CN209383711U - The full fraction ethylene bottom oil delayed coking production system of non-impurity-doped - Google Patents
The full fraction ethylene bottom oil delayed coking production system of non-impurity-doped Download PDFInfo
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- CN209383711U CN209383711U CN201821881588.6U CN201821881588U CN209383711U CN 209383711 U CN209383711 U CN 209383711U CN 201821881588 U CN201821881588 U CN 201821881588U CN 209383711 U CN209383711 U CN 209383711U
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G55/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process
- C10G55/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process plural serial stages only
- C10G55/04—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process plural serial stages only including at least one thermal cracking step
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
- C10G9/14—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils in pipes or coils with or without auxiliary means, e.g. digesters, soaking drums, expansion means
- C10G9/16—Preventing or removing incrustation
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
- C10G9/14—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils in pipes or coils with or without auxiliary means, e.g. digesters, soaking drums, expansion means
- C10G9/18—Apparatus
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
- C10G9/14—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils in pipes or coils with or without auxiliary means, e.g. digesters, soaking drums, expansion means
- C10G9/18—Apparatus
- C10G9/20—Tube furnaces
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1037—Hydrocarbon fractions
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/02—Gasoline
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/04—Diesel oil
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- General Chemical & Material Sciences (AREA)
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- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The utility model discloses a kind of full fraction ethylene bottom oil delayed coking production systems of non-impurity-doped, including feed system, flood pattern, heating furnace, coking still and gas recovery system for oil, heating furnace includes convection section and radiant section, and convection section is connected to radiant section, the entrance of convection section is feed end, the outlet of radiant section is discharge end, and the feed end of heating furnace is connected to the outlet line of feed system and steam injection system respectively；The discharge end of heating furnace and the inlet communication of coking still, the kettle top of coking still are connected with gas recovery system for oil.The utility model provide a kind of step it is simple, without catalyst, without preposition processing, without doping for full fraction ethylene bottom oil for carrying out delayed coking production system, realize full fraction ethylene bottom oil delay coking process consecutive production, it is simple that each fraction section of gained can carry out processing procedure of processing according to conventional refinery's production procedure, without catalyst and the operating condition without changing existing deep processing, economic cost is saved.
Description
Technical field
The utility model belongs to petroleum refining technology field more particularly to a kind of full fraction ethylene bottom oil delay coke of non-impurity-doped
Change production system.
Background technique
With the development of world economy, petroleum resources are being gradually decreased, and limited petroleum resources are rationally made good use of, to refining
Oily industry is particularly important.Currently, oil refining industry faces crude oil heaviness, high-sulfurized, cause demand to light oil into one
A series of problems, such as step increases.
Ethylene bottom oil is the by-product of cracking of ethylene, the composition of ethylene bottom oil is extremely complex, mainly there is alkane, C8-C15
Aromatic hydrocarbons, the fragrant impurity contents such as alkene and heterocyclic compound, sulphur and nitrogen are low, are substantially free of metal impurities.Boiling range 218 DEG C~
420℃.Plan to arrange according to China " 13 ", national ethylene production capacity increases production 7,000,000 tons/year to 2020, and ethylene bottom oil will
Reach 335.4 ten thousand tons/year or so.Currently, ethylene bottom oil is mainly used as fuel use, overall utilization rate is not high, and economic value is low, and
Ethylene bottom oil contains heavy arene etc., and when burning is also easy to produce coking and black smoke, pollutes environment.To sum up, using ethylene bottom oil as raw material
Production technology research and development, be of great significance.
Applicant has made intensive studies the delayed coking processing technology of ethylene bottom oil, and discovery has following characteristics:
1, processing and utilization is carried out after mixing ethylene bottom oil and other substances
Major part producer is to carry out delayed coking with the conventional coking blending ethylene tar of decompression residuum both at home and abroad；It is related to subtract
The report that pressure residual oil blending ethylene tar carries out delayed coking has: CN101608132A, " Responds Surface Methodology optimizes blending ethylene
The delayed coking of pyrolysis fuel oil is studied " (see " petroleum refining and chemical industry " the 8th phase P5-P8 in 2009, " delayed coking unit mixes refining
The research of grand celebration pyrolysis fuel oil " (see " petroleum refining and chemical industry " the 12nd phase P20-P22 in 2007), " blending ethylene cracking masout
Influence to delayed coking " (see " petrochemical technology and application " the 1st phase P44-P49 in 2010) and " decompression residuum blending ethylene weight
The test of tar co carbonization " (see " Maoming College's journal " the 1st phase P7-P9 in 2008 etc., these researchs are to evaporate ethylene bottom oil entirely
Divide and mix refining as delayed coking raw material with decompression residuum, can make the yield of liquid yield and light Fuel oil product lower in this way,
And liquid product --- the quality of coker gasoline, diesel oil and wax oil is still poor, also further processing is needed to handle for its gained.
2, ethylene bottom oil is raw material to prepare other products, but needs the program of preposition processing or fractionation
The land CN200810228387.0, CN200910187925.0, CN201010227457.8, CN201110350788.5
Continuous to disclose a kind of processing method of ethylene bottom oil, process characteristic is that ethylene bottom oil is fractionated into light fraction and heavy distillat, weight
Fraction is mixed with conventional coking raw material, and delayed coking obtains coker gasoline and coker gas oil, wax tailings, resulting coking vapour
Oil and coker gas oil are mixed with ethylene bottom oil light fraction, obtain mixed raw material, then carry out hydrofining reaction.The technical solution is simultaneously
The non-ethylene bottom oil for full fraction carries out, and subsequent operation can just be carried out by needing to carry out preposition fractionation.
3, temporarily there is the relevant report that delayed coking is carried out for pure, undoped full fraction ethylene bottom oil without discovery
CN201410705660.X discloses a kind of method with ethylene bottom oil production high-purity petroleum coke, by ethylene bottom oil
After being mixed with lighter component oil according to the weight ratio of 1:0.05-0.2, send to cracking coking furnace and distilled, that is, produce high-purity
Petroleum coke；Although the patent document declared multiple times are the ethylene bottom oils for full fraction, it has still carried out preposition doping
The step of (be mixed with a certain proportion of light component).
4, the prior art generally believes that the pyrogenetic reaction temperature of delay coking process is 495-505 DEG C, and temperature is excessively high or mistake
Low will lead to can not green coke or tube coking
The monograph " delayed coking " that Liang Chaolin, Shen Benxian are published in Sinopec publishing house page 5 discloses delayed coking
Process characteristic: " difference of delayed coking and other coking methods is the boiler tube that residual oil flows through heating furnace with high flow velocity, heating
500-505 DEG C of temperature needed for reaction, subsequently into coke drum, the heat in coke drum by itself bringing into carries out cracking contracting
The reaction such as conjunction "；
The periodical " linguistic term of delayed coking experimental rig " that Liang Chaolin, Shen Benxian, Wu Shikui are delivered, Xiao Huafang is delivered
The periodical research and utilization of pyrolysis fuel oil " be in progress ", describe and decompression residuum, ethylene heavy tar and their object of mixing exist
The reaction of co carbonization noncontinuity is carried out in tubular type coking reactor.The result shows that mixing ethylene heavy tar skill in decompression residuum
Art is feasible, but presses the conventional coking process of decompression residuum, and raw material must first pass through the convection type of heating furnace, with relatively low temperature
(300 DEG C) fractionating section fraction, then frequent pressure fractionating tower bottom pick out the radiant type into heating furnace, with relatively high temperature (500
DEG C) carry out pyrogenetic reaction.
Summary " the ethylene bottom oil comprehensive utilizating research in periodical " Shandong petrochemical industry " 2018 the 46th curly hair tables such as Wang Jian
Progress " in, mentioning ethylene bottom oil as the reaction temperature of the raw material of delayed coking is 500 DEG C；
Liu Jianshan etc. is in curly hair table " the delay coking heating furnace excess air of periodical " oil and gas chemical industry " 2017 the 46th
Measure influence to its cycle of operation " in analyze Furnace Tube of Coker Unit Coking Mechanism, be proposed for coking and be inclined to weaker original
Material, can be used higher heater outlet temperature, temperature is too low, and reaction depth is inadequate, is unfavorable for being normally carried out for green coke process；Such as with
Thin oil decompression residuum is raw material, and Furnace Tube of Coker Unit outlet temperature is 502 DEG C.Stronger raw material is inclined to for coking, can be adopted
With relatively low heater outlet temperature, temperature is excessively high, and pyrogenetic reaction depth is excessive, and the coke of generation is harder, the easy coking of boiler tube.Such as
Using high viscous crude as raw material, Furnace Tube of Coker Unit outlet temperature is 497 DEG C.
Therefore, those skilled in the art think to manage using the raw material of delay coking process production in order to guarantee production effect
The coking temperature thought is corresponding at 495-505 DEG C or so, if pyrogenetic reaction temperature is too low, reaction depth and speed are reduced, and makes coke
Tower froth bed increases, and easily causes the fugitive constituent increase for rushing tower, volatilization knot coke, coke, quality decline；Pyrogenetic reaction temperature mistake
Height, reaction depth and speed increase, and gas, gasoline, diesel yield rise, wax oil and coke yield decline, the fugitive constituent of coke
It reduces, Quality advance, but coke is hardened, decoking is difficult, and tube coking trend increases, and on-stream time shortens.
And the composition of ethylene bottom oil is extremely complex, mainly have alkane, the aromatic hydrocarbons of C8-C15, alkene, colloid, asphalitine and
Heterocyclic compounds such as sulphur, nitrogen, oxygen etc..Although it is rich in aromatic hydrocarbons, since the source of other raw materials of it and delayed coking exists
Bigger difference, thus chemical composition, in terms of and delayed coking other raw materials there is also larger differences.China from
The research and development of needle coke production technology are started the end of the seventies, and using thermal cracking residue and catalytic cracking clarified oil as raw material
Qualified needle coke product has been produced on commercial plant.And in the medium-sized test for producing needle coke using ethylene bottom oil as raw material
In research, it is found that boiler tube coke heavy, device are forced to stop work.
To sum up seeing, those skilled in the art think that ethylene bottom oil, which is carried out delayed coking production as single raw material, is
It can not implement, this is also that existing ethylene bottom oil mixes delay coke after refining in delayed coking or with other conventional coking raw materials
Change or pre-treatment separation heavy distillat is carried out to ethylene coke and mixes progress delayed coking with conventional coking raw material.
Therefore, how to carry out delayed coking production as single raw material using ethylene bottom oil is the technology for needing to solve at present
Problem.
Utility model content
The technical issues of the utility model is intended to solve above-mentioned ethylene bottom oil deep processing to a certain extent in the related technology it
One.Therefore, the purpose of this utility model is to provide a kind of steps simply, handles, without catalyst, without preposition without adulterating
For full fraction ethylene bottom oil for carrying out delayed coking production system.
To achieve the goals above, the technical solution adopted in the utility model is:
The major technology bottleneck of ethylene bottom oil is the fouling of the heat-exchange system that can cause delayed coking, pipeline, furnace tubing
Aggravation is accelerated in coking, seriously affects the normal operation and on-stream time of delayed coking unit.Analysis reason is: cracking of ethylene is burnt
The unsaturated hydrocarbons such as alkene, alkynes and heterocyclic compound content are higher in oil, and chemical property is active, and oxidation stability is poor, easily send out
It is born from polycondensation, secondary new gum asphalt etc.；In heat exchange temperature-rise period, since solvent effect and fuel factor necessarily all can
It changes, therefore metastable colloidal dispersion just loses stability, primary and secondary asphalitine meeting to ethylene bottom oil originally
Coagulation and be attached on tube wall and wall not with stream flow, form asphalitine grease, asphalitine is further condensed green coke.
The full fraction ethylene bottom oil delay coking process of the non-impurity-doped of the utility model much changes in view of the above-mentioned problems, having done
Into, last improved technique the following steps are included:
(1) ethylene bottom oil of full fraction is preheating to 150 DEG C -170 DEG C through normal pressure heat exchange；The utility model ethylene bottom oil mentions
The purpose of preceding preheating is to guarantee that ethylene bottom oil and furnace outlet set temperature have the lesser temperature difference, it is possible to reduce heating furnace is born
Lotus guarantees the operational safety of equipment.It is rapidly heated in heating furnace, to reduce the residence time in heating furnace, is conducive to keep away
Exempt from generation asphalitine to be precipitated too early and lead to coking phenomenon.
(2) Pipeline transport will be passed through to heating furnace after the ethylene bottom oil water filling after preheating in step (1), initially enters heating
The smoke pipeline of furnace exchanges heat, and then sequentially enters the convection section and radiant section of heating furnace, is rapidly heated to the outlet temperature of boiler tube
Degree is 440-470 DEG C；
The purpose filled the water in step (2) reduces ethylene bottom oil in heating furnace to improve the flow velocity of oil gas in boiler tube
Residence time, to avoid coking in pipe.
Heating furnace is radiation-convection oven with horizontal stringing type in step (2).The ethylene of the utility model
Tar stock first passes through the convection type of heating furnace, then immediately proceeds to the radiant type of heating furnace, and the ethylene bottom oil of full fraction is made to exist
Gasifying in the pipeline of heating furnace, it is ensured that the micel that ethylene bottom oil generates in heating furnace is smaller, is not easy to adhere to tube wall, from
And effectively avoid ethylene bottom oil coking in pipe.And extension coking technology in the prior art, it is pair for first passing through heating furnace
Streaming is picked out with relatively low temperature (300 DEG C) fractionating section fraction (light component), then frequent pressure fractionating tower bottom into heating furnace
Radiant type, with (500 DEG C) the progress pyrogenetic reactions of relatively high temperature.If the application is first proposed by path in the prior art
After a part of light component, heating furnace is entered back into, biggish molecular weight can be generated, tube wall is adhered to, thus coking.Therefore, full fraction
Ethylene bottom oil once pass through heating furnace convection type and radiant type heating, be one of main improvement of the utility model.
Heating furnace tube outlet temperature in step (2) is set in 440-470 DEG C, and ethylene bottom oil can be made complete in boiler tube
It will not be condensed at cracking, but substantially, therefore can also be to avoid generation tube coking, and ensure that material is sent into coking still
Temperature at 440-470 DEG C, so that material carries out condensation reaction in coking still.What the operation of step (2) needed to clearly state
It is that coil outlet temperature (440-470 DEG C) in technical solution provided by the utility model is less than common cognition in the prior art
Delayed coking reaction temperature (495-505 DEG C), overcome the prejudice of the prior art.
(3) ethylene bottom oil after step (2) being rapidly heated is sent into coking still, and condensation reaction occurs in coking still, raw
At high-temperature oil gas, high softening point bitumen and coke；In step (3), the temperature range of coking kettle top is 420 DEG C -450 DEG C, circulation
Than for 5%-8%
(4) high-temperature oil gas that step (3) generates is sent into atmospheric fractional tower distillation, is cut into gasoline fraction, diesel oil distillate, wax
Oil distillate etc.；
(5) high softening point bitumen and coke knot that step (3) generates gather in carrying out green coke in kettle；After green coke, with steaming
Vapour and water carry out the cold coke that cools down to the material in coking still；
(6) after the cold coke of step (5), cold coke is discharged out of kettle by machinery decoking, petroleum coke is made.
After green coke, coking still is small steam out enter together with by emptying tower cooling trough, knockout drum, gas into
Enter gas holder official website, oil recovery；
(7) coking still water supply, the oil gas vaporized in kettle, steam are cooling through emptying tower and cooling trough, and recycling separation evaporates
Part and device in Gas.
Wherein, ethylene bottom oil described in step (2) needs to inject water or high steam before entering smoke pipeline, injects water
Water is the 2% of ethylene bottom oil weight.
Wherein, the temperature of the high-temperature oil gas generated in step (3) is 440 DEG C -450 DEG C.
Further, the high-temperature oil gas generated in step (3) is cooled to 410 DEG C, flows out and is sent into from the kettle top of coking still
Scrubbing tower is washed；It is re-fed into atmospheric fractional tower distillation after washing and carries out step (4).
The fraction that the gasoline fraction is 210 DEG C of initial boiling point <.
The fraction that the diesel oil distillate is 200 DEG C -360 DEG C of initial boiling point.
The fraction that the wax oil fraction is 196 DEG C -370 DEG C of initial boiling point.
The heavy oil fraction is the fraction for initial boiling point > 370 DEG C.
A kind of production system of the full fraction ethylene bottom oil delayed coking of non-impurity-doped, the production system include feed system,
Flood pattern (can fill the water or inject high pressure steam, additional amount and the water injection rate equity of high pressure steam), heating furnace, coking still
And gas recovery system for oil, the heating furnace includes convection section and radiant section, and convection section is connected to radiant section, the convection section
Entrance is feed end, and the outlet of radiant section is discharge end, the feed end of the heating furnace respectively with feed system and steam injection system
Outlet line connection；The discharge end of the heating furnace and the inlet communication of coking still, the kettle top and oil gas of the coking still are returned
Receipts system is connected.
As the further improvement of above-described embodiment, the entrance of the convection section is at least one, and the convection section enters
The outlet number of mouth number and radiant section is equal to each other.The heating furnace of the utility model determines convection current according to the demand of material throughput
Section entrance number and radiant section outlet number, be ordinarily selected to it is single-entry single-out design, go with each other all the time design in addition four into four mouthfuls
Deng.
As the further improvement of above-described embodiment, the feed system includes raw material pump, the raw material pump and heat exchanger
After heat exchange, it is connected by pipeline with heating furnace.
As the further improvement of above-described embodiment, the feed system further includes relay pump, the raw material pump and heat exchange
After device heat exchange, it is connected by pipeline with relay pump, the relay pump is connected with by pipeline with heating furnace.Wherein, after preheating
Ethylene bottom oil relay pump is sent into heating furnace.Ethylene bottom oil after preheating is sent into heating furnace by relay pump, and the access of relay pump can drop
The low anti-pressure ability requirement to follow-up equipment, reduces production and cost of investment.
As the further improvement of above-described embodiment, the gas recovery system for oil includes atmospheric fractional tower, the coking still
Kettle top for vertical coking still, the vertical coking still is connected with atmospheric fractional tower.
As the further improvement of above-described embodiment, the gas recovery system for oil includes atmospheric fractional tower and scrubbing tower, institute
Stating coking still is horizontal coking still, and the kettle top of the horizontal coking still is connected with scrubbing tower, and scrubbing tower is connect with atmospheric fractional tower,
The scrubber overhead is connected with cooling trough.
The gas recovery system for oil includes atmospheric fractional tower and/or scrubbing tower, and the coking still is vertical coking still or crouches
Formula coking still.
As the further improvement of above-described embodiment, the gas recovery system for oil further includes emptying tower, the coking still
Another outlet of kettle top with emptying tower be connected, the emptying tower is connected with gas holder all the way, all the way with gs-oil separator side
Gas discharge mouth be connected；The atmospheric fractional tower is connected with the feed inlet of gs-oil separator.As above-described embodiment into one
Step is improved, and the coking still is vertical coking still or horizontal coking still.
As the further improvement of above-described embodiment, the furnace outlet is connected by four-way valve with vertical coking still.
As the further improvement of above-described embodiment, the heating furnace is connect by product distribution valve with horizontal coke drum,
The product distribution valve is provided with annular cavity, and the annular cavity is provided with an inlet valve and multiple outlet valves, the raw material
The outlet of the inlet valve connection heating furnace of distributing valve, the outlet valve of the product distribution valve connect the coke drum；The coke
Tower is horizontal reacting kettle, and the bottom end of the horizontal reacting kettle is provided with feed inlet, and the top of the horizontal reacting kettle connects washing
Tower.
The beneficial effects of the utility model are:
1, normal pressure and vacuum topping and direct coking full fraction ethylene bottom oil that need not be preliminary using the utility model technique,
Reduce pre-treating technology, and there can be very big economic value with the full fraction ethylene bottom oil delayed coking production of non-impurity-doped.
2, using the utility model technique, ethylene bottom oil is extracted out by raw material gs-oil separator, is preheated through normal pressure heat exchanger, in advance
Heat is to save energy consumption, and after the water filling with ethylene bottom oil processing capacity 2%, heated furnace flue tube heat exchange, ethylene bottom oil enters heating
Furnace；Water filling to increase feedstock oil in velocity in pipes, continuously across heating furnace convection section, radiant section be rapidly heated to 440 DEG C-
470 DEG C, the ethylene bottom oil after heating enters coking still, and the series reactions such as cracking condensation occur in coking still, realizes continuous
Property production.
3, using the utility model technique, the wax oil that is fractionated relative to wax tailings sulfur content is low, heavy metal contains
Measure low, following process hydrogenation catalyst is not easy to be poisoned, and extends catalyst service life, reduces the cost of catalyst change.
The petrol and diesel oil nitrogen content that fractionation obtains is low, sulfur content is low, is used for vapour bavin after not having desulfurization expense, following process to add hydrogen
The expense of oil modification is low, and environmentally friendly operating cost is low.
4, emptying tower is equipped in the delayed coking production system of the utility model, being vented in tower the methane gas collected can be with
It is further used for the heating of heating furnace, saves cost.
Detailed description of the invention
Fig. 1 is the full fraction ethylene bottom oil delayed coking production system schematic diagram of the first non-impurity-doped of the utility model；
Fig. 2 is the full fraction ethylene bottom oil delayed coking production system schematic diagram of second of non-impurity-doped of the utility model；
Fig. 3 is the full fraction ethylene bottom oil delayed coking production system schematic diagram of the third non-impurity-doped of the utility model；
Fig. 4 is the full fraction ethylene bottom oil delayed coking production system schematic diagram of the 4th kind of non-impurity-doped of the utility model.
Wherein, 1- feeding line, 2- heat exchange pipeline, P1- raw material pump, P2- heat exchange pump, 3- water filling or gas injection pipeline, F- add
Hot stove, 4- heated material feed-line, C3- coking still, 5- high-temperature oil gas feed-line, C1- scrubbing tower, 6- wash oil-gas transportation
Pipeline, 7- wash oil transfer pipeline, and 8-, which is washed, devokes pipeline, the small feed-line that steams out of 9- coking still, C4- emptying tower, and 10- watts
This letter shoot line, 11- oil gas collection pipeline, 12- emptying tower discharging pipeline, D1- gs-oil separator, 13- gasoline discharge pipe,
C2- atmospheric fractional tower, 14- atmospheric fractional tower gasoline gathering line, 15- atmospheric fractional tower diesel oil gathering line, the fractionation of 16- normal pressure
Tower wax oil gathering line, 17- wash heavy oil gathering line, 18- tail gas blow-down pipe, 19- coke gathering line, 20- sulfur-bearing dirt
Water discharge pipe line.
Specific embodiment
Test material:
Ethylene bottom oil outsourcing source has: the ground such as middle sand, Yan Hua, Panjin, Lanzhou, Xinjiang, if not explaining with middle sand as follows
Ethylene bottom oil is to process raw material.
Middle sand ethylene bottom oil specific gravity: 1.04-1.07, Han Shui≤1%.
Below by way of the drawings and specific embodiments, the utility model is described in further detail.
Embodiment 1
The full fraction ethylene bottom oil delayed coking production system of doping as shown in Figure 2 implements the delay coke chemical industry of ethylene bottom oil
Skill, it is specific as follows, after ethylene bottom oil preheats 160 degree, into heating furnace, filled the water with 2% water injection rate of feed ethylene tar, warp
Convection section, the radiant section of heating furnace are rapidly heated to 460 DEG C；Ethylene bottom oil after heating enters coking still, the circulation of coking still
Than being 5%, the series reactions such as cracking condensation occur in coking still, generate rich gas, solvent naphtha, high softening point bitumen and coke
Charcoal, high softening point bitumen and coke knot gather in kettle.In kettle 440 DEG C of oil gas temperature after quench oil is cooled to 410 DEG C from coking
The outflow of kettle kettle top enters oil gas and enters atmospheric fractional tower distillation, and the liquid phase of initial boiling point > 370 DEG C washs heavy oil fraction carrying device,
The quality test results for being cut into 210 DEG C of initial boiling point < of gasoline fraction are shown in Table the diesel oil distillate of 1A, 172 DEG C -352 DEG C of initial boiling point
Quality test results be shown in Table 1B, the quality test results of 196 DEG C -450 DEG C of initial boiling point of wax oil fraction are shown in Table 1C.
The quality test results of table 1A gasoline fraction
The quality test results of table 1B diesel oil distillate
The quality test results of table 1C wax oil fraction
Product yield: petroleum coke -23%, washing heavy oil -3%, wax oil -13%, bavin gasoline -59%, gas -2%.
Petroleum coke fugitive constituent: 11%
Embodiment 2
As shown in fig. 2, ethylene bottom oil is extracted out by raw material gs-oil separator, is preheating to 150 DEG C through normal pressure heat exchanger, is used relay
Ethylene bottom oil after preheating is sent into heating furnace by pump, is filled the water with 2% water injection rate of feed ethylene tar, is passed through the cigarette of heating furnace
Pipeline is logical to exchange heat, and then enters convection section, radiant section, is rapidly heated to 450 DEG C；Ethylene bottom oil after heating is through four-way valve
Into coking still, cracking condensation reaction occurs in coking still, the recycle ratio of coking still is 8%, generates rich gas, high softening-point drip
Green and coke, high softening point bitumen and coke knot gather in kettle.In kettle 450 DEG C of oil gas temperature after quench oil is cooled to 410 DEG C
After from the outflow of coking still kettle top into scrubbing tower washing, the liquid phase of initial boiling point > 370 DEG C washs heavy oil fraction carrying device, washing
Oil gas enters atmospheric fractional tower distillation, and the quality test results for being cut into 215 DEG C of initial boiling point < of gasoline fraction are shown in Table 2A, fore-running
The quality test results of the diesel oil distillate of 175 DEG C -361 DEG C of point are shown in Table the quality of 2B, 196 DEG C -455 DEG C of initial boiling point of wax oil fraction
Inspection result is shown in Table 2C.After coking still green coke, cooled down with steam and water to the material in coking still, coking still is small to be blown
Vapour green coke kettle oil gas enters atmospheric fractional tower together, enters tail gas blowdown system, waste oil recovery and gas when to water cooling coke.
The quality test results of table 2A gasoline fraction
The quality test results of table 2B diesel oil distillate
The quality test results of table 2C wax oil fraction
Petroleum coke -22%, washing heavy oil -4%, wax oil -14%, bavin gasoline -58%, gas -2%.
Petroleum coke fugitive constituent: 14%
Embodiment 3
As shown in Fig. 2, ethylene bottom oil is extracted out by raw material gs-oil separator, 170 DEG C are preheating to through normal pressure heat exchanger, uses relay
Ethylene bottom oil after preheating is sent into heating furnace by pump, is filled the water with 2% water injection rate of feed ethylene tar, is passed through the cigarette of heating furnace
Pipeline is logical to exchange heat, and then enters convection section, radiant section, is rapidly heated to 470 DEG C；Ethylene bottom oil after heating is through four-way valve
Into coking still, the recycle ratio of coking still is 7%, and cracking condensation reaction occurs in coking still, generates rich gas, high softening-point drip
Green and coke, high softening point bitumen and coke knot gather in kettle.In kettle 445 DEG C of oil gas temperature after quench oil is cooled to 410 DEG C
Enter scrubbing tower from the outflow of coking still kettle top；After washing, the liquid phase of initial boiling point > 470 DEG C washs heavy oil fraction carrying device, oil gas
It is distilled into atmospheric fractional tower, the quality test results for being cut into -210 DEG C of initial boiling point of gasoline fraction are shown in Table 3A, initial boiling point 200
The quality test results of DEG C -360 DEG C of diesel oil distillate are shown in Table the quality inspection of 2B, 196 DEG C -470 DEG C of initial boiling point of wax oil fraction
It the results are shown in Table 2C.The gasoline being cut into enters gs-oil separator by atmospheric fractional tower jacking, the uncolled methane gas component got off,
Enter the low pressure gas pipe network system being made of gas holder through oil gas tank gas export.After coking still green coke, steam is used
And water cools down to the material in coking still, coking still is small to steam out together with the oil gas by scrubbing tower washing into normal pressure point
Tower is evaporated, enters tail gas blowdown system when to water cooling coke；Coking still water supply, the steam vaporized in kettle is through emptying tower and cooling trough
Cooling, recovery section sump oil after gas component enters the low pressure gas pipe network system being made of gas holder.
The quality test results of table 3A gasoline fraction
The quality test results of table 3B diesel oil distillate
The quality test results of table 3C wax oil fraction
Petroleum coke -23%, washing heavy oil -3%, wax oil -12%, bavin gasoline -58.5%, gas -3.5%.
Petroleum coke fugitive constituent: 8%
Embodiment 4
As shown in Fig. 2, ethylene bottom oil is extracted out by raw material gs-oil separator, 160 DEG C are preheating to through normal pressure heat exchanger, uses relay
Ethylene bottom oil after preheating is sent into heating furnace by pump, is filled the water with 2% water injection rate of feed ethylene tar, is passed through the cigarette of heating furnace
Deferent exchanges heat, and then enters convection section, radiant section, is rapidly heated to 440 DEG C；Ethylene bottom oil after heating through four-way valve into
Enter coking still, the recycle ratio of coking still is 6%, and cracking condensation reaction occurs in coking still, generates rich gas, high softening point bitumen
And coke, high softening point bitumen and coke knot gather in kettle.In kettle 430 DEG C of oil gas temperature after quench oil is cooled to 410 DEG C from
The outflow of coking still kettle top enters scrubbing tower；After washing, the liquid phases of initial boiling point > 370 DEG C washs heavy oil fraction carrying device, oil gas into
Enter atmospheric fractional tower distillation, the quality test results for being cut into 215 DEG C of initial boiling point < of gasoline fraction are shown in Table 4A, initial boiling point 200
The quality test results of DEG C -360 DEG C of diesel oil distillate are shown in Table the quality inspection of 4B, 196 DEG C -470 DEG C of initial boiling point of wax oil fraction
It the results are shown in Table 4C.The gasoline being cut into enters gs-oil separator by atmospheric fractional tower jacking, the uncolled methane gas component got off,
Enter the low pressure gas pipe network system being made of gas holder through oil gas tank gas export.After coking still green coke, steam is used
And water cools down to the material in coking still, coking still is small to steam out together with the oil gas by scrubbing tower washing into normal pressure point
Tower is evaporated, enters tail gas blowdown system when to water cooling coke；Coking still water supply, the steam vaporized in kettle is through emptying tower and cooling trough
Cooling, recovery section sump oil after gas component enters the low pressure gas pipe network system being made of gas holder.
The quality test results of table 4A gasoline fraction
The quality test results of table 4B diesel oil distillate
The quality test results of table 4C wax oil fraction
Petroleum coke -24%, washing heavy oil -3%, wax oil -14%, bavin gasoline -57.2%, gas -1.8%.
Petroleum coke fugitive constituent: 18%
Embodiment 5
As shown in Figure 1, ethylene bottom oil is extracted out by raw material gs-oil separator, 155 DEG C are preheating to through normal pressure heat exchanger, uses relay
Ethylene bottom oil after preheating is sent into heating furnace by pump, is filled the water with 2% water injection rate of feed ethylene tar, is passed through the cigarette of heating furnace
Pipeline is logical to exchange heat, and then enters convection section, radiant section, is rapidly heated to 465 DEG C；Ethylene bottom oil after heating is through four-way valve
Into coking still, the recycle ratio of coking still is 7%, and cracking condensation reaction occurs in coking still, generates rich gas, solvent naphtha, height
Softening point asphalt and coke, high softening point bitumen and coke knot gather in kettle.It is cooled to through quench oil for 446 DEG C of oil gas temperature in kettle
Enter scrubbing tower from the outflow of coking still kettle top after 410 DEG C；After washing, the liquid phase washing heavy oil fraction of initial boiling point > 470 DEG C sends out dress
Set, oil gas enter atmospheric fractional tower distillation, be cut into 214 DEG C of initial boiling point < of gasoline fraction quality test results be shown in Table 6A,
The quality test results for the diesel oil distillate that 173 DEG C -358 DEG C of initial boiling point are shown in Table 6B, 196 DEG C -470 DEG C of initial boiling point of wax oil fraction
Quality test results are shown in Table 6C.The gasoline being cut into enters gs-oil separator, the uncolled gas to get off by atmospheric fractional tower jacking
Gas component enters the low pressure gas pipe network system being made of gas holder through oil gas tank gas export.Coking still green coke terminates
Afterwards, cooled down with steam and water to the material in coking still, coking still is small to steam out together with the oil gas by scrubbing tower washing
Into atmospheric fractional tower；Coking still water supply, the steam vaporized in kettle is cooling through emptying tower and cooling trough, recovery section sump oil
After gas component enters the low pressure gas pipe network system being made of gas holder.
The quality test results of table 6A gasoline fraction
The quality test results of table 6B diesel oil distillate
The quality test results of table 6C wax oil fraction
Product yield: petroleum coke -23%, washing heavy oil -3%, wax oil -13%, bavin gasoline -58.5%, gas -
2.5%.
Petroleum coke fugitive constituent: 10%
Example 1
Ethylene bottom oil is extracted out by raw material gs-oil separator, is preheating to 150 DEG C through normal pressure heat exchanger, after being preheated with relay pump
Ethylene bottom oil be sent into heating furnace, filled the water with 2% water injection rate of feed ethylene tar, the annular smoke flue for passing through heating furnace carries out
Heat exchange, and then enter convection section, radiant section, it is rapidly heated to 435 DEG C；Ethylene bottom oil after heating enters coking through four-way valve
Kettle.
When heating furnace tube outlet temperature controls 430 ± 5 DEG C, coking kettle top temperature is lower than 420 DEG C, the recycle ratio of coking still
It is 5%, pitch coke occurs in coke fugitive constituent > 20%, and coke product is unqualified；Total liquid yield reduces more, unqualified coking yield
Higher, device lost revenue is larger.
Comparative example 2
Ethylene bottom oil is extracted out by raw material gs-oil separator, is preheating to 150 DEG C through normal pressure heat exchanger, after being preheated with relay pump
Ethylene bottom oil be sent into heating furnace, filled the water with 2% water injection rate of feed ethylene tar, the annular smoke flue for passing through heating furnace carries out
Heat exchange, and then enter convection section, radiant section, it is rapidly heated to 490 DEG C；Ethylene bottom oil after heating enters coking through four-way valve
Kettle.
When heating furnace tube outlet temperature controls 490 ± 5 DEG C, stokehold pressure is up to 2.0MPa, and stokehold pipeline leaks,
Safety in production is not can guarantee；Heating furnace thermic load is excessive, and Tube surface heat strength superelevation leads to the coking of boiler tube short time, can not
Guarantee safety and consecutive production.
Embodiment 6
As shown in Figure 1, being the production system of the full fraction ethylene bottom oil delayed coking of the utility model non-impurity-doped, production system
Including feed system, flood pattern, heating furnace, coking still F and gas recovery system for oil, heating furnace includes convection section and radiant section,
And convection section is connected to radiant section, the feed end of the heating furnace outlet with the outlet line of feed system and steam injection system respectively
Line 3 is connected；The outlet of heating furnace is connected by heated material feed-line 4 with the import of coking still F, the kettle top and oil of coking still
Gas recovery system is connected.
Feed system includes raw material pump P1, heat exchanger and relay pump P2, raw material pump P1 fed by feed pipe 1 after with change
After hot device heat exchange, it is connected by heat exchange pipeline 2 with relay pump, relay pump is connected with by pipeline with heating furnace F.
Gas recovery system for oil includes scrubbing tower C1 and atmospheric fractional tower C2, and the kettle top of coking still C3 is connected with scrubbing tower C1,
Scrubbing tower C1 is connect with atmospheric fractional tower C2, and scrubber overhead C1 is connected with cooling trough.Coking still can be vertical or Horizontal counter
Answer kettle.Coking still is provided with shovel Jiao Kou, recycles petroleum coke by pipeline 19, and the top of coking still is high-temperature oil gas feed-line 5, will
High-temperature oil gas is transported in scrubbing tower C1, and the lower part scrubbing tower C1 is by passing through the washing recycling washing weight of heavy oil gathering line 17 after washing
Oil, the oil gas on the top scrubbing tower C1 is delivered to atmospheric fractional tower C2 by washing oil gas pipeline 6, atmospheric fractional tower C2's
Gasoline is recycled by gasoline gathering line 14 in top, recycles diesel oil by diesel oil gathering line 15, passes through wax oil gathering line 16
Recycle wax oil.
Embodiment 7
As the further improvement of above-described embodiment, as shown in Fig. 2, the full fraction ethylene bottom oil of the utility model non-impurity-doped prolongs
In the production system of slow coking, compared to Figure 1, gas recovery system for oil further includes emptying tower C4, the coking of the kettle top of coking still C3
The small feed-line 9 that steams out of kettle is connected with emptying tower C4, and the bottom of emptying tower C4 is equipped with tail gas blow-down pipe 18.It is vented mono- tunnel tower C1
It is connected with gas holder WQG, is connected all the way with the gas discharge mouth of gs-oil separator side, specifically: C2 atmospheric fractional tower
Gasoline gathering line 14 enters gasoline into gs-oil separator D1 through liquid phase drawer, and gs-oil separator lower part will be more than liquid level
Gasoline is collected by the discharge of gasoline discharge pipe 13, packing, and another outlet of gs-oil separator lower part is discharged by sour water
Sour water is discharged in pipeline 20, and discharge port of the gas through top of gs-oil separator D1 separation is entered by oil gas collection pipeline 11
Gas holder collects the light gas of methane gas and gs-oil separator separation, increases the rate of recovery of material, and the material of recycling is logical
Device in Gas feed-line 10 is crossed for heating stove heating, saves production cost.
Coking still C3 is horizontal coking still, and heating furnace is connect by product distribution valve with horizontal coke drum, product distribution valve
It is provided with annular cavity, annular cavity is provided with an inlet valve and multiple outlet valves, and the inlet valve of product distribution valve connects heating
The outlet valve of the outlet of furnace, product distribution valve connects coke drum；Coke drum is horizontal reacting kettle, and the bottom end of horizontal reacting kettle is arranged
There is feed inlet, the side of horizontal reacting kettle is provided with shovel Jiao Kou；The top of horizontal reacting kettle is connected with scrubbing tower.Horizontal reacting kettle needs
It is connected with scrubbing tower, and vertical reaction kettle is not required to be connected with scrubbing tower, this is because horizontal reacting kettle need to be easy to produce a large amount of glue
Powder needs to wash cleaning.
The specific structure of horizontal coking still can refer to the patent notes data application No. is 2013100317708.
Embodiment 8
As shown in Figure 3.It is the production system of the full fraction ethylene bottom oil delayed coking of the utility model non-impurity-doped.With Fig. 1 phase
Than difference is that reaction kettle is vertical response kettle C3, and furnace outlet is connected by four-way valve with vertical coking still.Vertical coking
The top of kettle is directly connected with atmospheric fractional tower, carries out material fractionation.
Embodiment 9
As shown in figure 4, in the production system of the full fraction ethylene bottom oil delayed coking of the utility model non-impurity-doped, with Fig. 2's
Difference is: coking still C3 is vertical coking still, and furnace outlet is connected by four-way valve with vertical coking still.Vertical coking still
Top be directly connected with atmospheric fractional tower, carry out material fractionation.
The structure of heating furnace in embodiment 6-8 belongs to radiation-convection current in the prior art with horizontal stringing type
Formula heating furnace, but the outlet of convection type heating tube is connected with the outlet of radiant section charge pipe.
Substantially using the processing step in embodiment 6-8 when production system progress ethylene bottom oil delayed coking are as follows:
(1) ethylene bottom oil is preheating to 150 DEG C -170 DEG C through normal pressure heat exchanger；It (2) will be through preheating in step (1) with relay pump
Ethylene bottom oil afterwards is sent into heating furnace, and smoke-intake pipe is filled the water before road, exchanged heat by heating furnace smoke pipeline, and then enters convection section, spoke
Section is penetrated, is rapidly heated to 440-470 DEG C；(3) ethylene bottom oil after heating up enters coking still, and cracking condensation occurs in coking still
Reaction generates rich gas, high softening point bitumen and coke；The oil gas of high temperature enters atmospheric fractional tower from the outflow of coking still kettle top and cuts
Gasoline fraction, diesel oil distillate, wax oil fraction out.After coking still green coke, the material in coking still is carried out with steam and water
Cooling, small steam out of coking still enter atmospheric fractional tower together with the oil gas by scrubbing tower washing；Coking still water supply, the vapour in kettle
The steam of change is cooling through emptying tower and cooling trough, recycling separation fraction and device in Gas.
Wherein, embodiment 6, embodiment 8 have lacked device in Gas recycling and gasoline gathering line relative to embodiment 7 or 9, but
Entire technique framework is relatively easy.
Obviously, above-described embodiment is only intended to clearly illustrate example, and does not limit the embodiments.For
For those of ordinary skill in the art, other various forms of variations or change can also be made on the basis of the above description
It is dynamic.There is no necessity and possibility to exhaust all the enbodiments.And obvious variation extended from this or change
Among the dynamic protection scope created still in the utility model.
Claims (10)
1. a kind of full fraction ethylene bottom oil delayed coking production system of non-impurity-doped, which is characterized in that including feed system, water filling system
System, heating furnace, coking still and gas recovery system for oil, the heating furnace include convection section and radiant section, and convection section and radiant section
Connection, the entrance of the convection section are feed end, and the outlet of radiant section is discharge end, the feed end of the heating furnace respectively with into
Material system is connected to the outlet line of steam injection system；The discharge end of the heating furnace and the inlet communication of coking still, the coking
The kettle top of kettle is connected with gas recovery system for oil.
2. the full fraction ethylene bottom oil delayed coking production system of non-impurity-doped according to claim 1, which is characterized in that described
The entrance of convection section is at least one, and the entrance number of the convection section and the outlet number of radiant section are equal to each other.
3. the full fraction ethylene bottom oil delayed coking production system of non-impurity-doped according to claim 1, which is characterized in that described
Feed system includes raw material pump, and the raw material pump is connected by pipeline with heating furnace with after heat exchanger heat exchange.
4. the full fraction ethylene bottom oil delayed coking production system of non-impurity-doped according to claim 3, which is characterized in that described
Feed system further includes relay pump, and the raw material pump is connected by pipeline with relay pump with after heat exchanger heat exchange, the relay pump
It is connected with by pipeline with heating furnace.
5. the full fraction ethylene bottom oil delayed coking production system of non-impurity-doped according to claim 1, which is characterized in that described
Gas recovery system for oil includes atmospheric fractional tower, and the coking still is vertical coking still, the kettle top and normal pressure of the vertical coking still
Fractionating column is connected.
6. the full fraction ethylene bottom oil delayed coking production system of non-impurity-doped according to claim 1, which is characterized in that described
Gas recovery system for oil includes atmospheric fractional tower and scrubbing tower, and the coking still is horizontal coking still, the kettle of the horizontal coking still
Top is connected with scrubbing tower, and scrubbing tower is connect with atmospheric fractional tower, and the scrubber overhead is connected with cooling trough.
7. the full fraction ethylene bottom oil delayed coking production system of non-impurity-doped according to claim 5 or 6, which is characterized in that
The gas recovery system for oil further includes emptying tower, and another outlet of the kettle top of the coking still is connected with emptying tower, the emptying
Tower is connected with gas holder all the way, is connected all the way with the gas discharge mouth of gs-oil separator side；The atmospheric fractional tower and oil
The feed inlet of gas separating device is connected.
8. the full fraction ethylene bottom oil delayed coking production system of non-impurity-doped according to claim 5, which is characterized in that described
Furnace outlet is connected by four-way valve with vertical coking still.
9. the full fraction ethylene bottom oil delayed coking production system of non-impurity-doped according to claim 6, which is characterized in that described
Heating furnace is connect by product distribution valve with coke drum, and the product distribution valve is provided with annular cavity, and the annular cavity is opened
There are an inlet valve and multiple outlet valves, the outlet of the inlet valve connection heating furnace of the product distribution valve, the product distribution
The outlet valve of valve connects the coke drum；The coke drum be horizontal reacting kettle, the bottom end of the horizontal reacting kettle be provided with into
The top of material mouth, the horizontal reacting kettle connects scrubbing tower.
10. the full fraction ethylene bottom oil delayed coking production system of non-impurity-doped according to claim 1, which is characterized in that institute
The number for stating the entrance of convection section is two.
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| CN1142259C (en) * | 2000-09-25 | 2004-03-17 | 中国石油化工股份有限公司 | Combined process of initial solvent asphalt elimination and delayed coking |
| CN102344825B (en) * | 2010-07-30 | 2014-02-26 | 中国石油化工集团公司 | Continuous delay coking device and method |
| US9023193B2 (en) * | 2011-05-23 | 2015-05-05 | Saudi Arabian Oil Company | Process for delayed coking of whole crude oil |
| CN102295943B (en) * | 2011-08-12 | 2013-06-26 | 中石油东北炼化工程有限公司葫芦岛设计院 | Method for coking needle coke by large recycle ratio oil system |
| 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 |
| CN105733648B (en) * | 2014-12-08 | 2017-12-05 | 中国石油天然气股份有限公司 | A kind of Delayed coking high temperature oil-gas line anti-coking method |
| CN105733649B (en) * | 2014-12-08 | 2017-12-05 | 中国石油天然气股份有限公司 | A kind of Delayed coking high temperature oil-gas line anti-coking method |
| CN105985803B (en) * | 2015-02-10 | 2017-11-24 | 中国石油化工股份有限公司 | A kind of method for preparing needle-shape coke raw material |
| CN206940795U (en) * | 2017-04-26 | 2018-01-30 | 杭州绿环橡塑制品有限公司 | A kind of cracker for being used to prepare water tar |
| CN109652121A (en) * | 2018-10-11 | 2019-04-19 | 天津市东盛工贸有限公司 | The full fraction ethylene bottom oil delayed coking equipment of non-impurity-doped |
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