CN109609182A - The technique of the full fraction ethylene bottom oil delayed coking of non-impurity-doped - Google Patents
The technique of the full fraction ethylene bottom oil delayed coking of non-impurity-doped Download PDFInfo
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- CN109609182A CN109609182A CN201811359440.0A CN201811359440A CN109609182A CN 109609182 A CN109609182 A CN 109609182A CN 201811359440 A CN201811359440 A CN 201811359440A CN 109609182 A CN109609182 A CN 109609182A
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- 238000004939 coking Methods 0.000 title claims abstract description 189
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 title claims abstract description 128
- 239000005977 Ethylene Substances 0.000 title claims abstract description 128
- 230000003111 delayed effect Effects 0.000 title claims abstract description 53
- 238000000034 method Methods 0.000 title claims abstract description 40
- 238000010438 heat treatment Methods 0.000 claims abstract description 88
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 44
- 238000006243 chemical reaction Methods 0.000 claims abstract description 21
- 239000002994 raw material Substances 0.000 claims description 38
- 238000005201 scrubbing Methods 0.000 claims description 26
- 238000011084 recovery Methods 0.000 claims description 20
- 239000000463 material Substances 0.000 claims description 19
- 238000001816 cooling Methods 0.000 claims description 18
- 238000005336 cracking Methods 0.000 claims description 14
- 238000004821 distillation Methods 0.000 claims description 8
- 238000006482 condensation reaction Methods 0.000 claims description 7
- 238000011049 filling Methods 0.000 claims description 6
- 238000000926 separation method Methods 0.000 claims description 6
- 239000003208 petroleum Substances 0.000 claims description 5
- 238000010793 Steam injection (oil industry) Methods 0.000 claims description 3
- 238000004891 communication Methods 0.000 claims description 2
- 238000004519 manufacturing process Methods 0.000 abstract description 16
- 239000002006 petroleum coke Substances 0.000 abstract description 15
- 230000008569 process Effects 0.000 abstract description 14
- 238000012545 processing Methods 0.000 abstract description 12
- 239000003054 catalyst Substances 0.000 abstract description 6
- 239000003921 oil Substances 0.000 description 200
- 239000007789 gas Substances 0.000 description 99
- 239000000571 coke Substances 0.000 description 44
- 239000003502 gasoline Substances 0.000 description 34
- 238000012360 testing method Methods 0.000 description 31
- 238000009835 boiling Methods 0.000 description 24
- 238000005406 washing Methods 0.000 description 24
- 239000002283 diesel fuel Substances 0.000 description 18
- 239000000295 fuel oil Substances 0.000 description 18
- 239000010426 asphalt Substances 0.000 description 11
- 239000002010 green coke Substances 0.000 description 11
- 230000006872 improvement Effects 0.000 description 11
- 239000000047 product Substances 0.000 description 11
- 238000005516 engineering process Methods 0.000 description 10
- 230000008859 change Effects 0.000 description 9
- 238000002347 injection Methods 0.000 description 9
- 239000007924 injection Substances 0.000 description 9
- 239000000779 smoke Substances 0.000 description 9
- 239000000470 constituent Substances 0.000 description 8
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 8
- 230000006837 decompression Effects 0.000 description 7
- 238000009826 distribution Methods 0.000 description 7
- 238000002156 mixing Methods 0.000 description 7
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 6
- 239000007791 liquid phase Substances 0.000 description 6
- 238000004064 recycling Methods 0.000 description 6
- 239000000126 substance Substances 0.000 description 6
- 238000005194 fractionation Methods 0.000 description 5
- 238000010791 quenching Methods 0.000 description 5
- 238000007670 refining Methods 0.000 description 5
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 4
- 150000001336 alkenes Chemical class 0.000 description 4
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 4
- 238000010586 diagram Methods 0.000 description 4
- 239000000203 mixture Substances 0.000 description 4
- 239000012071 phase Substances 0.000 description 4
- 238000011160 research Methods 0.000 description 4
- 239000006227 byproduct Substances 0.000 description 3
- 238000009833 condensation Methods 0.000 description 3
- 230000005494 condensation Effects 0.000 description 3
- 150000002391 heterocyclic compounds Chemical class 0.000 description 3
- 239000007788 liquid Substances 0.000 description 3
- 239000011331 needle coke Substances 0.000 description 3
- 229910052757 nitrogen Inorganic materials 0.000 description 3
- 238000005504 petroleum refining Methods 0.000 description 3
- 238000000197 pyrolysis Methods 0.000 description 3
- 239000004576 sand Substances 0.000 description 3
- 239000002904 solvent Substances 0.000 description 3
- 101100447665 Mus musculus Gas2 gene Proteins 0.000 description 2
- 239000005864 Sulphur Substances 0.000 description 2
- 150000001335 aliphatic alkanes Chemical group 0.000 description 2
- 238000003763 carbonization Methods 0.000 description 2
- 238000005235 decoking Methods 0.000 description 2
- 230000007423 decrease Effects 0.000 description 2
- 238000013461 design Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000000446 fuel Substances 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 239000002184 metal Substances 0.000 description 2
- 238000012827 research and development Methods 0.000 description 2
- 239000000243 solution Substances 0.000 description 2
- 229910052717 sulfur Inorganic materials 0.000 description 2
- 239000011593 sulfur Substances 0.000 description 2
- PZZOEXPDTYIBPI-UHFFFAOYSA-N 2-[[2-(4-hydroxyphenyl)ethylamino]methyl]-3,4-dihydro-2H-naphthalen-1-one Chemical group C1=CC(O)=CC=C1CCNCC1C(=O)C2=CC=CC=C2CC1 PZZOEXPDTYIBPI-UHFFFAOYSA-N 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 150000001345 alkine derivatives Chemical class 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000004523 catalytic cracking Methods 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 238000005345 coagulation Methods 0.000 description 1
- 230000015271 coagulation Effects 0.000 description 1
- 230000019771 cognition Effects 0.000 description 1
- 238000001246 colloidal dispersion Methods 0.000 description 1
- 239000000084 colloidal system Substances 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 239000010779 crude oil Substances 0.000 description 1
- 238000005520 cutting process Methods 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- -1 diesel yield rise Substances 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 239000010771 distillate fuel oil Substances 0.000 description 1
- 235000013399 edible fruits Nutrition 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 239000004519 grease Substances 0.000 description 1
- JEGUKCSWCFPDGT-UHFFFAOYSA-N h2o hydrate Chemical compound O.O JEGUKCSWCFPDGT-UHFFFAOYSA-N 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 238000005984 hydrogenation reaction Methods 0.000 description 1
- 230000008676 import Effects 0.000 description 1
- 238000007689 inspection Methods 0.000 description 1
- 239000012263 liquid product Substances 0.000 description 1
- 230000007246 mechanism Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 238000012946 outsourcing Methods 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 238000012856 packing Methods 0.000 description 1
- 239000006253 pitch coke Substances 0.000 description 1
- 238000006068 polycondensation reaction Methods 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 238000002203 pretreatment Methods 0.000 description 1
- 238000003672 processing method Methods 0.000 description 1
- 230000004044 response Effects 0.000 description 1
- 238000010025 steaming Methods 0.000 description 1
- 238000004227 thermal cracking Methods 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
- 229930195735 unsaturated hydrocarbon Natural products 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
- 239000011800 void material Substances 0.000 description 1
- 239000001993 wax Substances 0.000 description 1
Classifications
-
- 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
-
- 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
-
- 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
-
- 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
-
- 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
Abstract
The invention discloses a kind of technique of the full fraction ethylene bottom oil delayed coking of non-impurity-doped, technique is to enter heating furnace after the ethylene bottom oil after preheating fills the water to heat, and heating furnace tube outlet temperature is 440-470 DEG C；After ethylene bottom oil after heating enters coking still reaction, distills and separate into atmospheric fractional tower, obtain light fraction and petroleum coke and tail oil.The purpose of the present invention is to provide a kind of steps simply, is directed to technique of the full fraction ethylene bottom oil for carrying out delayed coking without catalyst, without preposition processing, without doping, 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, production efficiency is improved.
Description
Technical field
The invention belongs to petroleum refining technology field more particularly to a kind of full fraction ethylene bottom oil delayed cokings of non-impurity-doped
Technique.
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.Currently, ethylene bottom oil
It 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 easily produces
Raw coking and black smoke, pollute environment.To sum up, using ethylene bottom oil as the research and development of the production technology of raw material, there is weight
Want meaning.
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, " refining second is mixed in Responds Surface Methodology optimization
The delayed coking of alkene pyrolysis fuel oil is studied " (see " petroleum refining and chemical industry " the 8th phase P5-P8 in 2009, " delayed coking unit is mixed
Refine the research of grand celebration pyrolysis fuel oil " (see " petroleum refining and chemical industry " the 12nd phase P20-P22 in 2007), " blending ethylene cracking weight
Influence of the oil to delayed coking " (see " petrochemical technology and application " the 1st phase P44-P49 in 2010) and " decompression residuum blending ethylene
The test of tar heavy oil co carbonization " (see " Maoming College's journal " the 1st phase P7-P9 in 2008 etc., these researchs are by ethylene bottom oil
Full fraction and decompression residuum mix refining as delayed coking raw material, can make the yield of liquid yield and light Fuel oil product in this way
It is lower, 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
Gasoline and coker gas oil are mixed with ethylene bottom oil light fraction, obtain mixed raw material, then carry out hydrofining reaction.The technical side
Case is carried out not directed to the ethylene bottom oil of full fraction, 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,
It is heated to react required 500-505 DEG C of temperature, subsequently into coke drum, the heat in coke drum by itself bringing into is carried out
The reactions such as cracking condensation "；
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) progress pyrogenetic reactions.
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
Using thin oil decompression residuum as raw material, Furnace Tube of Coker Unit outlet temperature is 502 DEG C.Stronger raw material is inclined to for coking, it can
Using relatively low heater outlet temperature, temperature is excessively high, and pyrogenetic reaction depth is excessive, and the coke of generation is harder, and boiler tube is easily tied
It is burnt.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
The research and development of needle coke production technology since the end of the seventies, and with thermal cracking residue and catalytic cracking clarified oil be
Raw material has produced qualified needle coke product on commercial plant.And it is produced in needle coke by raw material of ethylene bottom oil
In type experimental study, 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.
Summary of the invention
One of the technical issues of the present invention is directed to solve above-mentioned ethylene bottom oil deep processing to a certain extent in the related technology.Cause
This, that the purpose of the present invention is to provide a kind of steps is simple, without catalyst, without preposition processing, without doping for complete
The technique that fraction ethylene bottom oil is used to carry out delayed coking.
To achieve the goals above, the technical solution adopted by the present invention is that:
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
The unsaturated hydrocarbons such as alkene, alkynes and heterocyclic compound content are higher in tar, and chemical property is active, and oxidation stability is poor, easily
Occur from polycondensation, secondary new gum asphalt etc.；In heat exchange temperature-rise period, since solvent effect and fuel factor are inevitable
It will change, therefore metastable colloidal dispersion just loses stability, primary and secondary pitch to ethylene bottom oil originally
Matter is understood coagulation and is attached on tube wall and wall not with stream flow, and asphalitine grease is formed, and asphalitine is further condensed life
It is burnt.
The technique of the full fraction ethylene bottom oil delayed coking of non-impurity-doped of the invention in view of the above-mentioned problems, done many improvement,
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；Ethylene bottom oil of the present invention is pre- in advance
The purpose of heat is to guarantee that ethylene bottom oil and furnace outlet set temperature have the lesser temperature difference, it is possible to reduce the load of heating furnace,
Guarantee the operational safety of equipment.It is rapidly heated in heating furnace, to reduce the residence time in heating furnace, is conducive to avoid
Asphalitine occurs 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).Ethylene bottom oil of the invention
Raw material first passes through the convection type of heating furnace, then immediately proceeds to the radiant type of heating furnace, is heating the ethylene bottom oil of full fraction
Gasifying in the pipeline of 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, thus
Effectively avoid ethylene bottom oil coking in pipe.And extension coking technology in the prior art, it is the convection current for first passing through heating furnace
Formula 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 invention.
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
The temperature of kettle is at 440-470 DEG C, so that material carries out condensation reaction in coking still.The operation needs of step (2) clearly state
Be that coil outlet temperature (440-470 DEG C) in technical solution provided by the invention 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 equipment of the full fraction ethylene bottom oil delayed coking of non-impurity-doped, the equipment includes 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 oil gas
Recovery system, the heating furnace includes convection section and radiant section, and convection section is connected to radiant section, the entrance of the convection section
For feed end, the outlet end 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 petroleum vapor recovery of the coking still
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.Heating furnace of the invention determines convection section according to the demand of material throughput
The outlet number of entrance number and radiant section, 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 etc..
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 and atmospheric fractional tower connect
It connects, 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 present invention are:
1, normal pressure and vacuum topping and direct coking full fraction ethylene bottom oil that need not be preliminary using present invention process, be reduced
Pre-treating technology, and can have very big economic value with the full fraction ethylene bottom oil delayed coking production of non-impurity-doped.
2, using present invention process, ethylene bottom oil is extracted out by raw material gs-oil separator, is preheated through normal pressure heat exchanger, preheating with
Energy consumption is saved, 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 is rapidly heated continuously across convection section, the radiant section of heating furnace to 440 DEG C -470 with increasing feedstock oil in velocity in pipes
DEG C, the ethylene bottom oil after heating enters coking still, and the series reactions such as cracking condensation occur in coking still, realize continuity
Production.
3, using present invention process, the wax oil that is fractionated relative to wax tailings sulfur content is low, content of beary metal is 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 delayed coking equipment of the invention, being vented the methane gas collected in tower can further use
In heating
Cost is saved in the heating of furnace.
Detailed description of the invention
Fig. 1 is the full fraction ethylene bottom oil delayed coking equipment schematic diagram of the first non-impurity-doped of the invention；
Fig. 2 is the full fraction ethylene bottom oil delayed coking equipment schematic diagram of second of non-impurity-doped of the invention；
Fig. 3 is the full fraction ethylene bottom oil delayed coking equipment schematic diagram of the third non-impurity-doped of the invention；
Fig. 4 is the full fraction ethylene bottom oil delayed coking equipment schematic diagram of the 4th kind of non-impurity-doped of the invention.
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, it is defeated that 6- washs oil gas
Pipeline is sent, 7- washs oil transfer pipeline, and 8- washing devokes pipeline, the small feed-line that steams out of 9- coking still, and C4- is vented tower,
10- device in Gas feed-line, 11- oil gas collection pipeline, 12- are vented tower discharging pipeline, D1- gs-oil separator, 13- gasoline row
Pipeline out, C2- atmospheric fractional tower, 14- atmospheric fractional tower gasoline gathering line, 15- atmospheric fractional tower diesel oil gathering line, 16-
Atmospheric fractional tower wax oil gathering line, 17- washing heavy oil gathering line, 18- tail gas blow-down pipe, 19- coke gathering line,
20- sour water discharge pipe.
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 present invention is described in further detail.
Embodiment 1
The full fraction ethylene bottom oil delayed coking equipment of doping as shown in Figure 2 implements the delay coking process of ethylene bottom oil,
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, through adding
Convection section, the radiant section of hot stove are rapidly heated to 460 DEG C；Ethylene bottom oil after heating enters coking still, the recycle ratio of coking still
It is 5%, the series reactions such as cracking condensation occurs in coking still, generate rich gas, solvent naphtha, high softening point bitumen and coke,
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 still
Kettle top outflow enters oil gas and enters atmospheric fractional tower distillation, and the liquid phase of initial boiling point > 370 DEG C is washed heavy oil fraction carrying device, cut
The quality test results for cutting out 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 heating furnace
Annular smoke flue exchanges heat, and then enters convection section, radiant section, is rapidly heated to 450 DEG C；Ethylene bottom oil after heating is through four
Port valve enters coking still, and cracking condensation reaction occurs in coking still, and the recycle ratio of coking still is 8%, and it is soft to generate rich gas, height
Change point pitch and coke, high softening point bitumen and coke knot gather in kettle.It is cooled to through quench oil for 450 DEG C of oil gas temperature in kettle
It is flowed out from coking still kettle top into after scrubbing tower washing after 410 DEG C, the liquid phase washing heavy oil fraction of initial boiling point > 370 DEG C, which is sent out, to be filled
It sets, 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, 175 DEG C -361 DEG C of initial boiling point of diesel oil distillate quality test results be shown in Table the wax oil of 2B, 196 DEG C -455 DEG C of initial boiling point
The quality test results of fraction are shown in Table 2C.After coking still green coke, the material in coking still is dropped with steam and water
Temperature, the small green coke kettle oil gas that steams out of coking still enter atmospheric fractional tower together, tail gas blowdown system are entered when to water cooling coke, recycling
Sump oil and gas.
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 heating furnace
Annular smoke flue exchanges heat, and then enters convection section, radiant section, is rapidly heated to 470 DEG C；Ethylene bottom oil after heating is through four
Port valve enters coking still, and the recycle ratio of coking still is 7%, and cracking condensation reaction occurs in coking still, and it is soft to generate rich gas, height
Change point pitch and coke, high softening point bitumen and coke knot gather in kettle.It is cooled to through quench oil for 445 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 is sent out
Device, oil gas enter atmospheric fractional tower distillation, and the quality test results for being cut into -210 DEG C of initial boiling point of gasoline fraction are shown in Table
3A, 200 DEG C -360 DEG C of initial boiling point of diesel oil distillate quality test results be shown in Table 2B, 196 DEG C -470 DEG C of initial boiling point of wax oil evaporates
The quality test results divided are shown in Table 2C.The gasoline being cut into enters gs-oil separator by atmospheric fractional tower jacking, uncolled to get off
Methane 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
After, cooled down with steam and water to the material in coking still, coking still is small to steam out and the oil gas by scrubbing tower washing
Enter atmospheric fractional tower together, enters tail gas blowdown system when to water cooling coke；Coking still water supply, the steam warp vaporized in kettle
It is vented tower and cooling trough is 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 heating furnace
Flue tube exchanges heat, and then enters convection section, radiant section, is rapidly heated to 440 DEG C；Ethylene bottom oil after heating is through four-way
Valve enters coking still, and the recycle ratio of coking still is 6%, and cracking condensation reaction occurs in coking still, generates rich gas, high softening
Point pitch and coke, high softening point bitumen and coke knot gather in kettle.In kettle 410 are cooled to through quench oil for 430 DEG C of oil gas temperature
Enter scrubbing tower from the outflow of coking still kettle top after DEG C；After washing, the liquid phase washing heavy oil fraction of initial boiling point > 370 DEG C sends out dress
Set, oil gas enter atmospheric fractional tower distillation, be cut into 215 DEG C of initial boiling point < of gasoline fraction quality test results be shown in Table 4A,
The quality test results for the diesel oil distillate that 200 DEG C -360 DEG C of initial boiling point are shown in Table the wax oil fraction of 4B, 196 DEG C -470 DEG C of initial boiling point
Quality test results be shown in Table 4C.The gasoline being cut into enters gs-oil separator, uncolled watt to get off by atmospheric fractional tower jacking
This 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 knot
Shu Hou cools down to the material in coking still with steam and water, and coking still is small to steam out and the oil gas one by scrubbing tower washing
It rises and enters atmospheric fractional tower, enter tail gas blowdown system when to water cooling coke；Coking still water supply, the steam vaporized in kettle is through putting
Void tower and cooling trough are cooling, and 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 heating furnace
Annular smoke flue exchanges heat, and then enters convection section, radiant section, is rapidly heated to 465 DEG C；Ethylene bottom oil after heating is through four
Port valve enters coking still, and the recycle ratio of coking still is 7%, and cracking condensation reaction occurs in coking still, generates rich gas, solvent
Oil, high softening point bitumen and coke, high softening point bitumen and coke knot gather in kettle.In kettle 446 DEG C of oil gas temperature through quench oil
Enter scrubbing tower from the outflow of coking still kettle top after being cooled to 410 DEG C；After washing, the liquid phase washing heavy oil of initial boiling point > 470 DEG C evaporates
Device is dispensed out, oil gas enters atmospheric fractional tower distillation, is cut into the quality inspection knot of 214 DEG C of initial boiling point < of gasoline fraction
Fruit is shown in Table 6A, the quality test results of 173 DEG C -358 DEG C of initial boiling point of diesel oil distillate are shown in Table 6B, 196 DEG C -470 DEG C of initial boiling point
The quality test results of wax oil fraction are shown in Table 6C.The gasoline being cut into enters gs-oil separator by atmospheric fractional tower jacking, uncolled
The methane gas component got off enters the low pressure gas pipe network system being made of gas holder through oil gas tank gas export.Coking
After kettle green coke, cooled down with steam and water to the material in coking still, small steam out of coking still is washed with by scrubbing tower
Oil gas enter atmospheric fractional tower together；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, by the annular smoke flue of heating furnace into
Row heat exchange, and then enter convection section, radiant section, it is rapidly heated to 435 DEG C；Ethylene bottom oil after heating enters coke through four-way valve
Change 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 coke receipts
Rate is higher, and 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, by the annular smoke flue of heating furnace into
Row heat exchange, and then enter convection section, radiant section, it is rapidly heated to 490 DEG C；Ethylene bottom oil after heating enters coke through four-way valve
Change 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 equipment of the full fraction ethylene bottom oil delayed coking of non-impurity-doped of the present invention, equipment includes charging system
System, flood pattern, heating furnace, coking still F and gas recovery system for oil, heating furnace include convection section and radiant section, and convection section and
Radiant section connection, the feed end of heating furnace are connected with the outlet line 3 of the outlet line of feed system and steam injection system respectively；
The outlet of heating furnace is connected by heated material feed-line 4 with the import of coking still F, the kettle top and petroleum vapor recovery of coking still
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,
High-temperature oil gas is transported in scrubbing tower C1, the lower part scrubbing tower C1 after washing by the washing recycling of heavy oil gathering line 17 by being washed
Heavy oil is washed, the oil gas on the top scrubbing tower C1 is delivered to atmospheric fractional tower C2 by washing oil gas pipeline 6, is fractionated in normal pressure
Gasoline is recycled by gasoline gathering line 14 in the top of tower C2, recycles diesel oil by diesel oil gathering line 15, is collected by wax oil
Pipeline 16 recycles wax oil.
Embodiment 7
As the further improvement of above-described embodiment, as shown in Fig. 2, the full fraction ethylene bottom oil delay coke of non-impurity-doped of the present invention
In the equipment of change, compared to Figure 1, gas recovery system for oil further includes emptying tower C4, and the coking still of the kettle top of coking still C3 is small to steam out
Feed-line 9 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 and gas
Gas holder WQG is connected, and is connected all the way with the gas discharge mouth of gs-oil separator side, specifically: the gasoline of C2 atmospheric fractional tower is received
Manifold line 14 enters gasoline into gs-oil separator D1 through liquid phase drawer, and gs-oil separator lower part leads to the gasoline more than liquid level
It crosses the discharge of gasoline discharge pipe 13 to collect, another outlet of packing, gs-oil separator lower part passes through sour water discharge pipe 20
Sour water is discharged, discharge port of the gas through top of gs-oil separator D1 separation enters device in Gas by oil gas collection pipeline 11
Cabinet collects the light gas of methane gas and gs-oil separator separation, increases the rate of recovery of material, the material of recycling passes through gas
Letter shoot line 10 saves production cost for heating stove heating.
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 set
It is equipped with 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 need to be 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 greatly
Rubber powder is measured, 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 equipment of the full fraction ethylene bottom oil delayed coking of non-impurity-doped of the present invention.Compared to Figure 1, difference exists
It is vertical response kettle C3 in reaction kettle, furnace outlet is connected by four-way valve with vertical coking still.The top of vertical coking still
Directly it is connected with atmospheric fractional tower, carries out material fractionation.
Embodiment 9
As shown in figure 4, the difference with Fig. 2 is in the equipment of the full fraction ethylene bottom oil delayed coking of non-impurity-doped of the present invention:
Coking still C3 is vertical coking still, and furnace outlet is connected by four-way valve with vertical coking still.The top of vertical coking still is straight
It connects and is 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 equipment 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 contracting occurs in coking still
Reaction is closed, rich gas, high softening point bitumen and coke are generated；The oil gas of high temperature, which is flowed out from coking still kettle top into atmospheric fractional tower, to be cut
Cut out gasoline fraction, diesel oil distillate, wax oil fraction.After coking still green coke, with steam and water to the material in coking still into
Row cooling, small steam out of coking still enter atmospheric fractional tower together with the oil gas by scrubbing tower washing；Coking still water supply, in kettle
The steam of vaporization 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, can also make on the basis of the above description it is other it is various forms of variation or
It changes.There is no necessity and possibility to exhaust all the enbodiments.And it is extended from this it is obvious variation or
It changes still within the protection scope of the invention.
Claims (10)
1. a kind of technique of the full fraction ethylene bottom oil delayed coking of non-impurity-doped, which comprises the following steps:
Enter heating furnace heat temperature raising after ethylene bottom oil water filling after preheating, heating furnace tube outlet temperature is 440-470 DEG C；
Ethylene bottom oil after heating enters coking still and cracking condensation reaction occurs；
The oil gas that coking still reaction generates enters atmospheric fractional tower distillation separation, obtains product.
2. a kind of technique of the full fraction ethylene bottom oil delayed coking of non-impurity-doped according to claim 1, which is characterized in that step
Suddenly in (1), the preheating temperature of ethylene bottom oil is 150 DEG C -170 DEG C；The water of water filling is the 2% of feed ethylene tar weight.
3. a kind of technique of the full fraction ethylene bottom oil delayed coking of non-impurity-doped according to claim 1 or 2, feature exist
In in step (2), the temperature range of coking kettle top is 420 DEG C -450 DEG C, recycle ratio 5%-8%.
4. the technique of the full fraction ethylene bottom oil delayed coking of non-impurity-doped according to claim 1, which is characterized in that non-impurity-doped
The equipment of full fraction ethylene bottom oil delayed coking, including feed system, flood pattern, heating furnace, coking still and petroleum vapor recovery system
System, the heating furnace includes convection section and radiant section, and convection section is connected to radiant section, and the entrance of the convection section is charging
End, the outlet end of radiant section are discharge end, the feed end of the heating furnace outlet with feed system and steam injection system respectively
Line connection；The discharge end of the heating furnace and the inlet communication of coking still, kettle top and the gas recovery system for oil phase of the coking still
Even.
5. the technique of the full fraction ethylene bottom oil delayed coking of non-impurity-doped according to claim 4, which is characterized in that described right
The entrance of stream 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.
6. the technique of the full fraction ethylene bottom oil delayed coking of non-impurity-doped according to claim 4, which is characterized in that it is described into
Material system includes raw material pump, and the raw material pump is connected by pipeline with heating furnace with after heat exchanger heat exchange.
7. the technique of the full fraction ethylene bottom oil delayed coking of non-impurity-doped according to claim 6, which is characterized in that it is described into
Material system further includes relay pump, and raw material pump is connected by pipeline with relay pump with after heat exchanger heat exchange, the relay pump and
It is connected by pipeline with heating furnace.
8. the technique of the full fraction ethylene bottom oil delayed coking of non-impurity-doped according to claim 4, which is characterized in that the oil
Gas recovery system includes atmospheric fractional tower, and the coking still is vertical coking still, the kettle top and normal pressure point of the vertical coking still
Tower is evaporated to be connected.
9. the technique of the full fraction ethylene bottom oil delayed coking of non-impurity-doped according to claim 4, which is characterized in that the oil
Gas recovery system includes atmospheric fractional tower and scrubbing tower, and the coking still is horizontal coking still, the kettle top of the horizontal coking still
It is connected with scrubbing tower, scrubbing tower is connect with atmospheric fractional tower, and the scrubber overhead is connected with cooling trough.
10. the technique of the full fraction ethylene bottom oil delayed coking of non-impurity-doped according to claim 4, which is characterized in that described
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 one
Road is connected with gas holder, is connected all the way with the gas discharge mouth of gs-oil separator side；The atmospheric fractional tower and oil gas point
Feed inlet from device is connected.
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