CN101215214B - Combined technique for preparing olefin by using refining plant C4 and catalytic dry gas as raw material - Google Patents
Combined technique for preparing olefin by using refining plant C4 and catalytic dry gas as raw material Download PDFInfo
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Abstract
The invention relates to a combined process for preparing olefin taking refinery C4 and catalytic dry gas as raw materials, belonging to the technical field of preparing olefin. The invention aims to resolve the problem that presently the refinery C4 can not be sufficiently used, and the provided process comprises firstly refinery mixed C4 entering a pre-separation tower, removing dimethylmethane, propylene and isobutene from the refinery mixed C4, delivering the residue to an olefin catalytic cracking system to generate catalytic cracking gas containing propylene and ethylene, charging the catalytic cracking gas into a cooling system for cooling, then entering a compression section, adding the catalytic dry gas to mix with the catalytic cracking gas after compression of a first section, charging the compressed cracking gas into an absorbing tower, taking C4 as absorbing agent to withdraw light components containing hydrogen gas and methane from the top of the absorbing tower and separating tower bottom materials via a separation system to obtain component C2, component C3, component C4, component C5 and heavier components. The combined process of the invention has the advantages of sufficient utilization of the refinery C4, little hydrogen recirculation, low energy consumption, high propylene yield, simple operation, low investment and the like.
Description
Technical field
The present invention relates to a kind of method of producing alkene, more particularly, the present invention relates to a kind of is raw material combination technology with refining plant C 4 and catalysis drying gas.
Background technology
Along with the raising of crude oil in China working ability, C4 hydrocarbon and catalysis drying gas that the catalytic cracking unit of refinery is a large amount of with by-product.By excessive, cheap C4 hydrocarbon transform that to produce ethene, propylene be oiling in conjunction with, efficiently utilize the important channel of C4 resource, can bring remarkable economic efficiency to petroleum chemical enterprise.Round the comprehensive utilization of refining plant C 4, each major company and research unit have carried out a large amount of research both at home and abroad, have obtained certain progress, but realize industrial application seldom.Ethylene content in the plant catalytic dry gas is about 12～20 moles of % usually, and ethane content is about 15～24 moles of %, also contains alkene and alkane such as propylene, propane, butane.Plant catalytic dry gas is burnt mainly as fuel at present, and utility value is lower.If alkene, alkane in the catalysis drying gas are reclaimed, be sent to ethene factory as the raw material of producing ethene, then can save a large amount of cracking stock oil, production cost of ethylene is descended significantly, thereby make enterprise obtain favorable economic benefit.
The OCT process using high temperature tungsten-based catalyst of ABB Lummus Global company carries out C4 alkene and ethene producing propylene with dismutation.Butylene (butylene also can be obtained by ethylene dimerization) from steam cracking device and catalytic cracking unit generates propylene with ethene disproportionation in fixed bed or moving-burden bed reactor, and unreacted butylene and ethylene recycle are used.The iso-butylene that contains in the raw material does not influence the performance of catalyzer.The per pass conversion of butylene is greater than 60% in the reaction, and total conversion rate is about 92%, and propylene quality selectivity is near 100%.OCT technology and preparing ethylene by steam cracking process integration use the P/E value is brought up to more than 0.95, and can be according to the price change flexible product structure of market ethene, propylene, butylene.At present, all adopt the mode with the OCT process integration to produce propylene on the ethylene unit of Lyonden company, BASF AG and Fina company etc.
ATOFINA company and Uop Inc. have developed jointly a kind of novel process-ATOFINA-UOP technology that propylene and ethene are produced in light olefin (C4～C8 hydrocarbon) cracking that is used for.ATOFINA-UOP technology can use C4-C8 hydrocarbon from steam cracking, catalytic cracking and MTO device by-product as raw material.This technological process is used the ZSM-5 molecular sieve catalyst, under 500～600 ℃, the reaction conditions of 1～5MPa (cutting off), higher space velocity, catalytic cracking reaction takes place in the contact of fixed-bed reactor catalyst neutralisation in raw material, propylene total mass yield is about 60% in the reaction, ethene total mass yield is about 15%, and the value of propylene/ethylene is 4.Decaying catalyst is regenerated in reactor.Do not need to add water vapour in the ATOFINA-UOP technological process, the raw material air speed is higher.The ATOFINA-UOP technological process mode of production is flexible, both can unite to form new technological process with steam cracking device, thus can be according to the demand flexible propylene in market and the ratio of ethene; Can also unite use with catalytic cracking unit, to reduce the light olefin content in the pressure gasoline, propylene enhancing; In addition,, can reduce the content of C4 and C5 alkene in the product, improve the yield of propylene and ethene if ATOFINA-UOP technology and MTO device are united use.
CN 1493659 has proposed a kind of catalysis conversion method that utilizes C 4 fraction volume increase small-numerator olefin, be that the hydrocarbon gas that will be rich in C 4 fraction injects fluidized-bed or riser reactor, contact, react with the catalyzer that contains the five-ring supersiliceous zeolite, temperature of reaction is that 500～750 ℃, catalyzer and the weight ratio that is rich in the C 4 fraction hydrocarbon gas are 1～180: 1, the bed weight hourly space velocity is 0.1～20 hour
-1Or the reaction times be 0.1～10 second, making coke deposited on catalyst charcoal amount is 0.1～1.0 heavy %; Contact with gasoline fraction and/or heavy oil fraction with the reacted band Pd/carbon catalyst of the hydrocarbon gas that is rich in C 4 fraction again and be 1～100 in the weight ratio of 500～700 ℃, catalyzer and gasoline fraction or heavy oil fraction: 1, the reaction times is that 0.1～5 second or bed weight hourly space velocity are 0.1～30 hour
-1, water vapor and gasoline fraction or heavy oil fraction weight ratio be to react under 0.0～0.25: 1 the condition; Reaction product isolated and reclaimable catalyst; Reclaimable catalyst Returning reactor after stripping, regeneration recycles.
The method that reclaims ethene at present from plant catalytic dry gas mainly contains separation by deep refrigeration, middle cold oil absorption process, Separation by Complexation method, pressure swing adsorption process etc., and the whole bag of tricks differs from one another.The separation by deep refrigeration technical maturity, ethylene recovery rate height, but investment is big, and it is higher to be used for rare ethylene recovery energy consumption; The Separation by Complexation method, the ethylene recovery rate is higher, but strict to impurities in raw materials, and the pre-treatment expense is higher, needs special complexed absorption agent; Pressure swing adsorption process is simple to operate, and energy consumption is lower, but product purity is low, and the ethylene recovery rate is low, and floor space is big.
Middle cold oil absorption process mainly is to utilize absorption agent that the different solubility of each component in the gas is come separating gas mixture, the general absorption agent that utilizes earlier absorbs C2 and the above heavy constituent of C2, isolate non-condensable gasess such as methane, hydrogen, use each component in the agent of rectification method separate absorbent again.This method has characteristics such as small scale, adaptability is strong, investment cost is low, can be used for separating alkene from splitting gas, reclaims technology such as lighter hydrocarbons from Sweet natural gas.Middle cold oil absorption process can be used for the recovery of low-concentration ethane in the catalytic cracked dry gas, but the loss of cold oil absorption technique absorption agent is big in traditional routine, the ethylene recovery rate is lower, and the rate of recovery has only about 85% usually.
US 6308532 has proposed a kind of technology that reclaims ethene and propylene from oil refinery dry gas, this technology comprises from the absorption tower still extracts C3, C4, C5, C6 liquid out and part tower bottoms phase materials is circulated to cat head, thereby keep the freezing temp of overhead condenser to be not less than-95 ℃, in the absorption tower, be rich in propylene or ethylene-propylene zone simultaneously and extract the gas phase side line out.Be unlikely to low although this technology is circulated to cat head with part tower still material to keep tower top temperature, tower top temperature is still low to reach-95 ℃, still belongs to a kind of of deep cooling process for separating, and therefore investment is bigger, and energy consumption is higher.
Above-mentioned study portion has solved the problem of utilizing of C4 resource, but does not make full use of various alkane and alkene in the C4 hydrocarbon.The existing technology that reclaims ethene and propylene from oil refinery dry gas all belongs to deep cooling process for separating, has the big and high problem of energy consumption of investment.
Summary of the invention
Refining plant C 4 and catalysis drying gas utilization ratio are not high, investment is big and the high problem of energy consumption in order to solve in the present invention, proposing a kind of is raw material with refining plant C 4 and catalysis drying gas, adopts olefins by catalytic cracking to produce, separate, reclaim the technical process that obtains C2, C3 component with the method that middle cold oil absorbs.
Concrete technical scheme is as follows:
What the present invention proposed is that the combination process of feedstock production alkene may further comprise the steps with refining plant C 4 and catalysis drying gas:
(1) pre-separation: refinery's hybrid C 4 enters the pre-separation tower, and from removed overhead propane, propylene and Trimethylmethane wherein, the logistics of tower still is sent to the olefins by catalytic cracking system;
(2) olefins by catalytic cracking: the tower still logistics that comes from pre-separation tower still is sent to the catalytic cracking reaction device through preheating, and reaction generates the catalytically cracked gas that contains propylene and ethene;
(3) cooling: catalytically cracked gas enters cooling system and cools, and reclaims heat; Described cooling system adopts earlier and reclaims heat through water wash column cooling or employing waste heat boiler generation middle pressure steam again through oil scrubber, and the catalytically cracked gas temperature enters the compression section after reducing to 30～80 ℃;
(4) compression: cooled catalytically cracked gas enters the compression section, through 3 sections compressions, makes the catalytic pyrolysis atmospheric pressure reach the absolute pressure of 2.0～3.0MPa, the splitting gas that obtains compressing, wherein after the 1st section compression, add catalysis drying gas, mix, enter the 2nd section compression then with described catalytically cracked gas; At intersegmental interchanger and the surge tank of being provided with, with cooling splitting gas and the liquid phase of separating the compression generation;
(5) absorb: the splitting gas of compression enters the absorption tower after desulfurization and drying treatment, with the C4 component as absorption agent, mainly contain the light constituent of hydrogen and methane from absorption tower cat head extraction, the mixture that is dissolved with C2, C3, C4 component is sent into separation system from the extraction of tower still;
(6) separate: the mixture that contains C2, C3, C4 component enters separation system, separates by deethanizing unit, depropanizing unit and debutylize unit successively, obtains C2 component, C3 component, C4 component and C5 and more heavy constituent.
Preferably, ice chest and decompressor are set behind the absorption tower, to make full use of the cold of cat head light constituent.
Preferably, in step (2), described olefins by catalytic cracking technology is raw material with the carbon four that step (1) obtains, and mixes with water vapor, and the mass ratio of water vapor and carbon four is 0.3～0.8.Enter fixed-bed reactor after mixed material preferably is preheating to 400～500 ℃ and contact, at 400～600 ℃ of temperature, pressure 0.1～0.5MPa absolute pressure and mass space velocity 1～10h with catalyzer
-1Condition under react, generate the mixture contain propylene and ethene.The selectivity of purpose product propylene reaches 40%, and productivity of propylene reaches 25～35%.Wherein used catalyzer is that silica alumina ratio is preferably 50～300 ZSM type molecular sieve, and wherein molecular sieve carries out modification with heteropolyacid, and heteropolyacid content is preferably 5 weight %～20 weight % in the catalyzer.ZSM type molecular sieve preferably adopts the ZSM-5 molecular sieve, and the commerce of more preferably using economic technology trade center, Garden of Ten-Thousand Trees, Beijing to sell is called the molecular sieve of ZRP series, and this molecular sieve is the ZSM-5 molecular sieve of modification.Molecular sieve silica alumina ratio more preferably 180～300.What heteropolyacid was selected the combination of heteroatoms (P, Si, Fe, Co etc.) and polyatom (Mo, W, V, Nb, Ta etc.) for use in the catalyzer contains the oxygen polyacid, and preferred tungsten is heteropolyacid, more preferably phospho-wolframic acid, and content is preferably 8.0 weight %～15.0 weight %.In the fixed bed of olefins by catalytic cracking, described catalyzer is that silica alumina ratio is 50～300 ZSM type molecular sieve, and described molecular sieve carries out modification with heteropolyacid, contains the heteropolyacid of 5 weight %～20 weight % in the described catalyzer.The object lesson of described catalyzer is the catalytic cracking catalyst that the Beijing Chemical Research Institute produces.
Preferably, in step (5), the cat head working pressure on described absorption tower is 2.0～2.4MPa absolute pressure, and tower top temperature is-30～-20 ℃, and tower still temperature is 55～65 ℃, and the mass ratio of absorption agent and catalytically cracked gas is 0.8～1.6.
Preferably, the C2 component that step (6) obtains contains the ethene of 50 moles of %～60 mole %, is sent to the charging of ethylene unit as the ethene treating tower.Contain the above propylene of 85 moles of % in the C3 component that obtains, as the charging of propylene refining tower.The part of the C4 component that obtains loops back the absorption tower as absorption agent, and another part returns the catalytic cracking reaction device, the surplus extraction.The amount of C4 component various piece does not limit especially, and those skilled in the art can adjust as required.C5 reaches more heavy constituent and sends the battery limit (BL).
As required, the C4 component logistics of returning the catalytic cracking reaction device can be sent to the butylene extraction plant earlier separates, isolated alkene is returned the catalytic cracking reaction device, alkane is sent to the charging of ethylene unit as pyrocrack furnace, also can as required the C4 component not carried out extracting and separates and direct Returning reactor.
In the present invention, the described C2 that relates to, C3, C4, C5 are meant the hydro carbons that contains 2,3,4,5 carbon atoms respectively.
Owing to the present invention is directed to the problem that the refining plant C 4 that exists in the existing full scale plant and catalysis drying gas also do not make full use of, many prior aries are optimized combination, proposition is fit to make full use of the combination process of refining plant C 4 and catalysis drying gas, therefore, employed isolation technique and catalyzer etc. can adopt prior art among the present invention, enforcement of the present invention is not subjected to that disclosed or undocumented technical essential limits among the present invention, those skilled in the art can be according to circumstances selected suitably, but the present invention anything but these prior aries simply enumerate combination, but prior art is organically reasonably combined, solve the problem that present industrial production exists really, had quite significant industrial value.
Of the present invention is that the combination process of feedstock production alkene has following characteristics with refining plant C 4 and catalysis drying gas:
(1) made full use of the refining plant C 4 resource, adopting the olefins by catalytic cracking technology is propylene, ethene with the conversion of olefines in the C4 hydrocarbon, and is raw material with the catalysis drying gas simultaneously, has reclaimed alkene wherein, has improved refining plant C 4 and Utilization of Dry-Gas from Catalytic Cracking rate;
(2) refining plant C 4 of available cheapness substitutes comparatively expensive cracking stocks such as petroleum naphtha, thereby reduces production costs; Olefins by catalytic cracking reaction and employed catalyzer are not subjected to the influence of organosulfur in the refining plant C 4 substantially, have therefore avoided the interference of organosulfur;
(3) light constituents such as the methane in employing oil-absorption process separating and cracking gas and the catalysis drying gas, hydrogen, obtain components such as C2 component, C3 component, C4 respectively through separating, the C2 component is sent to ethylene unit as the charging of ethene treating tower, the C3 component can further be separated and obtained polymerization-grade propylene, the C4 component can partly circulate do absorption agent, the part loop back the catalytic cracking reaction device, each component all is fully used;
(4) olefins by catalytic cracking can be propylene, ethene with most conversion of olefines, reduced the circulation of the hydrogen that steam heat cracking behind whole hydrogenation of olefins is brought, the methane content of olefins by catalytic cracking generation simultaneously is significantly less than the methane content that the steam heat cracking is produced, thereby reduced the load of cold-zone, reduced energy consumption;
(5) adopted ice chest and decompressor in the flow process, the cold that makes full use of logistics carries out heat exchange, has reduced process cost, has reduced energy consumption, and the C2 component recovery can reach more than 95%.
(6) use the refining plant C 4 component as absorption agent, raw material obtains easily, and is with low cost;
(7) with in cold oil absorb flow process and remove methane, hydrogen, the cat head absorption temperature does not need ethylene refrigeration compressor at-30～-20 ℃, simple to operate, less investment.
Description of drawings
Fig. 1 for of the present invention be the schematic flow sheet of the combination process of feedstock production alkene with refining plant C 4 and catalysis drying gas;
Fig. 2 for of the present invention be the schematic flow sheet of the combination process of feedstock production alkene with refining plant C 4 and catalysis drying gas, adopted the butylene extraction technique to separate butylene and butane;
Fig. 3 is ice chest and a decompressor schematic flow sheet partly in the combination process of the present invention.
Nomenclature:
1. from the gaseous component that absorbs cat head; 2. liquid-phase reflux goes to the absorption tower; 3. light constituent extraction; 4. liquid phase loops back compression system; 5. ice chest; 6. first knockout drum; 7. decompressor; 8. second knockout drum.
Embodiment
Below with reference to accompanying drawing 1～3, produce the combination process of alkene with further employing refining plant C 4 of the present invention and the catalysis drying gas explained of the mode of embodiment, but be not limited to these schemes.
Fig. 1 for of the present invention be the schematic flow sheet that raw material is produced alkene with refining plant C 4 and catalysis drying gas.
With reference to figure 1, the main composition (mass percent) of refining plant C 4 is: propane 9.3%, 1-butylene 13.8%, iso-butylene 13.9%, anti--2-butylene 20%, suitable-2-butylene 16.2%, Trimethylmethane 0.5～10.0%, normal butane 16.3%, surplus are propylene, and flow is 15400kg/h.Refining plant C 4 is introduced into the pre-separation tower, the stage number of pre-separation tower is 130, operational condition is: 74.6 ℃ of 41.7 ℃ of tower top temperatures, tower top pressure 0.95MPa (cutting off), tower still temperature, cat head extraction light constituent, it is mainly formed (molar percentage) and is: propylene 1.6%, propane 48.1%, Trimethylmethane 44.7%, surplus are butylene.The logistics of pre-separation Tata still extraction is preheating to 500 ℃, enter the catalytic cracking reaction device then, loaded catalyst is 7 tons, catalyzer adopts the trade mark BOC-1 catalyzer of Beijing Chemical Research Institute, the amount 9630kg/h of water vapor, reaction conditions is: 550 ℃ of temperature, pressure 0.2MPa (cutting off), mass space velocity 2.5h
-1Reaction conditions under, the C4 raw material contacts with catalyzer in fixed-bed reactor catalytic cracking reaction takes place, propylene total mass yield is about 30% in the reaction, ethene total mass yield is about 15%.
The catalytically cracked gas that reaction generates enters oil scrubber, and operational condition is: 199.4 ℃ of 137.3 ℃ of tower top temperatures, tower top pressure 0.12MPa (cutting off), tower still temperature.Catalytically cracked gas is gone into water wash column through oil scrubber is laggard, and operational condition is: 89.3 ℃ of 43.5 ℃ of tower top temperatures, tower top pressure 0.12MPa (cutting off), tower still temperature, the catalytically cracked gas temperature is reduced to 43.5 ℃, enters the compression section then.Pressure is 0.7MPa (cutting off) after 1 section compression, is that the catalysis drying gas of 9663kg/h is mixed into 2 sections compressions with flow after the heat exchange, and through the 3rd section compression, mixture pressure enters the absorption tower after reaching 2.6MPa (cutting off) again.The main composition (mole) of catalysis drying gas is: H
223.4%, N
218.1%, CH
426.1%, C
2H
411.1%, C
2H
612.4%, surplus is C
3H
6In the absorption tower, make absorption agent with the C4 component, the mass flux ratio of absorption agent and splitting gas is 1.2, and the stage number on absorption tower is 45, operational condition is: tower top temperature-26.6 ℃, tower top pressure 2.16MPa (cutting off), 60.2 ℃ of tower still temperature, tower still pressure 2.2MPa (cutting off), the H of cat head extraction
2, CH
4Enter thereafter ice chest system Deng light constituent, be dissolved with C
2H
4, C
3H
6The logistics of tower still from the extraction of tower still, be sent to separation system.
The logistics that comes from the absorption tower still separates through deethanizing column, depropanizing tower, debutanizing tower successively.The deethanizing column stage number is 45, operational condition is: tower top temperature-16.0 ℃, tower top pressure 2.35MPa (cutting off), 103.5 ℃ of tower still temperature, reflux ratio 4.0, cat head extraction C2 component is sent to ethylene unit, wherein contains ethene 58.4% (mole), and depropanizing tower is sent in the logistics of deethanizing column still; The depropanizing tower stage number is 65, operational condition is: 43.6 ℃ of tower top temperatures, tower top pressure 1.77MPa (cutting off), 104.4 ℃ of tower still temperature, reflux ratio 7.5, cat head extraction C3 component, wherein contain more than the propylene 89% (mole), can be used as the charging of propylene refining tower, debutanizing tower is sent in the logistics of depropanizing tower still; The debutanizing tower stage number is 45, and operational condition is: 46.8 ℃ of tower top temperatures, tower top pressure 0.59MPa (cutting off), 98.4 ℃ of tower still temperature, reflux ratio 1.1, and cat head extraction C4 component, the battery limit (BL) is sent in tower still extraction C5 and more heavy constituent.Separate the C4 component part that obtains and loop back the absorption tower as absorption agent, part loops back the olefins by catalytic cracking reactor, the surplus extraction, and the ratio of three parts is 8: 1.5: 0.5.
With reference to figure 2, adopt the refining plant C 4 raw material identical with example 1, through pre-separation, olefins by catalytic cracking, cooling, compression, absorption, deethanizing, depropanizing, debutylize unit, C4 component by the extraction of debutylize cat head, part loops back the absorption tower as absorption agent, rest part is gone to the butylene extraction plant, and two-part throughput ratio is 3: 1.The butylene extraction plant adopts acetonitrile to make solvent, and the operational condition of extractive distillation column is: solvent ratio (quality) 10,46 ℃ of tower top temperatures, tower top pressure 0.45MPa (cutting off), reflux ratio 20.Isolated alkene loops back olefins by catalytic cracking, separates that to obtain flow be that the butane of 3427kg/h is sent the battery limit (BL) as product, and wherein mainly forming (quality) is Trimethylmethane 10.9%, normal butane 83.9%, and this logistics can be used as the charging of ethene pyrocrack furnace.
Fig. 3 is ice chest and a decompressor schematic flow sheet partly in the combination process of the present invention.
With reference to figure 3, from absorbing the gas phase 1 of cat head, temperature is-26.6 ℃, pressure is 2.16MPa (cutting off), enter first knockout drum 6 after entering ice chest 5 heat exchange, isolated liquid phase 2 is gone to the absorption tower as backflow, gas phase goes decompressor 7 to be expanded to 0.98MPa (cutting off), temperature is reduced to-107.6 ℃, the liquid separating tank 8 that degass of the material after the cooling, isolated gas phase and liquid phase go respectively ice chest 5 as the cold flow thigh with carry out heat exchange from the gas phase that absorbs cat head, after the heat exchange, the temperature of gas phase 3 is-30 ℃, pressure 0.97MPa (cutting off), as the light constituent extraction, it is mainly formed (mole) and is: H
232.7%, N
225.4%, CH
437.1%, C
2H
41.5%, surplus is C
2H
6 Liquid phase 4 loops back compression system.
Claims (8)
1. one kind is the combination process of feedstock production alkene with refining plant C 4 and catalysis drying gas, it is characterized in that, described combination process may further comprise the steps:
(1) pre-separation: refinery's hybrid C 4 enters the pre-separation tower, and from removed overhead propane, propylene and Trimethylmethane wherein, the logistics of tower still is sent to the olefins by catalytic cracking system;
(2) olefins by catalytic cracking: the tower still logistics that comes from pre-separation tower still is sent to the catalytic cracking reaction device through preheating, and reaction generates the catalytically cracked gas that contains propylene and ethene;
(3) cooling: catalytically cracked gas enters cooling system and cools, and reclaims heat; Described cooling system adopts earlier and reclaims heat through water wash column cooling or employing waste heat boiler generation middle pressure steam again through oil scrubber, and the catalytically cracked gas temperature enters the compression section after reducing to 30～80 ℃;
(4) compression: cooled catalytically cracked gas enters the compression section, through 3 sections compressions, makes the catalytic pyrolysis atmospheric pressure reach the absolute pressure of 2.0～3.0MPa, the splitting gas that obtains compressing, wherein after the 1st section compression, add catalysis drying gas, mix, enter the 2nd section compression then with described catalytically cracked gas; At intersegmental interchanger and the surge tank of being provided with, with cooling splitting gas and the liquid phase of separating the compression generation;
(5) absorb: the splitting gas of compression enters the absorption tower after desulfurization and drying treatment, with the C4 component as absorption agent, mainly contain the light constituent of hydrogen and methane from absorption tower cat head extraction, the mixture that is dissolved with C2, C3, C4 component is sent into separation system from the extraction of tower still;
(6) separate: the mixture that contains C2, C3, C4 component enters separation system, separates by deethanizing unit, depropanizing unit and debutylize unit successively, obtains C2 component, C3 component, C4 component and C5 and more heavy constituent.
2. combination process as claimed in claim 1 is characterized in that, ice chest and decompressor are set behind the absorption tower, and absorption tower cat head light constituent enters ice chest and decompressor to reclaim cold.
3. combination process as claimed in claim 1, it is characterized in that, olefins by catalytic cracking technology described in the step (2) is raw material with the carbon four that step (1) obtains, after water vapor mixes, in fixed-bed reactor, contact, at 400～600 ℃ of temperature of reaction, pressure 0.1～0.5MPa absolute pressure and mass space velocity 1～10h with catalyzer
-1Condition under react, generate the mixture contain propylene and ethene.
4. combination process as claimed in claim 1 is characterized in that, in step (5), the cat head working pressure on described absorption tower is 2.0～2.4MPa absolute pressure, tower top temperature is-30～-20 ℃, and tower still temperature is 55～65 ℃, and the mass flux ratio of absorption agent and catalytically cracked gas is 0.8～1.6.
5. combination process as claimed in claim 1 is characterized in that, the C2 component that step (6) obtains contains the ethene of 50 moles of %～60 mole %, is sent to the charging of ethylene unit as the ethene treating tower.
6. combination process as claimed in claim 1 is characterized in that, contains the above propylene of 85 moles of % in the C3 component that step (6) obtains, as the charging of propylene refining tower.
7. combination process as claimed in claim 1 is characterized in that, the part of the C4 component that step (6) obtains loops back the absorption tower as absorption agent, and a part is returned the catalytic cracking reaction device, the surplus extraction.
8. combination process as claimed in claim 1, it is characterized in that, the C4 component logistics of returning the catalytic cracking reaction device that step (6) is obtained is sent to the butylene extraction plant earlier and separates, isolated alkene is returned the catalytic cracking reaction device, and alkane is sent to the charging of ethylene unit as pyrocrack furnace.
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| CN102285853A (en) * | 2010-06-18 | 2011-12-21 | 中国石油化工股份有限公司 | Method for increasing yield of propylene and ethylene by using cracked C4 as raw material |
| CN102070389A (en) * | 2011-01-12 | 2011-05-25 | 王伟跃 | Technology for preparing propylene by utilizing by-products in refinery |
| CN102965143B (en) | 2011-09-01 | 2015-01-21 | 富德（北京）能源化工有限公司 | Absorption separation method of cracking gas in low-carbon olefin preparation process |
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