CN102115355B - Method for separating low-carbon olefins - Google Patents
Method for separating low-carbon olefins Download PDFInfo
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- CN102115355B CN102115355B CN2010106076792A CN201010607679A CN102115355B CN 102115355 B CN102115355 B CN 102115355B CN 2010106076792 A CN2010106076792 A CN 2010106076792A CN 201010607679 A CN201010607679 A CN 201010607679A CN 102115355 B CN102115355 B CN 102115355B
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- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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Abstract
The invention discloses a separation method of low-carbon olefins, which adopts the mature normal separation process flow of the traditional ethylene industry and improves ethylene yield by using a solvent absorption process in a demethanizer. In the invention, the normal separation process is adopted, ethane, propane or mixture of ethane and propane is used as an absorbent, a deep-cooling cold box and an ethylene compressor are not used, equipment investment and energy consumption are lowered, and the method is very applicable to a process for producing low-carbon olefins by using oxygenated chemicals or catalytic reaction of olefins.
Description
Technical field
The invention belongs to the low-carbon alkene separation technology field, relate in particular to the separation method of preparing low-carbon olefin from oxygen-containing compounds or hydro carbons catalyzed reaction producing light olefins.
Background technology
Ethene, propylene are the basic materials of petrochemical industry, and its conventional production methods mainly adopts the naphtha steam cracking method to make, and petroleum resources are relied on serious.Growing tension along with oil supply, preparing low-carbon olefin from oxygen-containing compounds becomes the focus of research, and obtained significant progress, oxygenatedchemicals comprises alcohol, ether, aldehyde and ketone etc., wherein methyl alcohol and dme are used more extensive, can make by coal or Sweet natural gas, the pressure that this can alleviate oil supply to a certain extent especially meets the national conditions of China's " oil starvation, weak breath, rich coal ".
Because hydrogen, methane content are higher, generally adopt deep cooling to come separation of methane and ethene in the conventional tubular stove splitting gas, to improve yield of ethene.Typical deep cooling separating method comprises order separation, front-end deethanization and predepropanization process, three kinds of flow processs have relative merits separately, but all need the deep cooling condition below-100 ℃, need ethylene compressor, even need methane compressor to provide cold for it, ice chest is had relatively high expectations, make construction investment strengthen.
The characteristics of preparing low-carbon olefin from oxygen-containing compounds are that hydrogen, methane content are lower, and ethene, propylene content are higher, and high-carbon hydrocarbon contents such as C5+ are less, the cold that causes demethanizing tower to need is less, as adopting deep cooling separating method, to the equipment requirements height, investment is big, the energy consumption height, and economic benefit is not good.
US7714180 has proposed a kind of processing method of olefin recovery.According to this method, process gas at first removes C5+ through debutanizing tower after compression, C4-further compresses again, cool off back laggard demethanizing tower, deethanizing column, depropanizing tower earlier, and hybrid C 4 goes demethanizing tower to absorb ethene in the overhead gas as absorption agent at the bottom of the depropanizing Tata, improves yield of ethene.This invention avoids adopting deep cooling process for separating, but adopts oily absorption technique, has reduced investment, but is to use hybrid C 4 absorption agent internal circulating load big and circulation process is long, and energy consumption is big, and if when containing more divinyl among the C4, can make that the upstream device coking is serious.
Chinese patent 200810201217.3 has proposed the separation method of light hydrocarbon product in a kind of MTO/MTP reaction product.According to this method, directly send into deethanizing column after the pre-treatment of lighter hydrocarbons product, cat head C2-enters the absorption tower again, makees absorption agent to improve the ethylene recovery rate with ethane.This method is similar with above-mentioned two kinds of methods, avoided the use ethylene compressor, adopted ethane to make absorption agent, part ethane steams from the absorption tower cat head and makes fuel gas, when but the ethane that produces when reaction process was less than the ethane that the absorption tower steams, it was just improper to use ethane to make absorption agent.
Summary of the invention
The present invention is according to the characteristics of preparing low-carbon olefin from oxygen-containing compounds gas composition, proposed that a kind of energy consumption is low, less investment and make full use of the lower carbon number hydrocarbons separation method that self-produced byproduct is made absorption agent.
The present invention adopts following technical scheme:
A kind of separation method of low-carbon alkene, adopt the sophisticated order separation process of traditional ethylene industry, it is characterized in that using the method for solvent absorbing to improve yield of ethene at demethanizing tower, lyosorption is the self-produced ethane of system, propane or ethane/propane mixture, specifically may further comprise the steps:
(1) will react the product mixing of producing light olefins after after the series of preprocessing steps such as chilling, compression, purification and cooling from the product of oxygenatedchemicals reaction for preparing light olefins device or from olefin catalytic, be divided into gas phase hydrocarbon and hydrocarbon liquid phase, the gas phase hydrocarbon advances demethanizing tower with hydrocarbon liquid phase to be separated;
(2) demethanizing tower uses the method that ethane, propane or ethane/propane mixture absorbs, and to improve yield of ethene, light constituent is told from cat head, and light constituent comprises CH
4, CO, H
2, N
2Etc. component, isolated light constituent is made fuel gas or is gone hydrogen manufacturing after reclaiming cold, and the above heavy constituent of C2 and C2 are told at the bottom of demethanizer;
(3) go deethanizing column to carry out separating of C2 and C3+ by isolated C2+ component at the bottom of the demethanizer;
(4) all or part of acetylene rear section that removes of deethanizer overhead C2 enters ethylene column, or portion C 2 directly loops back reactive system with further system propylene, improves the selectivity of propylene, and C3+ removes depropanizing tower at the bottom of the deethanizing Tata;
(5) by the smart ethene of ethylene column cat head or top side line extraction, by ethylene column bottom side line extraction crude ethylene, or the whole crude ethylenes of ethylene column cat head extraction, or all smart ethene of extraction, not extraction crude ethylene; Crude ethylene reclaims the low temperature cold more earlier through decompressor reclaim under reduced pressure energy or through expenditure and pressure, and the crude ethylene behind decompression and recovery cold loops back reactive system and further makes propylene, to improve the propylene selectivity; Enter demethanizing tower as absorption agent after all or part of cooling of ethane at the bottom of the tower;
(6) the depropanizing tower cat head removes hydrogenation or directly removes propylene tower, and by propylene tower cat head or side line extraction propylene, another component that propane all makes to do after byproduct output or all or part of cooling absorption agent at the bottom of the tower enters demethanizing tower; The C4+ component directly or through subsequent disposal rear section dereaction system is further made propylene at the bottom of the depropanizing Tata, or directly does byproduct output after treatment.
The separation method of low-carbon alkene, described preprocessing process are that process atmospheric pressures is reduced to 2.2～3.8MPa, and C5+ is told from process gas, are cooled to 5～-40 ℃, the removing of sour gas and oxygenatedchemicals, and the drying process of moisture.
The separation method of low-carbon alkene, described demethanizing tower adopt ethane, propane or ethane/propane mixture to make absorption agent, and the preferred temperature of absorption agent is 5～-40 ℃,
The separation method of low-carbon alkene, described depropanizing tower adopt single tower or high and low pressure double tower process flow process.
The separation method of low-carbon alkene, all or part of C2 of deethanizer overhead extraction removes ethylene column, and all the other C2 loop back reactive system and further make propylene.
The separation method of low-carbon alkene, all or part of smart ethene of ethylene column cat head or top side line extraction, part ethene loops back reactive system with the crude ethylene form from the side line extraction of ethylene column bottom and further makes propylene, to improve the propylene selectivity.
The separation method of low-carbon alkene, the crude ethylene of the C2 component of deethanizing cat head extraction and ethylene column cat head or side line extraction is earlier through decompressor reclaim under reduced pressure energy or through expenditure and pressure, reclaim the low temperature cold again, crude ethylene behind decompression and recovery cold loops back reactive system and further makes propylene, to improve the propylene selectivity.
The separation method of low-carbon alkene, demethanizing tower top is provided with a side cooler, to reduce absorption agent consumption and overhead condenser refrigeration duty.
Advantage of the present invention:
The characteristics that the present invention forms according to the preparing low-carbon olefin from oxygen-containing compounds product, use order separation process, and use ethane, propane or ethane/propane mixture to make absorption agent, avoid adopting deep cooling ice chest and ethylene compressor, reduced facility investment and energy consumption, preparing low-carbon olefin from oxygen-containing compounds or olefin catalytic reaction preparing low carbon olefin hydrocarbon have been had good suitability.
Description of drawings
Fig. 1 is the block diagram of the separation method of the 1st kind of low-carbon alkene of the present invention.
Fig. 2 is the block diagram of the separation method of the 2nd kind of low-carbon alkene of the present invention.
Fig. 3 is the block diagram of the separation method of the 3rd kind of low-carbon alkene of the present invention.
Embodiment
If demethanizing tower uses propane absorbent, then use technical process shown in Figure 1.From the product of preparing low-carbon olefin from oxygen-containing compounds reactor with or mix after behind a series of pre-treatment steps such as chilling, compression, purification and cooling, be divided into gas phase hydrocarbon and hydrocarbon liquid phase from the product of olefin catalytic reaction producing light olefins.Gas phase hydrocarbon and hydrocarbon liquid phase advance demethanizing tower and tell light constituent, and demethanizer column overhead uses propane to make absorption agent, to improve yield of ethene.C2+ enters deethanizing column at the bottom of the demethanizer, and deethanizer overhead C2 all goes ethylene column or part to go ethylene column, part to loop back reactive system, and C3+ advances depropanizing tower at the bottom of the deethanizing Tata.The smart ethene of ethylene column top side line extraction, the portion C 2 of cat head and bottom side line extraction crude ethylene and deethanizer overhead extraction loops back reactive system and further makes propylene after reclaiming cold again behind throttling or the decompressor recovered energy; Ethylene column also can be selected not extraction crude ethylene, and a small amount of light constituent of ethylene column cat head this moment removes compression system, and the gas extraction acts as a fuel behind the ethane recovery cold at the bottom of the tower; Ethylene column also can be selected the smart ethene of not extraction, cat head extraction crude ethylene, extraction ethane at the bottom of the tower.C3+ removes the two depropanizing towers of high and low pressure at the bottom of the deethanizing Tata, high pressure depropanizer cat head extraction C3 removes propylene tower, extraction C4+ component directly or loop back reactive system through the subsequent disposal rear section and further make propylene or is directly exported as byproduct after treatment at the bottom of the low pressure depropanizing Tata.Propylene tower cat head extraction propylene product, extraction propane is all or part of at the bottom of the tower exports as byproduct as demethanizing tower absorption agent, part.
If demethanizing tower uses the ethane absorption agent, then use technical process shown in Figure 2.From the product of preparing low-carbon olefin from oxygen-containing compounds reactor with or mix after behind a series of pre-treatment steps such as chilling, compression, purification and cooling, be divided into gas phase hydrocarbon and hydrocarbon liquid phase from the product of olefin catalytic reaction producing light olefins.Gas phase hydrocarbon and hydrocarbon liquid phase advance demethanizing tower and tell light constituent, and demethanizer column overhead uses ethane to make absorption agent, to improve yield of ethene.C2+ enters deethanizing column at the bottom of the demethanizer, and deethanizer overhead C2 all goes ethylene column or part to go ethylene column, part to loop back reactive system, and C3+ advances depropanizing tower at the bottom of the deethanizing Tata.The smart ethene of ethylene column top side line extraction, the portion C 2 of cat head and bottom side line extraction crude ethylene and deethanizer overhead extraction loops back reactive system and further makes propylene after throttling or decompressor recovered energy reclaim cold again, ethylene column also can be selected not extraction crude ethylene, the a small amount of light constituent of ethylene column cat head this moment removes compression system, and the gas extraction acts as a fuel behind the ethane recovery cold at the bottom of the tower; Ethylene column also can be selected the smart ethene of not extraction, cat head extraction crude ethylene, extraction ethane at the bottom of the tower.C3 removes propylene tower at the bottom of the deethanizing Tata, and extraction C4+ component directly or loop back reactive system through the subsequent disposal rear section and further make propylene or is directly exported as byproduct after treatment at the bottom of the low pressure depropanizing Tata.Propylene tower cat head extraction propylene product, extraction propane byproduct at the bottom of the tower.
If demethanizing tower need use ethane, propane two-pack absorption agent, then use technical process shown in Figure 3.From the product of preparing low-carbon olefin from oxygen-containing compounds reactor with or mix after behind a series of pre-treatment steps such as chilling, compression, purification and cooling, be divided into gas phase hydrocarbon and hydrocarbon liquid phase from the product of olefin catalytic reaction producing light olefins.Gas phase hydrocarbon and hydrocarbon liquid phase advance demethanizing tower and tell light constituent, and demethanizer column overhead is used ethane, propane two-pack absorption agent, to improve yield of ethene.C2+ enters deethanizing column at the bottom of the demethanizer, and deethanizer overhead C2 all goes ethylene column or part to go ethylene column, part to loop back reactive system, and C3+ advances depropanizing tower at the bottom of the deethanizing Tata.The smart ethene of ethylene column top side line extraction, the portion C 2 of cat head and bottom side line extraction crude ethylene and deethanizer overhead extraction loops back reactive system and further makes propylene after throttling or decompressor recovered energy reclaim cold again, ethylene column also can be selected not extraction crude ethylene, the a small amount of light constituent of ethylene column cat head this moment removes compression system, and the gas extraction acts as a fuel behind the ethane recovery cold at the bottom of the tower; Ethylene column also can be selected the smart ethene of not extraction, cat head extraction crude ethylene, extraction ethane at the bottom of the tower.Do demethanizing tower absorption agent, the part gas extraction that acts as a fuel at the bottom of the ethene Tata after all or part of cooling of ethane.C3+ removes the two depropanizing towers of high and low pressure at the bottom of the deethanizing Tata, high pressure depropanizer cat head extraction C3 removes propylene tower, extraction C4+ component directly or loop back reactive system through the subsequent disposal rear section and further make propylene or is directly exported as byproduct after treatment at the bottom of the low pressure depropanizing Tata.Propylene tower cat head extraction propylene product, all or part of another component or the part as the demethanizing tower absorption agent of extraction propane exported as byproduct at the bottom of the tower.
Embodiment 1
As Fig. 1, come self-reacting lower carbon number hydrocarbons through chilling, compression and impurity removal postcooling, at first advance demethanizing tower charging separating tank and carry out gas-liquid separation under 3.2MPa ,-30 ℃ condition, demethanizing tower adopts propane to make absorption agent, and wherein the propane absorbent temperature is-20 ℃.Demethanizer column overhead is CH
4, H
2, CO and N
2Deng the propane absorbent of light constituent and partial loss, at the bottom of the demethanizer C2+ component, directly advance deethanizing column.Deethanizer overhead C2 all removes ethylene column, does not loop back reactive system, and C3+ advances depropanizing tower at the bottom of the deethanizing Tata.The smart ethene of ethylene column side line extraction, the cat head crude ethylene removes compression system, bottom not extraction of side line crude ethylene, the gas extraction acts as a fuel behind the ethane recovery cold at the bottom of the tower.High pressure depropanizer cat head extraction C3 removes the propine hydrogenation or directly removes propylene tower, and extraction C4+ component directly or loop back reactive system through the subsequent disposal rear section and further make propylene or is directly exported as byproduct after treatment at the bottom of the low pressure depropanizing Tata.Propylene tower cat head extraction propylene product, the extraction part is exported as byproduct as absorption agent, part at the bottom of the tower.
Table 1 is an embodiment calculation result, and as can be seen from the table, the ethene that loses in the cat head dry gas is 0.0414kmol/h, and yield of ethene is 99.994%, and the propane of loss is 7.8395kmol/h, accounts for 2.9% of total absorption agent.
Table 1 with the propylene Tata at the bottom of propane be the calculation result of absorption agent
| The logistics title | Feed component | Lyosorption | The cat head dry gas | |
| The thing stream number | S1 | S3 | S2 | |
| Temperature | ℃ | -20.00 | -20.00 | -37.00 |
| Pressure | MPaG | 3.00 | 3.00 | 3.00 |
| Molar flow | kmol/h | 2021 | 270 | 160.613 |
| Mass rate | kg/h | 77004.6 | 11961.8 | 1724.44 |
| Each component molar flow | kmol/h | |||
| N 2 | 11.9900 | 0 | 11.9900 | |
| H 2 | 89.0000 | 0 | 89.0000 | |
| CO | 0.6068 | 0 | 0.6068 | |
| CH 4 | 50.4466 | 0 | 50.2336 | |
| C 2H 2 | 0.0576 | 0 | 0.0000 | |
| C 2H 4 | 693.77 | 0 | 0.0414 | |
| C 2H 6 | 85.78 | 0 | 0.0002 | |
| C 3H 6 | 611.12 | 10.92 | 0.5517 | |
| C 3H 8 | 45.10 | 231.16 | 7.8395 | |
| C 4H 8 | 298.05 | 2.06 | 0.0073 | |
| C 4H 10 | 33.1800 | 0.1630 | 0.0007 | |
| C 5H 10 | 51.0500 | 0 | 0 | |
| C 5H 12 | 28.6000 | 0 | 0 | |
| C 6H 12 | 15.5950 | 0 | 0 | |
| DME | 6.6500 | 25.6880 | 0.3415 |
Embodiment 2
As Fig. 2, come self-reacting lower carbon number hydrocarbons through chilling, compression and impurity removal postcooling, at first advance demethanizing tower charging separating tank and carry out gas-liquid separation under 3.2MPa ,-30 ℃ condition, demethanizing tower adopts ethane to make absorption agent, and wherein ethane absorption agent temperature is-20 ℃.Demethanizer column overhead is CH
4, H
2, CO and N
2In the ethane absorption agent of light constituent and partial loss, at the bottom of the tower C2+ component, directly advance deethanizing column.Deethanizer overhead C2 partly goes ethylene column, part to loop back reactive system, and C3+ advances depropanizing tower at the bottom of the deethanizing Tata.The smart ethene of ethylene column side line extraction, the portion C 2 of cat head and side line extraction crude ethylene and deethanizer overhead extraction loops back reactive system and further makes propylene after reclaiming cold again behind the decompressor recovered energy, make the demethanizing tower absorption agent after all or part of cooling of ethane at the bottom of the ethene Tata, the gas extraction partly acts as a fuel.High pressure depropanizer cat head extraction C3 removes the propine hydrogenation or directly removes propylene tower, and extraction C4+ component directly or loop back reactive system through the subsequent disposal rear section and further make propylene or is directly exported as byproduct after treatment at the bottom of the low pressure depropanizing Tata.Propylene tower cat head extraction propylene product, extraction propane is exported as byproduct at the bottom of the tower.
Table 2 is an embodiment calculation result, as can be seen from the table, the ethene that loses in the cat head dry gas is 0.8757kmol/h, yield of ethene is 99.874%, the ethane of loss is 77.708kmol/h, accounts for 25.94% of total absorption agent, though lose more, but this dry gas still can be used as the fuel gas use after reclaiming cold, does not reduce the utility value of ethane.
Table 2 with the ethane Tata at the bottom of ethane be the calculation result of absorption agent
| The logistics title | Feed component | Lyosorption | The cat head dry gas | |
| S1 | S3 | S2 | ||
| Temperature | ℃ | -30.00 | -20.00 | -37.00 |
| Pressure | MPaG | 2.96 | 2.97 | 3.00 |
| Molar flow | kmol/h | 2025.75 | 300.00 | 230.46 |
| Mass rate | kg/h | 77147.5 | 9033.85 | 3701.38 |
| Each component molar flow | kmol/h | |||
| N 2 | 11.99 | 0 | 11.99 | |
| H 2 | 89 | 0 | 89 | |
| CO | 0.6068 | 0 | 0.6068 | |
| CH 4 | 50.4466 | 0 | 50.2371 | |
| C 2H 2 | 0.0576 | 0 | 0 | |
| C 2H 4 | 693.765 | 1.5005 | 0.87568 | |
| C 2H 6 | 90.53 | 297.179 | 77.708 | |
| C 3H 6 | 611.122 | 1.2604 | 0.0444 | |
| C 3H 8 | 45.1042 | 0.0600 | 0.0014 | |
| C 4H 8 | 298.05 | 0 | 0 | |
| C 4H 10 | 33.18 | 0 | 0 | |
| C 5H 10 | 51.05 | 0 | 0 | |
| C 5H 12 | 28.6 | 0 | 0 | |
| C 6H 12 | 15.595 | 0 | 0 | |
| DME | 6.6500 | 0 | 0 |
Embodiment 3
As Fig. 3, come self-reacting lower carbon number hydrocarbons through chilling, compression and impurity removal postcooling, at first advance demethanizing tower charging separating tank and carry out gas-liquid separation under 3.2MPa ,-30 ℃ condition, demethanizing tower adopts the mixture of ethane and propane to make absorption agent, and wherein the absorption agent temperature is-20 ℃.Demethanizer column overhead is CH
4, H
2, CO and N
2Deng ethane, the propane absorbent of light constituent and partial loss, at the bottom of the tower C2+ component, directly advance deethanizing column.Deethanizer overhead C2 partly goes ethylene column, part to loop back reactive system, and C3+ advances depropanizing tower at the bottom of the deethanizing Tata.The smart ethene of ethylene column side line extraction, the portion C 2 of cat head and side line extraction crude ethylene and deethanizer overhead extraction loops back reactive system and further makes propylene after reclaiming cold again behind throttling or the decompressor recovered energy, make the demethanizing tower absorption agent after all or part of cooling of ethane at the bottom of the ethene Tata, the gas extraction partly acts as a fuel.High pressure depropanizer cat head extraction C3 removes the propine hydrogenation or directly removes propylene tower, and extraction C4+ component directly or loop back reactive system through the subsequent disposal rear section and further make propylene or is directly exported as byproduct after treatment at the bottom of the low pressure depropanizing Tata.Propylene tower cat head extraction propylene product, extraction propane part is exported as byproduct as absorption agent, part at the bottom of the tower.
Table 3 is an embodiment calculation result, as can be seen from the table, the ethene that loses in the cat head dry gas is 0.43225kmol/h, yield of ethene is 99.94%, the ethane of loss is 40.9917kmol/h, account for 13.66% of total absorption agent, the propane of loss is 4.544kmol/h, accounts for 1.515% of total absorption agent.
Table 3 is the calculation result of composite absorber with ethane and propane
| The logistics title | Feed component | Lyosorption | The cat head dry gas | |
| S1 | S3 | S2 | ||
| Temperature | ℃ | -30 | -20 | -37 |
| Pressure | MPaG | 2.96 | 2.97 | 3 |
| Molar flow | kmol/h | 2025.75 | 300 | 198.265 |
| Mass rate | kg/h | 77147.5 | 11162.4 | 2803.66 |
| Each component molar flow | kmol/h | |||
| N 2 | 11.99 | 0 | 11.99 | |
| H 2 | 89 | 0 | 89 | |
| CO | 0.6068 | 0 | 0.6068 | |
| CH 4 | 50.4466 | 0 | 50.2339 | |
| C 2H 2 | 0.0576 | 0 | 0 | |
| C 2H 4 | 693.765 | 0.75023 | 0.43225 | |
| C 2H 6 | 90.53 | 148.59 | 40.9917 | |
| C 3H 6 | 611.122 | 6.69655 | 0.29156 | |
| C 3H 8 | 45.1042 | 128.455 | 4.54435 | |
| C 4H 8 | 298.05 | 1.14703 | 0.00334 | |
| C 4H 10 | 33.18 | 0.09054 | 0.0003 | |
| C 5H 10 | 51.05 | 0 | 0 | |
| C 5H 12 | 28.6 | 0 | 0 | |
| C 6H 12 | 15.595 | 0 | 0 | |
| DME | 6.65 | 14.2711 | 0.17111 |
Claims (7)
1. the separation method of a low-carbon alkene, adopt the sophisticated order separation process of traditional ethylene industry, it is characterized in that using the method for solvent absorbing to improve yield of ethene at demethanizing tower, lyosorption is the self-produced ethane of system, propane or ethane/propane mixture; May further comprise the steps:
(1) will react the product mixing of producing light olefins after after chilling, compression, purification and the cooling series of preprocessing step from the product of oxygenatedchemicals reaction for preparing light olefins device or from olefin catalytic, be divided into gas phase hydrocarbon and hydrocarbon liquid phase, the gas phase hydrocarbon advances demethanizing tower with hydrocarbon liquid phase to be separated;
(2) demethanizing tower uses the method that ethane, propane or ethane/propane mixture absorbs, and to improve yield of ethene, light constituent is told from cat head, and light constituent comprises CH
4, CO, H
2, N
2Component, isolated light constituent is made fuel gas or is gone hydrogen manufacturing after reclaiming cold, and the above heavy constituent of C2 and C2 are told at the bottom of demethanizer;
(3) go deethanizing column to carry out separating of C2 and C3+ by isolated C2+ component at the bottom of the demethanizer;
(4) all or part of acetylene rear section that removes of deethanizer overhead C2 enters ethylene column, or portion C 2 directly loops back reactive system with further system propylene, improves the selectivity of propylene, and C3+ removes depropanizing tower at the bottom of the deethanizing Tata;
(5) by the smart ethene of ethylene column cat head or top side line extraction, by ethylene column bottom side line extraction crude ethylene, or the whole crude ethylenes of ethylene column cat head extraction or all smart ethene of extraction, not extraction ethene; Crude ethylene reclaims the low temperature cold more earlier through decompressor reclaim under reduced pressure energy or through expenditure and pressure, and the crude ethylene behind decompression and recovery cold loops back reactive system and further makes propylene, to improve the propylene selectivity; Enter demethanizing tower as absorption agent after all or part of cooling of ethane at the bottom of the tower;
(6) demethanizer column overhead is removed hydrogenation or is directly removed propylene tower, and by propylene tower cat head or side line extraction propylene, another component that propane all makes to do after byproduct output or all or part of cooling absorption agent at the bottom of the tower enters demethanizing tower; The C4+ component directly or through subsequent disposal rear section dereaction system is further made propylene at the bottom of the demethanizer, or directly does byproduct output after treatment;
Described demethanizing tower adopts ethane, propane or ethane/propane mixture to make absorption agent, and the absorption agent temperature is 5～-40 ℃.
2. the separation method of a kind of low-carbon alkene according to claim 1 is characterized in that, described preprocessing process is that process atmospheric pressures is reduced to 2.2～3.8MPa, is cooled to 5～-40 ℃, the removing of sour gas and oxygenatedchemicals, and the drying process of moisture.
3. the separation method of a kind of low-carbon alkene according to claim 1 is characterized in that, described depropanizing tower adopts single tower or high and low pressure double tower process flow process.
4. the separation method of a kind of low-carbon alkene according to claim 1 is characterized in that, deethanizer overhead adopts all or part of C2 to remove ethylene column, and all the other C2 loop back reactive system and further make propylene.
5. the separation method of a kind of low-carbon alkene according to claim 1, it is characterized in that, the all or part of smart ethene of ethylene column cat head or top side line extraction, part ethene loops back reactive system with the crude ethylene form from the side line extraction of ethylene column bottom and further makes propylene, to improve the propylene selectivity.
6. the separation method of a kind of low-carbon alkene according to claim 1, it is characterized in that, the crude ethylene of the C2 component of deethanizing cat head extraction and ethylene column cat head or side line extraction is earlier through decompressor reclaim under reduced pressure energy or through expenditure and pressure, reclaim the low temperature cold again, crude ethylene behind decompression and the recovery cold is looped back reactive system further make propylene, to improve the propylene selectivity.
7. the separation method of a kind of low-carbon alkene according to claim 1 is characterized in that, demethanizing tower top is provided with a side cooler, to reduce absorption agent consumption and overhead condenser refrigeration duty.
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| CN102351624B (en) * | 2011-08-24 | 2013-12-11 | 西安交通大学 | System for preparing low-carbon olefins by CO2 hydrogenation |
| 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 |
| CN103242123B (en) * | 2012-02-10 | 2015-09-23 | 中国石油化工股份有限公司 | A kind of separation method of low carbon olefin gas |
| CN103073379B (en) * | 2013-01-28 | 2016-02-10 | 神华集团有限责任公司 | Olefin separation and alkene separation method |
| CN104109070B (en) * | 2013-04-16 | 2016-12-28 | 中国石油化工股份有限公司 | The product separation method of preparing propylene from methanol |
| CN103626619B (en) * | 2013-12-02 | 2015-07-22 | 中国天辰工程有限公司 | Light hydrocarbon separation method used in methanol to olefin device |
| CN103787814B (en) * | 2014-01-23 | 2016-01-20 | 东华工程科技股份有限公司 | A kind of middle cold solvent of lower carbon number hydrocarbons washes separation method |
| CN106631664B (en) * | 2015-10-28 | 2019-06-28 | 中国石油化工股份有限公司 | A kind of separation method of methanol to olefins reaction gas |
| CN106631672B (en) * | 2015-10-28 | 2019-06-28 | 中国石油化工股份有限公司 | A kind of separation method of methanol to olefins reaction gas |
| CN110092701B (en) * | 2018-01-31 | 2023-08-15 | 中国寰球工程有限公司 | Light hydrocarbon separation method for MTO product mixed gas |
| CN108676579B (en) * | 2018-05-09 | 2023-04-25 | 天津市天地创智科技发展有限公司 | Dry gas sequential separation system and separation method based on argon circulation refrigeration |
| CN109456139B (en) * | 2018-12-10 | 2022-03-11 | 中石化上海工程有限公司 | Oil absorption separation method for reaction product of preparing ethylene from methane |
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