CN111116300A - Shallow cooling separation device and method for preparing olefin from synthesis gas - Google Patents
Shallow cooling separation device and method for preparing olefin from synthesis gas Download PDFInfo
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- CN111116300A CN111116300A CN201811275737.9A CN201811275737A CN111116300A CN 111116300 A CN111116300 A CN 111116300A CN 201811275737 A CN201811275737 A CN 201811275737A CN 111116300 A CN111116300 A CN 111116300A
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- 238000003786 synthesis reaction Methods 0.000 title claims abstract description 85
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- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 title claims abstract description 58
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- 239000005977 Ethylene Substances 0.000 claims abstract description 67
- 238000011084 recovery Methods 0.000 claims abstract description 64
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- 229910002092 carbon dioxide Inorganic materials 0.000 claims abstract description 59
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 41
- 239000001257 hydrogen Substances 0.000 claims abstract description 40
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- 238000006356 dehydrogenation reaction Methods 0.000 claims abstract description 29
- 238000005262 decarbonization Methods 0.000 claims abstract description 25
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 23
- 229930195733 hydrocarbon Natural products 0.000 claims description 101
- 150000002430 hydrocarbons Chemical class 0.000 claims description 98
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- 239000002250 absorbent Substances 0.000 claims description 53
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- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 claims description 50
- 229910052799 carbon Inorganic materials 0.000 claims description 43
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 37
- 238000001179 sorption measurement Methods 0.000 claims description 21
- -1 olefin hydrocarbon Chemical class 0.000 claims description 12
- 238000002360 preparation method Methods 0.000 claims description 12
- BVKZGUZCCUSVTD-UHFFFAOYSA-M Bicarbonate Chemical compound OC([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-M 0.000 claims description 7
- 238000010521 absorption reaction Methods 0.000 claims description 7
- 239000012528 membrane Substances 0.000 claims description 6
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- 238000004519 manufacturing process Methods 0.000 claims description 4
- 238000003795 desorption Methods 0.000 claims description 2
- 238000006243 chemical reaction Methods 0.000 abstract description 23
- 238000005265 energy consumption Methods 0.000 abstract description 16
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- 230000008901 benefit Effects 0.000 abstract description 7
- 238000011027 product recovery Methods 0.000 abstract description 4
- 239000000047 product Substances 0.000 description 127
- 230000000052 comparative effect Effects 0.000 description 34
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 14
- 150000002431 hydrogen Chemical class 0.000 description 13
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 12
- 238000005261 decarburization Methods 0.000 description 11
- 239000003054 catalyst Substances 0.000 description 9
- CRVGTESFCCXCTH-UHFFFAOYSA-N methyl diethanolamine Chemical compound OCCN(C)CCO CRVGTESFCCXCTH-UHFFFAOYSA-N 0.000 description 9
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 8
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 8
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 7
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- 239000003245 coal Substances 0.000 description 6
- 239000003208 petroleum Substances 0.000 description 5
- 239000002994 raw material Substances 0.000 description 5
- HZAXFHJVJLSVMW-UHFFFAOYSA-N 2-Aminoethan-1-ol Chemical compound NCCO HZAXFHJVJLSVMW-UHFFFAOYSA-N 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- 229910052742 iron Inorganic materials 0.000 description 4
- 239000000203 mixture Substances 0.000 description 4
- BWHMMNNQKKPAPP-UHFFFAOYSA-L potassium carbonate Chemical compound [K+].[K+].[O-]C([O-])=O BWHMMNNQKKPAPP-UHFFFAOYSA-L 0.000 description 4
- 229910000029 sodium carbonate Inorganic materials 0.000 description 4
- 239000000126 substance Substances 0.000 description 4
- 238000011161 development Methods 0.000 description 3
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- 238000010586 diagram Methods 0.000 description 3
- ZBCBWPMODOFKDW-UHFFFAOYSA-N diethanolamine Chemical compound OCCNCCO ZBCBWPMODOFKDW-UHFFFAOYSA-N 0.000 description 3
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- 238000000746 purification Methods 0.000 description 3
- 239000012264 purified product Substances 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 description 2
- 238000005336 cracking Methods 0.000 description 2
- 150000001993 dienes Chemical class 0.000 description 2
- LVTYICIALWPMFW-UHFFFAOYSA-N diisopropanolamine Chemical compound CC(O)CNCC(C)O LVTYICIALWPMFW-UHFFFAOYSA-N 0.000 description 2
- 229940043276 diisopropanolamine Drugs 0.000 description 2
- VUZPPFZMUPKLLV-UHFFFAOYSA-N methane;hydrate Chemical compound C.O VUZPPFZMUPKLLV-UHFFFAOYSA-N 0.000 description 2
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- PVXVWWANJIWJOO-UHFFFAOYSA-N 1-(1,3-benzodioxol-5-yl)-N-ethylpropan-2-amine Chemical compound CCNC(C)CC1=CC=C2OCOC2=C1 PVXVWWANJIWJOO-UHFFFAOYSA-N 0.000 description 1
- QMMZSJPSPRTHGB-UHFFFAOYSA-N MDEA Natural products CC(C)CCCCC=CCC=CC(O)=O QMMZSJPSPRTHGB-UHFFFAOYSA-N 0.000 description 1
- 229910021536 Zeolite Inorganic materials 0.000 description 1
- 239000006096 absorbing agent Substances 0.000 description 1
- VNWKTOKETHGBQD-YPZZEJLDSA-N carbane Chemical compound [10CH4] VNWKTOKETHGBQD-YPZZEJLDSA-N 0.000 description 1
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- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
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- 238000002309 gasification Methods 0.000 description 1
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- 238000005057 refrigeration Methods 0.000 description 1
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- 238000004088 simulation Methods 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 238000004230 steam cracking Methods 0.000 description 1
- 125000000383 tetramethylene group Chemical group [H]C([H])([*:1])C([H])([H])C([H])([H])C([H])([H])[*:2] 0.000 description 1
- 230000001131 transforming effect Effects 0.000 description 1
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/11—Purification; Separation; Use of additives by absorption, i.e. purification or separation of gaseous hydrocarbons with the aid of liquids
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/005—Processes comprising at least two steps in series
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/04—Purification; Separation; Use of additives by distillation
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/12—Purification; Separation; Use of additives by adsorption, i.e. purification or separation of hydrocarbons with the aid of solids, e.g. with ion-exchangers
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Water Supply & Treatment (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention relates to a shallow cooling separation device and a shallow cooling separation method for preparing olefin from synthesis gas, which mainly solve the problems that the subsequent separation process is influenced by a large amount of unconverted synthesis gas contained in product gas due to low conversion rate in the reaction process of preparing olefin from synthesis gas, the efficiency of equipment for removing carbon dioxide, carbon monoxide and hydrogen in the prior separation technology is low, and the prior separation technology needs cryogenic separation. The separation device comprises: 1) a depropanizer; 2) a decarbonization zone; 3) a dehydrogenation zone; 4) a heat exchange zone; 5) roughly dividing the tower; 6) the technical scheme of the ethylene recovery tower better solves the problems, can be used for the separation process of preparing olefin products from synthesis gas, and has the advantages of high equipment efficiency, high product recovery rate, high product purity and low energy consumption in the separation process.
Description
Technical Field
The invention relates to a shallow cooling separation device and a method for preparing olefin from synthesis gas, in particular to a separation device and a method for preparing olefin from synthesis gas by a one-step method.
Technical Field
Olefins, particularly ethylene, propylene and butylene, are important basic chemical raw materials, and the demand for them has been increasing in recent years. Generally, olefins are derived primarily from petroleum processing. With the increasing scarcity of petroleum resources, the cost of producing ethylene and propylene from petroleum resources is increasing, and the development of the technology for producing olefin from non-petroleum resources such as coal or natural gas and the like attracts more and more attention at home and abroad. The method for preparing low-carbon olefin by using coal, natural gas and the like as raw materials generally comprises the steps of converting the coal and the natural gas into synthesis gas and then preparing the low-carbon olefin from the synthesis gas. In the long run, the method has important strategic significance on the adjustment of energy structures in China and the reduction of dependence on petroleum resources.
The current mature technical route for preparing olefin from coal comprises four core technologies of coal gasification, synthesis gas purification, methanol synthesis and preparing olefin from methanol. Firstly, gasifying coal to prepare synthesis gas, then transforming the synthesis gas, purifying the transformed synthesis gas, finally preparing the purified synthesis gas into crude methanol and rectifying to finally produce qualified methanol. The main problems of coal-to-olefin are as follows: long technical route, large equipment quantity, large equipment investment, large raw material and energy consumption and high water consumption.
The direct preparation of olefin from synthesis gas avoids the synthesis and purification procedures of intermediate products, has shorter process route and reduces investment cost and operation cost. However, the process for directly preparing olefin from synthesis gas has not yet realized industrialized operation, and the main research is still focused on the development of the catalyst, but the research on the aspects of the development of the process flow, the design of the product separation scheme and the like is very deficient.
From the patent and literature methods, the direct preparation of olefins from synthesis gas is a Fischer-Tropsch (F-T) synthesis process, the product is distributed in a wide carbon number range, the product gas at the reaction outlet contains a large amount of unconverted synthesis gas, and the selectivity of low-carbon olefins is low, so that the separation difficulty is increased, and the improvement of economic benefit is greatly influenced.
CN 102666441 a discloses a supported iron-based catalyst for use in the production of lower olefins from synthesis gas by a process for producing lower olefins from a feed stream comprising carbon monoxide and hydrogen, for example by the Fischer-Tropsch (Fischer-Tropsch) process, at a temperature above 270 ℃ and not above 500 ℃, the iron-containing particles of the catalyst composition having an average particle size below 20m, preferably below 10 nm.
CN 102971277A discloses the production of light olefins such as C from synthesis gas using an iron based catalyst, the step of contacting the synthesis gas with the iron based catalyst at a temperature in the range of 250 to 350 ℃ and a pressure in the range of 10 to 40 bar (bar)2～4A process for producing olefins. H2 of syngas: the molar ratio of CO is in the range of 1.5 to 2.5.
CN 103664447A discloses a catalyst composition for preparing olefin from synthesis gas, which comprises CO and H with a molar ratio of 0.8-2.22The mixed gas is used as a raw material, and the reaction temperature is 250-350 ℃, the reaction pressure is 0.5-2.5 MPa, and the volume space velocity is 1000-4000 hours-1Under the condition of (1), the catalyst is in contact reaction with a catalyst to generate olefin, wherein the catalyst comprises the following components, by weight, 1-20 parts of a shell selected from one of ZSM-5 or β zeolite and 80-99 parts of an inner core.
CN108017481 discloses a separation method of a product gas for directly preparing low-carbon olefin from synthesis gas, which comprises the steps of cooling and drying the product gas of a reaction for directly preparing olefin from synthesis gas, and then feeding the cooled and dried product gas into a product gas purification unit to remove a carbon dioxide component in the product gas, so as to obtain a purified product gas; the purified product gas enters a synthesis gas primary recovery unit, and primary recovery is carried out on unconverted synthesis gas in the synthesis gas primary recovery unit; the product gas after primary recovery enters a synthesis gas secondary recovery unit for secondary recovery; the tower bottom material after secondary recovery enters a carbon dioxide and carbon three and heavy component separation unit to separate a carbon dioxide component from the carbon three and the heavy component; feeding the materials at the top of the tower of the carbon two and carbon three and heavy component separation unit into an ethylene rectification unit to obtain an ethylene product; the tower bottom material enters a carbon three and heavy component separation unit to separate carbon three components from carbon four and heavy components; and the tower top material of the carbon three and heavy component separation unit enters a propylene rectification unit to obtain a propylene product, and the tower bottom material enters a debutaning unit to obtain a carbon four product and a gasoline product. The method sends all the product gas into the carbon dioxide removing area, the dehydrogenation gas area and the carbon monoxide removing area, reduces the efficiency of the separation equipment, and increases the size and the investment of the equipment. In addition, after the high-temperature product gas is cooled, the high-temperature product gas is sent to a carbon dioxide removal area, a dehydrogenation gas area and a carbon monoxide removal area, and then the high-temperature product gas is sequentially separated, so that the energy loss is large. The method also needs to cool the pressure swing adsorption product gas to 125 ℃ below zero for cryogenic separation, needs to adopt ethylene refrigerant or binary refrigerant for cooling, needs to add an expensive set of refrigeration equipment for factories without ethylene steam cracking devices, and is not cost-effective in investment and land occupation.
In summary, in order to accelerate the industrialization process of directly preparing olefin from syngas, it is very necessary to provide a separation method with convenient operation and simple process, which can smoothly complete the separation of each component in the product gas at the outlet of the reaction for directly preparing olefin from syngas. Meanwhile, the composition distribution characteristics of each component in the product gas are considered, and a proper separation technology is selected to ensure the quality of the low-carbon olefin product.
The invention provides a separation method for preparing olefin from synthesis gas, which aims to solve the problems in a targeted manner.
Disclosure of Invention
The invention relates to a separation method for preparing olefin from synthesis gas, which mainly solves the problems that the subsequent separation process is influenced by a large amount of unconverted synthesis gas contained in product gas due to low conversion rate in the reaction process of preparing olefin from synthesis gas, the equipment efficiency of removing carbon dioxide, carbon monoxide and hydrogen in the prior separation technology is low, and cryogenic separation is needed in the prior separation technology.
In order to solve the above problems, the present invention provides a separation apparatus for producing olefins from synthesis gas, comprising:
1) a depropanizer; configured to receive a product gas stream, to discharge a light hydrocarbon stream overhead and a heavy hydrocarbon stream bottoms;
2) a decarbonization zone; configured to receive the light hydrocarbon stream, to emit a carbon dioxide stream and a decarbonated stream;
3) a dehydrogenation zone; configured to receive the decarbonated stream, discharge a recycle stream and a mixed hydrocarbon stream;
4) a heat exchange zone; configured to receive the mixed hydrocarbon stream and discharge a low temperature mixed hydrocarbon stream;
5) roughly dividing the tower; configured to receive the low temperature mixed hydrocarbon stream, an overhead discharge crude methane stream, a bottom discharge C2C3 component stream;
6) an ethylene recovery column: configured to receive the crude methane stream at a lower portion, an absorbent stream at an upper portion, a methane stream at an overhead portion, and a rich absorbent stream at a bottom portion of the column.
In the technical scheme of the invention, the separation device also comprises a product separation area; configured to receive the C2C3 component stream and discharge an olefin product.
In the technical scheme of the invention, the decarbonization zone comprises an absorption tower and a resolving tower.
In the technical scheme of the invention, the dehydrogenation zone comprises one or at least one of a pressure swing adsorption device, a temperature swing adsorption device and a membrane separation device.
In the technical scheme of the invention, the heat exchange area comprises a heat exchanger; it is preferable to use a heat exchanger containing propylene as a refrigerant.
In the technical scheme of the invention, the product separation zone comprises a deethanizer, an ethylene rectifying tower and a propylene rectifying tower.
In the technical scheme of the invention, the separation device also comprises an absorbent tower; configured to receive the heavy hydrocarbon stream, an overhead discharge absorbent stream, and a bottoms discharge gasoline product stream.
The invention also provides a separation method by using the separation device, which comprises the following steps:
a) separating the product gas stream by a depropanizing tower to obtain a light hydrocarbon stream containing three or less carbon components and a heavy hydrocarbon stream containing four or more carbon components;
b) separating the light hydrocarbon material flow into a carbon dioxide material flow mainly containing carbon dioxide components and a decarbonization material flow through a decarbonization area;
c) the decarbonized material flow is separated into a circulating material flow mainly containing carbon monoxide and hydrogen and a mixed hydrocarbon material flow through a dehydrogenation area;
d) the mixed hydrocarbon material flow is cooled in a heat exchange area to obtain a low-temperature mixed hydrocarbon material flow, and the low-temperature mixed hydrocarbon material flow is sent into a rough separation tower to be separated into a rough methane material flow mainly containing ethylene and methane and a C2C3 component material flow;
e) feeding the crude methane material flow into the lower part of an ethylene recovery tower, feeding the crude methane material flow into an absorbent material flow from the upper part of the ethylene recovery tower to be contacted in the tower, separating the tower top to obtain a methane material flow, obtaining a rich absorbent material flow rich in ethylene from the tower bottom, and returning the rich absorbent material flow to a depropanizer as a feed;
in the above technical solution, at least a part of the product gas stream comes from a reactor for preparing olefins from synthesis gas; optionally, at least part of the recycle stream obtained in step c) is returned to the synthesis gas to olefins reactor.
In the technical scheme, the heavy hydrocarbon material flow is sent into an absorbent tower to be separated to obtain a carbon-containing four-component absorbent material flow and a gasoline product material flow containing five or more carbon components. .
In the above technical scheme, at least part of the absorbent material flow is sent to the upper part of the ethylene recovery tower.
In another technical scheme of the invention, the heavy hydrocarbon material flow is separated by an absorbent tower to obtain a carbon-containing four-carbon six-component mixed carbon-four material flow and a carbon-containing seven-component or above carbon-containing seven-component material flow, at least part of the carbon-four material flow is used as the absorbent material flow and is sent to the upper part of an ethylene recovery tower to be used as an absorbent, at the same time, at least part of the mixed carbon-four material flow is sent to an olefin cracking device to crack olefin components into a crude propylene material flow mainly containing ethylene and propylene, and the crude propylene material flow is sent to a depropanizer to be used as a feed.
In the above technical solution, the product gas stream comprises carbon dioxide, carbon monoxide, hydrogen and mixed hydrocarbons.
In the above technical solution, preferably, the product gas stream contains, by weight, 10% to 40% of carbon dioxide, 1% to 5% of hydrogen, 30% to 70% of carbon monoxide, and 10% to 40% of mixed hydrocarbons.
In the above technical solution, preferably, the product gas stream contains 15% to 35% of carbon dioxide by weight percentage.
In the above technical solution, preferably, the mixed hydrocarbon stream contains at least 60% by weight of C2-C4 hydrocarbons.
In the above technical solution, more preferably, the mixed hydrocarbon stream contains at least 70% by weight of C2-C4 hydrocarbons.
In the above technical solution, most preferably, the mixed hydrocarbon stream contains at least 75% by weight of C2-C4 hydrocarbons.
In a technical solution of the present invention, at least 75% of the recycle stream is returned to the synthesis gas to olefins reactor.
In the technical scheme of the invention, preferably, at least 95% of the circulating stream is returned to the synthesis gas olefin preparation reactor.
In the technical scheme of the invention, more preferably, all the recycle stream is returned to the synthesis gas olefin preparation reactor.
In the technical scheme of the invention, the carbon dioxide is separated from the decarbonization zone by an absorption and desorption method.
In the technical scheme of the invention, the decarbonization area generates bicarbonate ions.
In the technical scheme of the invention, carbon monoxide or/and hydrogen is separated from the dehydrogenation zone by one or at least one of a pressure swing separation method, a temperature swing adsorption separation method and a membrane separation method.
In the technical scheme of the invention, the temperature of the low-temperature mixed hydrocarbon stream is lower than or equal to minus 15 ℃, preferably lower than or equal to minus 17 ℃.
In the technical scheme of the invention, the pressure of the low-temperature mixed hydrocarbon stream is greater than or equal to 2.4MPaG, preferably greater than or equal to 2.5 MPaG.
In the technical scheme of the invention, the C2C3 component stream is sequentially separated in a product separation zone to obtain an olefin product.
In the technical scheme of the invention, the decarbonized material flow mainly contains carbon monoxide, hydrogen, methane, ethylene, ethane, propylene and propane.
In the technical scheme of the invention, the mixed hydrocarbon stream mainly contains methane, ethylene, ethane, propylene and propane.
According to the technical scheme, when the carbon dioxide absorbent in the decarbonization region adopts potassium carbonate and sodium carbonate of the same series as the potassium carbonate as the absorbent, carbon dioxide is firstly hydrolyzed to generate hydrogen ions and bicarbonate ions, the hydrogen ions and the carbonate ions react to generate the bicarbonate ions, namely, carbon dioxide, water and carbonate react to generate bicarbonate, so that the effect of absorbing the carbon dioxide is achieved.
In another technical scheme of the invention, when the carbon dioxide absorbent in the decarbonization region adopts methyldiethanolamine and the ethanolamine, diethanolamine and diisopropanolamine which are the same series as the methyldiethanolamine as the absorbent, carbon dioxide is firstly hydrolyzed to generate hydrogen ions and bicarbonate ions, the hydrogen ions react with alcohol amine substances to generate protonated alcohol amine, namely, the carbon dioxide, water and the alcohol amine react to generate the bicarbonate ions and the protonated alcohol amine, so that the effect of absorbing the carbon dioxide is achieved.
The inventor considers that the energy is saved when the methyldiethanolamine and the ethanolamine, diethanolamine and diisopropanolamine in the same series are used as the absorbent through screening and simulation of the carbon dioxide absorbent in the decarbonization zone.
In the technical scheme of the invention, the C2C3 component stream is sequentially separated in a product separation zone to obtain an olefin product, namely the C2C3 component stream is sent to a deethanizer to obtain a C2 component and a C3 component, the C2 component is further separated in an ethylene separation tower to obtain an ethylene product, and the C3 component is further separated in a propylene separation tower to obtain a propylene product.
In the technical scheme of the invention, the temperature of the low-temperature mixed hydrocarbon needs to meet the condition of being lower than or equal to minus 15 ℃, the process requirements can be met only by adopting common propylene refrigerant, and the cryogenic cooling by adopting ethylene refrigerant is not needed, so that the investment is saved, the requirements on equipment materials are reduced on the other hand, and the safety is improved.
The technical scheme includes that after the product gas is properly cooled, heavy hydrocarbon material flow containing four or more carbon components is separated, then light hydrocarbon material flow containing three or less carbon components is sent to a decarbonization area and a dehydrogenation area to be subjected to carbon dioxide, carbon monoxide and hydrogen removal, the obtained mixed hydrocarbon material flow is sent to a heat exchange area to be cooled to obtain low-temperature mixed hydrocarbon material flow, and the obtained circulating material flow containing carbon monoxide and hydrogen is returned to a synthesis gas olefin preparation reactor. In the separation process of the technical scheme, the light hydrocarbon material flow is separated from the heavy hydrocarbon material flow by utilizing reaction heat, so that energy can be saved; only one part (light hydrocarbon material flow) in the product gas is sent to the decarbonization area and the dehydrogenation area, so that the utilization efficiency of equipment in the decarbonization area and the dehydrogenation area can be improved, the size of the equipment is reduced, and the investment cost is reduced; the recycle stream is returned to the reactor for preparing olefin from synthesis gas, so that the product yield is improved, the unit consumption of the device is reduced, and the device benefit is increased.
According to the technical scheme, by optimizing the separation process for preparing olefin from the synthesis gas, the heavy hydrocarbon material flow containing four or more carbon components and the light hydrocarbon material flow containing three or less carbon components are separated firstly, and are separated step by step according to a reasonable sequence through the serial connection of the optimized decarbonization area and the optimized dehydrogenation area, so that the unreacted raw materials are fully utilized, more diene products are obtained under the conditions of no need of cryogenic process conditions, low energy consumption, low investment and high efficiency, and a good technical effect is achieved; when the absorbent is preferred, the energy consumption can be further reduced, and a better technical effect can be achieved.
The technical scheme adopted by the invention is applied to the separation process for preparing olefin from synthesis gas, particularly the technology for preparing olefin from synthesis gas by a one-step method, has greater advantages in the aspects of yield of diolefin, material consumption, energy consumption, wastewater yield and investment progression compared with the existing coal chemical technology, and particularly has more obvious advantages in the preferred scheme of the technical scheme.
The embodiment and the comparative example show that the technical scheme adopted by the invention is applied to the separation process for preparing olefin from synthesis gas, compared with the comparative example technology, the separation process has the advantages of high carbon dioxide removal rate, high carbon monoxide and hydrogen recovery rate, high yield and high recovery rate of ethylene products and propylene products, solves the problems that the subsequent separation process is influenced by a large amount of unconverted synthesis gas contained in product gas due to low conversion rate in the reaction process for preparing olefin from synthesis gas, and the equipment efficiency of carbon dioxide, carbon monoxide and hydrogen removal in the existing cryogenic separation technology is low, and has the advantages of high equipment efficiency, high product recovery rate, high product purity and low energy consumption in the separation process.
All publications, patent applications, patents, and other references mentioned in this specification are herein incorporated by reference in their entirety. Unless defined otherwise, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art. In case of conflict, the present specification, including definitions, will control.
When the specification concludes with claims with the heading "known to those skilled in the art", "prior art", or the like, to derive materials, substances, methods, procedures, devices, or components, etc., it is intended that the subject matter derived from the heading encompass those conventionally used in the art at the time of filing this application, but also include those that are not currently in use, but would become known in the art to be suitable for a similar purpose.
In the context of the present specification, anything or things which are not mentioned, except where explicitly stated, are directly applicable to those known in the art without any changes. Moreover, any embodiment described herein may be freely combined with one or more other embodiments described herein, and the technical solutions or concepts resulting therefrom are considered part of the original disclosure or original disclosure of the invention, and should not be considered as new matters not disclosed or contemplated herein, unless a person skilled in the art would consider such a combination to be clearly unreasonable.
The present invention will be further illustrated by the following examples, but is not limited to these examples.
Drawings
FIG. 1 is a light cooling separation device for preparing olefin by synthesis gas.
FIG. 2 is a schematic flow diagram of a separation process according to the present invention.
FIG. 3 is a schematic flow diagram of a separation process described in a comparative example.
FIG. 1 depicts the following:
11 is a depropanizer
12 is a decarburization zone
13 is a dehydrogenation zone
14 is a heat exchange zone
15 is a rough separation tower
16 is an ethylene recovery column
In FIG. 1, a depropanizer column; configured to receive a product gas stream, to discharge a light hydrocarbon stream overhead and a heavy hydrocarbon stream bottoms; a decarbonization zone; configured to receive the light hydrocarbon stream, to emit a carbon dioxide stream and a decarbonated stream; a dehydrogenation zone; configured to receive the decarbonated stream, discharge a recycle stream and a mixed hydrocarbon stream; a heat exchange zone; configured to receive the mixed hydrocarbon stream and discharge a low temperature mixed hydrocarbon stream; roughly dividing the tower; configured to receive the low temperature mixed hydrocarbon stream, an overhead discharge crude methane stream, a bottom discharge C2C3 component stream; an ethylene recovery column: configured to receive the crude methane stream at a lower portion, an absorbent stream at an upper portion, a methane stream at an overhead portion, and a rich absorbent stream at a bottom portion
Fig. 2 is a schematic flow diagram of a separation method according to the present invention, and for comparison with a comparative example, the separation device shown in fig. 1 is further expanded and separated to obtain a full-flow separation method of ethylene products and propylene products.
FIG. 2 depicts the following:
101 product gas stream
102 is a light hydrocarbon stream (containing C3 and the following components)
103 is a heavy hydrocarbon stream (containing C4 and above)
104 is a carbon dioxide stream
105 is a decarbonated stream
106 is a recycle stream
107 is a mixed hydrocarbon stream
108 is a low temperature mixed hydrocarbon stream
109 is a crude methane stream
110 is a C2C3 component stream
111 is a methane stream
112 is a rich absorbent stream
113 is a C2 component stream
114 is a C3 component stream
115 is a propylene product stream
116 is a propane stream
117 is an ethylene product stream
118 is an ethane stream
119 is an absorbent stream
120 is an absorbent stream
121 is a gasoline product stream
11 is a depropanizer
12 is a decarburization zone
13 is a dehydrogenation zone
14 is a heat exchange zone
15 is a rough separation tower
16 is an ethylene recovery column
17 is a deethanizer
18 is a propylene separating column
19 is an ethylene separation column
20 is an absorbent tower
In fig. 2, a product gas stream 101 is separated by a depropanizer 11 to obtain a light hydrocarbon stream 102 containing three or less carbon components and a heavy hydrocarbon stream 103 containing four or more carbon components, the light hydrocarbon stream 102 is separated by a decarbonization zone 12 to obtain a carbon dioxide stream 104 mainly containing carbon dioxide components and a decarbonization stream 105, the decarbonization stream 105 is separated by a dehydrogenation zone 13 to obtain a recycle stream 106 mainly containing carbon monoxide and hydrogen and a mixed hydrocarbon stream 107, the mixed hydrocarbon stream 107 is cooled by a heat exchange zone 14 to obtain a low-temperature mixed hydrocarbon stream 108, and the low-temperature mixed hydrocarbon stream 108 is sent to a crude separation tower 15 to be separated to obtain a crude methane stream 109 mainly containing ethylene and methane and a C2C3 component stream 110; feeding the crude methane stream 109 into the lower part of an ethylene recovery tower 16, feeding the crude methane stream into an absorbent stream 120 from the upper part, contacting the crude methane stream with the absorbent stream in the tower, separating the methane stream 111 from the tower top, obtaining a rich absorbent stream 112 rich in ethylene from the tower bottom, returning the rich absorbent stream 112 to a depropanizer 11 as a feed, and returning at least part of a recycle stream 106 to a synthesis gas olefin preparation reactor; the C2C3 component stream 110 is sent to the deethanizer 17 to yield a C2 component stream 113 and a C3 component stream 114, the C2 component stream 113 is further separated in an ethylene splitter 19 to provide an ethylene product stream 117 and an ethane stream 118, and the C3 component stream is further separated in a propylene splitter 18 to provide a propylene product stream 115 and a propane stream 116. Heavy hydrocarbon stream 103 is separated in absorber 20 to produce absorbent streams 119, 120 and a gasoline product stream 121, absorbent stream 120 being returned to the upper portion of ethylene recovery column 16 as absorbent.
FIG. 3 illustrates in labeled form:
201 is product gas
202 is decarbonized product gas
203 is carbon dioxide
204 is unconverted synthesis gas
205 is pressure swing adsorption product gas
206 is the first unconverted synthesis gas and methane
207 is a second unconverted synthesis gas and methane
208 is an ethylene product
209 is an ethane product
210 is a propylene product
211 is a propane product
212 is a carbon four product
213 is a gasoline product.
21 is a dryer
22 is an absorption tower
23 is a regeneration tower
24 is a pressure swing adsorption device
25 is a carbon separation tank
26 is a demethanizer
27 is a deethanizer
28 is an ethylene rectifying tower
29 is a depropanizer
30 is a propylene rectifying tower
31 is a debutanizer.
In fig. 3, a product gas 201 enters a dryer 21 to remove a small amount of moisture, then enters an absorption tower 22 to perform mass transfer and heat transfer with an MDEA solvent, a carbon dioxide component in the gas is absorbed, then a carbon dioxide material stream 203 is released from the top of a regeneration tower 23, a purified product gas, namely a decarbonized product gas 202, is led out from the top of the absorption tower 22 and sent to a pressure swing adsorption device 24, the content of H2 and CO components in the product gas subjected to pressure swing adsorption is greatly reduced, the pressure swing adsorption product gas 205 is subjected to cryogenic cooling and then sent to a carbon-first separation tank 25 and a demethanizer 26 to separate unconverted synthesis gas and methane, and the remaining mixed hydrocarbons enter a deethanizer 27 to complete the separation of carbon dioxide, carbon three and heavy components. The materials at the top of the deethanizer 27 mainly comprise ethylene and a small amount of ethane, the materials are rectified and separated by the ethylene rectifying tower 28, a polymer-grade ethylene product 208 is obtained at the top of the tower, an ethane material flow is obtained at the bottom of the tower, the materials at the bottom of the deethanizer 27 mainly comprise carbon three and heavy components, the separation of the carbon three and the heavy components is completed by the depropanizer 29, the materials at the top of the depropanizer 29 mainly comprise propylene and a small amount of propane, the materials are rectified and separated by the propylene rectifying tower 30, a polymer-grade propylene product 210 is obtained at the top of the tower, and a propane material flow is obtained at the bottom of the tower; the tower bottom material composition of the depropanizing tower 29 is mainly carbon four and heavy components, and the separation of the carbon four and the heavy component gasoline is completed through the debutanizing tower 31 to obtain a carbon four product 212 and a gasoline product 213.
Detailed Description
By taking a product gas stream with the flow rate of 800000 kgh as a reference and adopting the technical scheme of the technology and the technical scheme of the comparative example, the mixed hydrocarbon material is cooled to below 15 ℃ below zero in the heat exchange zone of the technical scheme of the invention, and the product gas is cooled to below 100 ℃ below zero in the technical scheme of the comparative example, so that the carbon dioxide removal rate, the carbon monoxide and hydrogen recovery rate, the yield and recovery rate of the ethylene product and the propylene product, and the energy consumption are compared.
[ example 1 ]
The product stream obtained from the reaction zone comprises: 25.00 percent of carbon dioxide, 3.40 percent of hydrogen, 46.40 percent of carbon monoxide and 15.70 percent of mixed hydrocarbon, adopting the technical scheme shown in figure 2, adopting methyldiethanolamine as an absorbent in a decarburization area, adopting a pressure swing adsorption separation method in a dehydrogenation area, returning 76 percent of circulating material flow to a reactor for preparing olefin from synthesis gas, and separating to obtain an ethylene product and a propylene product.
The low temperature mixed hydrocarbon stream was at 29 deg.C below zero temperature and a pressure of 2.51 MPaG.
The carbon dioxide removal rate is 98.65%, the carbon monoxide recovery rate is 98.99%, the hydrogen recovery rate is 98.19%, the ethylene product yield is 2.63% higher than that of the technical scheme of the comparative example, the recovery rate is 97.29%, the propylene product yield is 2.68% higher than that of the technical scheme of the comparative example, the recovery rate is 99.84%, and the energy consumption is 1.90% lower than that of the technical scheme of the comparative example.
[ example 2 ]
The product stream obtained from the reaction zone comprises: 25.00 percent of carbon dioxide, 3.40 percent of hydrogen, 46.40 percent of carbon monoxide and 15.70 percent of mixed hydrocarbon, adopting the technical scheme shown in figure 2, adopting methyldiethanolamine as an absorbent in a decarburization area, adopting a pressure swing adsorption separation method in a dehydrogenation area, returning 86 percent of circulating material flow to a reactor for preparing olefin from synthesis gas, and separating to obtain an ethylene product and a propylene product.
The low temperature mixed hydrocarbon stream was at 26 ℃ below zero and a pressure of 2.60 MPaG.
The carbon dioxide removal rate is 98.64 percent, the carbon monoxide recovery rate is 98.98 percent, the hydrogen recovery rate is 98.18 percent, the ethylene product yield is 2.97 percent higher than that of the technical scheme of the comparative example, the recovery rate is 97.39 percent, the propylene product yield is 3.03 percent higher than that of the technical scheme of the comparative example, the recovery rate is 99.87 percent, and the energy consumption is 1.89 percent less than that of the technical scheme of the comparative example.
[ example 3 ]
The product stream obtained from the reaction zone comprises: 25.00 percent of carbon dioxide, 3.40 percent of hydrogen, 46.40 percent of carbon monoxide and 15.70 percent of mixed hydrocarbon, adopting the technical scheme shown in figure 2, adopting methyldiethanolamine as an absorbent in a decarburization area, adopting a pressure swing adsorption separation method in a dehydrogenation area, returning 96 percent of circulating material flow to a reactor for preparing olefin from synthesis gas, and separating to obtain an ethylene product and a propylene product.
The low temperature mixed hydrocarbon stream has a temperature of-23 deg.C and a pressure of 2.70 MPaG.
The carbon dioxide removal rate is 98.63%, the carbon monoxide recovery rate is 98.97%, the hydrogen recovery rate is 98.17%, the ethylene product yield is 3.32% higher than that of the technical scheme of the comparative example, the recovery rate is 97.49%, the propylene product yield is 3.38% higher than that of the technical scheme of the comparative example, the recovery rate is 99.90%, and the energy consumption is 1.88% lower than that of the technical scheme of the comparative example.
[ example 4 ]
The product stream obtained from the reaction zone comprises: 25.00 percent of carbon dioxide, 3.40 percent of hydrogen, 46.40 percent of carbon monoxide and 15.70 percent of mixed hydrocarbon, adopting the technical scheme shown in figure 2, adopting methyldiethanolamine as an absorbent in a decarburization area, adopting a pressure swing adsorption separation method in a dehydrogenation area, returning all circulating material flows to a reactor for preparing olefin from synthesis gas, and separating to obtain an ethylene product and a propylene product.
The low temperature mixed hydrocarbon stream was at 20 deg.C below zero and a pressure of 2.8 MPaG.
The carbon dioxide removal rate is 98.61%, the carbon monoxide recovery rate is 98.96%, the hydrogen recovery rate is 98.16%, the ethylene product yield is 3.46% higher than that of the technical scheme of the comparative example, the recovery rate is 97.59%, the propylene product yield is 3.53% higher than that of the technical scheme of the comparative example, the recovery rate is 99.93%, and the energy consumption is 1.87% lower than that of the technical scheme of the comparative example.
[ example 5 ]
The product stream obtained from the reaction zone comprises: 20.00 percent of carbon dioxide, 3.05 percent of hydrogen, 40.35 percent of carbon monoxide and 27.1 percent of mixed hydrocarbon, adopting the technical scheme shown in figure 2, adopting methyldiethanolamine as an absorbent in a decarburization area, adopting a pressure swing adsorption separation method in a dehydrogenation area, returning all circulating material flows to a reactor for preparing olefin from synthesis gas, and separating to obtain an ethylene product and a propylene product.
The low temperature mixed hydrocarbon stream was 17.5 deg.C at-zero and a pressure of 2.9 MPaG.
The carbon dioxide removal rate is 98.61%, the carbon monoxide recovery rate is 98.97%, the hydrogen recovery rate is 98.17%, the ethylene product yield is 5.97% higher than that of the technical scheme of the comparative example, the recovery rate is 97.59%, the propylene product yield is 6.09% higher than that of the technical scheme of the comparative example, the recovery rate is 99.93%, and the energy consumption is 1.91% lower than that of the technical scheme of the comparative example.
[ example 6 ]
The product stream obtained from the reaction zone comprises: 20.00 percent of carbon dioxide, 3.05 percent of hydrogen, 40.35 percent of carbon monoxide and 27.1 percent of mixed hydrocarbon, adopting the technical scheme shown in figure 2, adopting diethanolamine as an absorbent in a decarburization area, adopting a pressure swing adsorption separation method in a dehydrogenation area, returning all circulating material flows to a reactor for preparing olefin from synthesis gas, and separating to obtain an ethylene product and a propylene product.
The low temperature mixed hydrocarbon stream was 17.5 deg.C at-zero and a pressure of 2.9 MPaG.
The carbon dioxide removal rate is 98.61%, the carbon monoxide recovery rate is 98.97%, the hydrogen recovery rate is 98.17%, the ethylene product yield is 5.97% higher than that of the technical scheme of the comparative example, the recovery rate is 97.59%, the propylene product yield is 6.09% higher than that of the technical scheme of the comparative example, the recovery rate is 99.93%, and the energy consumption is 1.91% lower than that of the technical scheme of the comparative example.
[ example 7 ]
The product stream obtained from the reaction zone comprises: 20.00 percent of carbon dioxide, 3.05 percent of hydrogen, 40.35 percent of carbon monoxide and 27.1 percent of mixed hydrocarbon, adopting the technical scheme shown in figure 2, adopting sodium carbonate as an absorbent in a decarburization area, adopting a temperature swing adsorption separation method in a dehydrogenation area, returning all circulating material flows to a synthesis gas olefin preparation reactor, and separating to obtain an ethylene product and a propylene product.
The low temperature mixed hydrocarbon stream was 17.5 deg.C at-zero and a pressure of 2.9 MPaG.
The carbon dioxide removal rate is 98.59 percent, the carbon monoxide recovery rate is 98.97 percent, the hydrogen recovery rate is 98.17 percent, the ethylene product yield is 5.97 percent higher than that of the technical scheme of the comparative example, the recovery rate is 97.59 percent, the propylene product yield is 6.09 percent higher than that of the technical scheme of the comparative example, the recovery rate is 99.93 percent, and the energy consumption is 1.89 percent less than that of the technical scheme of the comparative example.
[ example 8 ]
The product stream obtained from the reaction zone comprises: 20.00 percent of carbon dioxide, 3.05 percent of hydrogen, 40.35 percent of carbon monoxide and 27.1 percent of mixed hydrocarbon, adopting the technical scheme shown in figure 2, adopting sodium carbonate as an absorbent in a decarburization area, adopting a membrane separation method in a dehydrogenation area, returning all the circulating material flow to a reactor for preparing olefin from synthesis gas, and separating to obtain an ethylene product and a propylene product.
The low temperature mixed hydrocarbon stream was 17.5 deg.C at-zero and a pressure of 2.9 MPaG.
The carbon dioxide removal rate is 98.59 percent, the carbon monoxide recovery rate is 98.98 percent, the hydrogen recovery rate is 98.16 percent, the ethylene product yield is 5.97 percent higher than that of the technical scheme of the comparative example, the recovery rate is 97.59 percent, the propylene product yield is 6.09 percent higher than that of the technical scheme of the comparative example, the recovery rate is 99.93 percent, and the energy consumption is 1.90 percent less than that of the technical scheme of the comparative example.
[ example 9 ]
The product stream obtained from the reaction zone comprises: 20.00 percent of carbon dioxide, 3.05 percent of hydrogen, 40.35 percent of carbon monoxide and 27.1 percent of mixed hydrocarbon, adopting the technical scheme of figure 1, and the difference is that in another technical scheme of the invention, a heavy hydrocarbon stream is separated by a dehexanizer to obtain a mixed C-IV stream containing four to six carbon components and a C-VII stream containing seven or more carbon components, the C-IV stream can be sent to an olefin cracking device to crack olefin components into a crude propylene stream mainly containing ethylene and propylene, and the crude propylene stream is sent to a depropanizer as a feed. The decarbonization zone adopts sodium carbonate as an absorbent, the dehydrogenation zone adopts a membrane separation method, all the circulating material flow returns to a synthesis gas olefin preparation reactor, and ethylene products and propylene products are obtained through separation.
The low temperature mixed hydrocarbon stream was 17.5 deg.C at-zero and a pressure of 2.9 MPaG.
The carbon dioxide removal rate is 98.59 percent, the carbon monoxide recovery rate is 98.98 percent, the hydrogen recovery rate is 98.16 percent, the ethylene product yield is 9.88 percent higher than that of the technical scheme of the comparative example, the recovery rate is 97.59 percent, the propylene product yield is 10.02 percent higher than that of the technical scheme of the comparative example, the recovery rate is 99.93 percent, and the energy consumption is 2.58 percent less than that of the technical scheme of the comparative example.
[ COMPARATIVE EXAMPLE 1 ]
The product stream obtained from the reaction zone comprises: 25.00 percent of carbon dioxide, 3.40 percent of hydrogen, 46.40 percent of carbon monoxide and 15.70 percent of mixed hydrocarbon, adopting the technical scheme shown in figure 3, adopting methyldiethanolamine as an absorbent in a decarburization area, adopting a pressure swing adsorption separation method in a dehydrogenation area, returning all circulating material flows to a reactor for preparing olefin from synthesis gas, and separating to obtain an ethylene product and a propylene product.
The low temperature mixed hydrocarbon stream was 125 deg.C below zero and at a pressure of 3.5 MPaG.
The carbon dioxide removal rate is 98.40%, the carbon monoxide recovery rate is 98.60%, the hydrogen recovery rate is 98.00%, the ethylene product recovery rate is 97.2%, and the propylene product recovery rate is 99.80%.
Claims (17)
1. A shallow cold separation unit for producing olefins from synthesis gas, comprising:
1) a depropanizer; configured to receive a product gas stream, to discharge a light hydrocarbon stream overhead and a heavy hydrocarbon stream bottoms;
2) a decarbonization zone; configured to receive the light hydrocarbon stream, to emit a carbon dioxide stream and a decarbonated stream;
3) a dehydrogenation zone; configured to receive the decarbonated stream, discharge a recycle stream and a mixed hydrocarbon stream;
4) a heat exchange zone; configured to receive the mixed hydrocarbon stream and discharge a low temperature mixed hydrocarbon stream;
5) roughly dividing the tower; configured to receive the low temperature mixed hydrocarbon stream, an overhead discharge crude methane stream, a bottom discharge C2C3 component stream;
6) an ethylene recovery column: configured to receive the crude methane stream at a lower portion, an absorbent stream at an upper portion, a methane stream at an overhead portion, and a rich absorbent stream at a bottom portion of the column.
2. The separation device for the preparation of olefins from synthesis gas according to claim 1, characterized in that the separation device further comprises a product separation zone; configured to receive the C2C3 component stream and discharge an olefin product.
3. The separation plant for the preparation of olefins from synthesis gas according to claim 1, characterized in that the decarbonization section comprises an absorption column and a stripper column.
4. The separation device for producing olefin from synthesis gas according to claim 1, characterized in that the dehydrogenation zone comprises one or at least one of a pressure swing adsorption device, a temperature swing adsorption device, and a membrane separation device.
5. The separation unit for synthesis gas to olefins according to claim 1, characterized in that the heat exchange zone comprises a heat exchanger; it is preferable to use a heat exchanger containing propylene as a refrigerant.
6. The separation plant for the preparation of olefins from synthesis gas according to claim 2, characterized in that the product separation zone comprises a deethanizer, an ethylene rectifier and a propylene rectifier.
7. The separation unit for the synthesis gas to olefins according to claim 1, characterized in that the separation unit further comprises an absorbent column; configured to receive the heavy hydrocarbon stream, an overhead discharge absorbent stream, and a bottoms discharge gasoline product stream.
8. A shallow cooling separation method for preparing olefin by synthesis gas comprises the following steps:
a) separating the product gas stream by a depropanizing tower to obtain a light hydrocarbon stream containing three or less carbon components and a heavy hydrocarbon stream containing four or more carbon components;
b) separating the light hydrocarbon material flow into a carbon dioxide material flow mainly containing carbon dioxide components and a decarbonization material flow through a decarbonization area;
c) the decarbonized material flow is separated into a circulating material flow mainly containing carbon monoxide and hydrogen and a mixed hydrocarbon material flow through a dehydrogenation area;
d) the mixed hydrocarbon material flow is cooled in a heat exchange area to obtain a low-temperature mixed hydrocarbon material flow, and the low-temperature mixed hydrocarbon material flow is sent into a rough separation tower to be separated into a rough methane material flow mainly containing ethylene and methane and a C2C3 component material flow;
e) and feeding the crude methane material flow into the lower part of an ethylene recovery tower, feeding the crude methane material flow into an absorbent material flow from the upper part of the ethylene recovery tower to be contacted in the tower, separating the tower top to obtain a methane material flow, obtaining a rich absorbent material flow rich in ethylene from the tower bottom, and returning the rich absorbent material flow to a depropanizer as a feed.
9. The separation process for synthesis gas to olefins according to claim 8, characterized in that the product gas stream is at least partially derived from a synthesis gas to olefins reactor; optionally, at least part of the recycle stream obtained in step c) is returned to the synthesis gas to olefins reactor.
10. The separation method for preparing olefin hydrocarbon by synthesis gas according to claim 8, characterized in that the heavy hydrocarbon stream is sent to an absorbent tower to be separated to obtain a carbon-containing four-component absorbent stream and a carbon-containing five-component and above gasoline product stream.
11. The separation process for olefins from synthesis gas according to claim 8, characterized in that at least part of the absorbent stream is sent to the upper part of the ethylene recovery column.
12. The separation process for olefins production from synthesis gas according to claim 8, characterized in that the carbon dioxide is separated by absorption and desorption in the decarbonization zone.
13. A separation process for olefins from synthesis gas according to claim 8, characterized in that the decarbonization zone has the formation of bicarbonate ions.
14. The separation process for olefins from synthesis gas according to claim 8, wherein carbon monoxide and/or hydrogen is separated in the dehydrogenation zone by one or at least one of a pressure swing adsorption separation process, a temperature swing adsorption separation process and a membrane separation process.
15. The separation process for the preparation of olefins from synthesis gas according to claim 8, characterized in that the low temperature mixed hydrocarbon stream has a temperature of-15 ℃ or lower, preferably-17 ℃ or lower.
16. The separation process for the production of olefins from synthesis gas according to claim 8, characterized in that the pressure of the low temperature mixed hydrocarbon stream is equal to or higher than 2.4MPaG, preferably equal to or higher than 2.5 MPaG.
17. The separation process for preparing olefin hydrocarbon from synthesis gas as claimed in claim 8, wherein the C2C3 component stream is subsequently separated in the product separation zone to obtain olefin hydrocarbon product.
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Application publication date: 20200508 |