuum, vacuum residuum, visbroken resids, heavy deasphalted oil, catalytically cracked oil, viscous crude, topped crude, shale oil and liquefied coal coil.
9. a delayed coking unit, is characterized in that, sets up flashing tower and settling vessel between coke drum and separation column; Flashing tower is provided with oil gas entrance, and flash distillation tower top is provided with oil gas vent and reflux inlet, is provided with oil export at the bottom of tower at the bottom of flashing tower; Settling vessel is provided with opening for feed, and settling vessel top is provided with top oil export, and settling vessel bottom is provided with end oil export; Top of coke tower oil gas vent pipeline and flashing tower oil gas source line are connected, and flashing tower oil gas vent pipeline and fractionating tower oil gas source line are connected, and at the bottom of flashing tower tower, oil export pipeline and settling vessel feeding hole pipeline are connected; Settling vessel top oil export pipeline and flashing tower reflux inlet pipeline are connected, and the pipeline that at the bottom of settling vessel, oil export pipeline and process furnace radiation section enter coke drum is connected; Fractionator Bottom oil export and process furnace convection zone entrance are connected; The outlet of process furnace convection zone is connected with process furnace radiation section entrance.
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| WO2021135802A1 (en) * | 2019-12-31 | 2021-07-08 | 中国石油化工股份有限公司 | System and method for producing needle coke |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1417294A (en) * | 2001-11-06 | 2003-05-14 | 中国石化集团长岭炼油化工有限责任公司 | Delayed coking process capable of flexibly regulating circulation ratio |
| CN1417293A (en) * | 2001-10-30 | 2003-05-14 | 中国石油化工股份有限公司 | Delayed coking process with low circulation ratio |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN1417293A (en) * | 2001-10-30 | 2003-05-14 | 中国石油化工股份有限公司 | Delayed coking process with low circulation ratio |
| CN1417294A (en) * | 2001-11-06 | 2003-05-14 | 中国石化集团长岭炼油化工有限责任公司 | Delayed coking process capable of flexibly regulating circulation ratio |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2021135802A1 (en) * | 2019-12-31 | 2021-07-08 | 中国石油化工股份有限公司 | System and method for producing needle coke |
| US11946003B2 (en) | 2019-12-31 | 2024-04-02 | China Petroleum & Chemical Corporation | System and method for producing needle coke |
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