CN212425918U - Utilize low temperature methanol to wash processing membrane separation non-permeate gas system methanol system and including its methanol production system - Google Patents
Utilize low temperature methanol to wash processing membrane separation non-permeate gas system methanol system and including its methanol production system Download PDFInfo
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- CN212425918U CN212425918U CN202020217470.4U CN202020217470U CN212425918U CN 212425918 U CN212425918 U CN 212425918U CN 202020217470 U CN202020217470 U CN 202020217470U CN 212425918 U CN212425918 U CN 212425918U
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- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 title claims abstract description 686
- 239000012528 membrane Substances 0.000 title claims abstract description 40
- 238000000926 separation method Methods 0.000 title claims abstract description 31
- 239000012466 permeate Substances 0.000 title claims abstract description 28
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 19
- 230000015572 biosynthetic process Effects 0.000 claims abstract description 64
- 238000003786 synthesis reaction Methods 0.000 claims abstract description 64
- 238000005406 washing Methods 0.000 claims abstract description 30
- 239000007788 liquid Substances 0.000 claims abstract description 10
- 239000007789 gas Substances 0.000 claims description 152
- 238000010521 absorption reaction Methods 0.000 claims description 23
- 238000006243 chemical reaction Methods 0.000 claims description 14
- 239000000446 fuel Substances 0.000 claims description 9
- 238000000746 purification Methods 0.000 claims description 8
- 239000003245 coal Substances 0.000 claims description 7
- 239000000571 coke Substances 0.000 claims description 7
- 238000010926 purge Methods 0.000 claims description 6
- 239000000567 combustion gas Substances 0.000 claims description 3
- 238000005201 scrubbing Methods 0.000 claims 1
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 abstract description 42
- 229910002092 carbon dioxide Inorganic materials 0.000 abstract description 23
- 239000001569 carbon dioxide Substances 0.000 abstract description 21
- 229910052799 carbon Inorganic materials 0.000 abstract description 19
- 239000006227 byproduct Substances 0.000 abstract description 10
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 abstract description 7
- 230000008901 benefit Effects 0.000 abstract description 6
- 230000007613 environmental effect Effects 0.000 abstract description 2
- 230000004308 accommodation Effects 0.000 abstract 1
- 229910052739 hydrogen Inorganic materials 0.000 description 9
- 239000001257 hydrogen Substances 0.000 description 9
- 229910002091 carbon monoxide Inorganic materials 0.000 description 6
- 239000002737 fuel gas Substances 0.000 description 6
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 5
- 238000000034 method Methods 0.000 description 5
- 238000002360 preparation method Methods 0.000 description 5
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 4
- 239000002994 raw material Substances 0.000 description 4
- 230000008929 regeneration Effects 0.000 description 4
- 238000011069 regeneration method Methods 0.000 description 4
- 239000003054 catalyst Substances 0.000 description 3
- 150000002431 hydrogen Chemical class 0.000 description 3
- 229920006395 saturated elastomer Polymers 0.000 description 3
- 239000007795 chemical reaction product Substances 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000001704 evaporation Methods 0.000 description 2
- 230000008020 evaporation Effects 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 1
- 230000003044 adaptive effect Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 229910052802 copper Inorganic materials 0.000 description 1
- 239000010949 copper Substances 0.000 description 1
- 230000006837 decompression Effects 0.000 description 1
- 238000010828 elution Methods 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 230000008595 infiltration Effects 0.000 description 1
- 238000001764 infiltration Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 230000002194 synthesizing effect Effects 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
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- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The utility model discloses an utilize low temperature methyl alcohol to wash processing membrane separation non-permeate gas system methyl alcohol system and including its methyl alcohol production system, include that newly-increased low temperature methyl alcohol washes unit and newly-increased methyl alcohol synthesis unit in original methyl alcohol synthesizer. The non-permeable gas discharged from the original methanol synthesis device and coming out of the membrane separation unit enters a newly-added low-temperature methanol washing unit, part of carbon dioxide in the non-permeable gas is removed by using low-temperature methanol liquid in the existing low-temperature methanol washing system, the hydrogen-carbon ratio is improved, the gas after carbon dioxide removal is synthesis gas, and the hydrogen-carbon ratio meets the requirements of methanol synthesis, and then the synthesis gas enters the newly-added methanol synthesis unit to synthesize methanol. The utility model discloses with methyl alcohol speed out non-permeate gas of gas membrane separation and turn into methyl alcohol, the by-product steam reduces carbon emission simultaneously, energy saving and consumption reduction has fine economic benefits and environmental protection benefit to can realize that methyl alcohol washes the hydrogen-carbon ratio in the non-permeate gas and adjust in a flexible way, enlarged the accommodation of device to non-permeate gas nature.
Description
Technical Field
The utility model belongs to the technical field of the methyl alcohol preparation, concretely relates to non-permeate gas and coal or coke oven gas system methyl alcohol production system are washed to low temperature methyl alcohol.
Background
The preparation of methanol by using synthesis gas is a main device for preparing methanol by using coal or coke oven gas at present. In the prior art, the preparation of methanol from synthesis gas mainly comprises units such as low-temperature methanol washing, methanol reaction synthesis, purification and the like. The raw material gas is purified by low-temperature methanol in the low-temperature methanol washing unit, the methanol can be regenerated and circulated, the purified raw material gas is synthesized into methanol by the methanol reaction synthesis unit under the condition of a catalyst, and the crude methanol is purified by the purification unit by adopting the combination of flash evaporation, rectification and the like. Most of methanol purge gas of a device for preparing methanol from synthesis gas in the prior art adopts membrane separation to recover hydrogen, the recovered hydrogen returns to a methanol synthesis system, and membrane separation non-permeable gas cannot be directly used for preparing methanol because the hydrogen-carbon ratio is usually lower than 1.5 and is all sent to be used as fuel. The non-permeable gas contains a large amount of carbon monoxide and carbon dioxide, and also contains hydrogen, the non-permeable gas pressure is high, and the direct decompression as fuel wastes resources.
SUMMERY OF THE UTILITY MODEL
In order to solve the problem, the utility model aims to provide a non-permeate gas and coal or coke oven gas system methanol production system are washed to low temperature methyl alcohol, wash through low temperature methyl alcohol and handle further preparation methyl alcohol after membrane separation non-permeate gas prepares the synthetic gas again, improve resource utilization.
The utility model discloses a following technical scheme:
a system for preparing methanol from non-permeable gas by utilizing low-temperature methanol washing processing membrane separation, which is taken as an auxiliary device of a main device for preparing methanol from synthesis gas, comprises:
the low-temperature methanol washing unit comprises a first heat exchanger and an absorption tower filled with low-temperature methanol, wherein a heat source inlet of the first heat exchanger is connected with a non-permeation gas inlet pipeline, a heat source outlet is connected with a gas inlet of the absorption tower, and a gas outlet of the absorption tower is connected with a cold source inlet of the first heat exchanger;
the methanol synthesis unit comprises a second heat exchanger, a methanol synthesis tower, a cooler and a methanol separator, wherein a cold source outlet of the first heat exchanger is connected with a cold source inlet of the second heat exchanger, a cold source outlet of the second heat exchanger is connected with a reaction inlet of the methanol synthesis tower, a reaction outlet of the methanol synthesis tower is connected with a heat source inlet of the second heat exchanger, a heat source outlet of the second heat exchanger is sequentially connected with the cooler and the methanol separator, and the methanol separator comprises a crude methanol discharge port and a tail gas discharge port.
According to the utility model discloses an utilize low temperature methyl alcohol to wash a concrete scheme of processing membrane separation non-permeate gas system methyl alcohol system, exhaust port sets up two strands of reposition of redundant personnel pipelines, and one of them reposition of redundant personnel pipeline reposition of redundant personnel partial tail gas sends into the fuel pipe network as combustion gas, and another reposition of redundant personnel pipeline reposition of redundant personnel surplus tail gas joins back with the cold source entry pipeline of second heat exchanger after letting in the compressor and joins.
According to the utility model discloses an utilize low temperature methyl alcohol to wash a concrete scheme of processing membrane separation non-permeate gas system methyl alcohol system, the methyl alcohol synthetic tower is connected with the steam pocket, with the heat with steam recovery that produces in the methyl alcohol synthesis.
According to the utility model discloses an utilize low temperature methyl alcohol to wash a concrete scheme of processing membrane separation non-permeate gas system methyl alcohol system, non-permeate gas pipeline divide into two strands of feeding branches through the shunt, and one of them feeding branch is connected with the heat source entry of first heat exchanger, and another feeding branch joins to the cold source outlet line of first heat exchanger. The hydrogen-carbon ratio (hydrogen content-carbon dioxide content)/(carbon dioxide content + carbon monoxide content)) of the synthesis gas after the low-temperature methanol elution unit removes carbon dioxide from the non-permeable gas needs to meet the requirement of the hydrogen-carbon ratio of the synthesis gas in methanol synthesis (usually more than or equal to 2). The amount of carbon dioxide in the non-permeable gas separated from the membrane by the low-temperature methanol eluting unit is determined according to the hydrogen-carbon ratio of the non-permeable gas and the flow rate of the non-permeable gas, when the hydrogen-carbon ratio of the non-permeable gas is smaller, the flow rate of the non-permeable gas is larger, the amount of carbon dioxide required to be separated from the low-temperature methanol eluting unit is larger, and vice versa. The hydrogen-to-carbon ratio of the synthesis gas can be realized by changing the flow dividing rate of the two feeding branches.
According to the utility model discloses an utilize low temperature methyl alcohol to wash a concrete scheme of processing membrane separation non-permeate gas system methyl alcohol system, the absorption tower leakage fluid dram is connected to the low temperature methyl alcohol system of synthetic gas system methyl alcohol main part and washes the system for the low temperature methyl alcohol liquid regeneration that will contain the carbon dioxide of deviating from.
According to the utility model discloses an utilize low temperature methyl alcohol to wash a concrete scheme of processing membrane separation non-permeate gas system methyl alcohol system, the purification unit of synthetic gas system methyl alcohol main device is connected to methanol separator's thick methyl alcohol discharge port, improves the purity with thick methyl alcohol.
The utility model discloses still include a coal or coke oven gas system methyl alcohol production system, including first methyl alcohol production system and second methyl alcohol production system, first methyl alcohol production system is synthetic gas system methyl alcohol main device, and the membrane separator is connected to the methanol relief gas of its production, and the membrane separation non-permeate gas that membrane separator produced links second methyl alcohol production system, and second methyl alcohol production system is aforementioned utilize low temperature methyl alcohol to wash the non-permeate gas system methyl alcohol system of processing membrane separation.
Since the technical scheme is used, the utility model discloses following beneficial effect has:
1. the low-temperature methanol washing unit and the methanol synthesis unit are newly added, the device is subjected to adaptive matching improvement, and the membrane separation non-permeate gas can be purified and then further synthesized into methanol, so that the methanol yield of the original methanol device can be increased, the contents of carbon monoxide and carbon dioxide in the non-permeate gas can be reduced, the carbon emission generated by combustion of the non-permeate gas can be reduced, and the economic benefit and the environmental protection benefit of the original methanol device can be increased;
2. the newly added low-temperature methanol washing unit and the methanol synthesis unit are combined with a synthesis gas methanol preparation system in the prior art, the systems such as low-temperature methanol cycle regeneration of the newly added low-temperature methanol washing unit and the like are supported by the existing low-temperature methanol washing system, the crude methanol treatment is supported by the existing methanol purification system, the investment cost of the whole device is reduced, the function of the existing device is fully exerted, and the economic benefit is further improved;
3. by optimizing the feeding process, the flexible adjustment of the hydrogen-carbon ratio in the non-permeable gas after methanol washing can be realized, the application range of the device to the properties of the non-permeable gas is expanded, and the conversion efficiency of finally synthesizing methanol is ensured.
Drawings
In order to more clearly illustrate the technical solution of the mode of the invention, the drawings that are required to be used in the embodiment are briefly described below, it should be understood that the following drawings only illustrate some embodiments of the invention, and are not to be considered as limiting the scope, and that for a person skilled in the art, other relevant drawings can be obtained from these drawings without inventive effort.
FIG. 1 is a schematic diagram of the apparatus of the membrane separation of non-permeate gas to methanol system of the low temperature methanol wash process of example 1;
FIG. 2 is a schematic diagram of the apparatus of the membrane separation of non-permeate gas to methanol system of the low temperature methanol wash process of example 2;
in the figure: 1 is a first heat exchanger, 2 is an absorption tower, 3 is an impermeable gas inlet pipeline, 4 is a second heat exchanger, 5 is a methanol synthesis tower, 6 is a cooler, 7 is a methanol separator, 8 is a steam drum, and 9 is a compressor.
Detailed Description
To make the objects, technical solutions and advantages of the embodiments of the present invention clearer, the drawings of the embodiments of the present invention are combined to clearly and completely describe the technical solutions of the embodiments of the present invention, and obviously, the described embodiments are some embodiments of the present invention, not all embodiments. Based on the embodiments in the present invention, all other embodiments obtained by a person skilled in the art without creative work belong to the protection scope of the present invention. Thus, the following detailed description of the embodiments of the present invention, presented in the accompanying drawings, is not intended to limit the scope of the invention, as claimed, but is merely representative of selected embodiments of the invention. Based on the embodiments in the present invention, all other embodiments obtained by a person skilled in the art without creative work belong to the protection scope of the present invention.
In the description of the present invention, it is to be understood that the terms indicating orientation or positional relationship are based on the orientation or positional relationship shown in the drawings, and are only for convenience of description and simplification of description, and do not indicate or imply that the equipment or elements referred to must have a specific orientation, be constructed and operated in a specific orientation, and thus, should not be construed as limiting the present invention.
In the present invention, unless otherwise expressly stated or limited, the terms "mounted," "connected," and "fixed" are to be construed broadly and may, for example, be fixedly connected, detachably connected, or integrally formed; either directly or indirectly through intervening media, either internally or in any other relationship. The specific meaning of the above terms in the present invention can be understood according to specific situations by those skilled in the art.
In the present disclosure, unless otherwise expressly stated or limited, the first feature may comprise both the first and second features directly contacting each other, and also may comprise the first and second features not being directly contacting each other but being in contact with each other by means of further features between them. Also, the first feature being above, on or above the second feature includes the first feature being directly above and obliquely above the second feature, or merely means that the first feature is at a higher level than the second feature. A first feature that underlies, and underlies a second feature includes a first feature that is directly under and obliquely under a second feature, or simply means that the first feature is at a lesser level than the second feature.
Example 1
As shown in figure 1, a production system for preparing methanol from low-temperature methanol-washing non-permeable gas and coal or coke oven gas is used as an auxiliary device of a main device for preparing methanol from synthesis gas, namely a raw methanol device, and the utility model discloses still include the system for preparing methanol from coal or coke oven gas that combines the system for preparing methanol from low-temperature methanol-washing processing membrane separation non-permeable gas and the raw methanol device. The original methanol device mainly comprises units of low-temperature methanol washing, methanol reaction synthesis, purification and the like as the prior art. The raw material gas is purified by low-temperature methanol in the low-temperature methanol washing unit, the methanol can be regenerated and circulated, the purified raw material gas is synthesized into methanol by the methanol reaction synthesis unit under the condition of a catalyst, and the crude methanol is purified by the purification unit by adopting the combination of flash evaporation, rectification and the like.
The utility model discloses a low temperature methyl alcohol is washed non-infiltration gas system methyl alcohol system of processing membrane separation includes:
the newly-added low-temperature methanol washing unit comprises a first heat exchanger 1 and an absorption tower 2 filled with low-temperature methanol, wherein a heat source inlet of the first heat exchanger is connected with a non-permeation gas inlet pipeline 3, a heat source outlet is connected with a gas inlet of the absorption tower 2, and a gas outlet of the absorption tower 2 is connected with a cold source inlet of the first heat exchanger 1; the methanol purge gas refers to tail gas discharged by an original methanol device in the prior art, enters a membrane separation unit to be separated into two streams of gas, wherein one stream of gas is permeation gas and mainly contains hydrogen and is sent back to the existing synthesis gas methanol synthesis device; the other strand is non-permeable gas mainly containing hydrogen, carbon monoxide and carbon dioxide, and the non-permeable gas enters the first heat exchanger.
A newly-added methanol synthesis unit which comprises a second heat exchanger 4, a methanol synthesis tower 5, a cooler 6 and a methanol separator 7; the methanol synthesis tower 5 is a main reaction device, which converts the synthesis gas into methanol by being filled with, for example, a copper-based catalyst, the reaction is an exothermic reaction and can release a large amount of heat, and optionally, the methanol synthesis tower is connected with a steam drum 8, and the heat generated in the methanol synthesis is recovered as steam; the cooler 6 may be a water cooler to cool the methanol stream; the methanol separator 7 is a gas-liquid separator for separating liquid crude methanol and tail gas; cold source exit linkage second heat exchanger 4's of first heat exchanger 1 cold source entry, second heat exchanger 4's cold source export and methanol synthesis tower 5's reaction entry linkage, methanol synthesis tower's reaction export and second heat exchanger's heat source entry linkage, second heat exchanger 4's heat source export connects gradually cooler 6 and methanol separator 7, methanol separator 7 includes thick methanol discharge port and exhaust emission port, preferably, exhaust emission port sets up two strands of reposition of redundant personnel pipelines, one of them reposition of redundant personnel pipeline reposition of redundant personnel part tail gas sends into current fuel pipe network as combustion gas, another reposition of redundant personnel pipeline reposition of redundant personnel surplus tail gas joins with second heat exchanger's cold source entry pipeline after letting in compressor 9.
The specific implementation method of the device is as follows, taking 50 ten thousand tons/year coal-to-methanol as an example, the raw methanolThe methanol purge gas of the device is connected with a membrane separation device, the pressure of the non-permeable gas after the methanol purge gas is separated by a membrane separation unit is about 6.2Mpa (G), the temperature is 40 ℃, and the flow of the non-permeable gas is 10000Nm3The impermeable gas composition is: h2： 56％、N2：11％、CH4：4％、CO：16.9％、CO2：12％、CH30.1 percent of OH and the hydrogen-carbon ratio is about 1.5.
The non-permeable gas separated by the membrane enters a first heat exchanger 1 for heat exchange from a non-permeable gas pipeline 3, the temperature is reduced to about-30 ℃, and then the non-permeable gas enters an absorption tower 2, part of carbon dioxide in the non-permeable gas in the absorption tower 2 is absorbed by low-temperature methanol which is added from the upper part and comes from the existing low-temperature methanol washing device, and the absorption rate is about 460Nm3The/h carbon dioxide is absorbed, and the methanol liquid after absorbing the carbon dioxide is discharged from the bottom of the absorption tower and sent to the low-temperature methanol washing device in the prior art for regeneration. The synthesis gas after removing the carbon dioxide enters a first heat exchanger 1 for heat exchange from the top of an absorption tower 2, the temperature is raised to about 20 ℃, the pressure is about 6.15Mpa (G), and the flow rate is about 9540Nm3H, a hydrogen to carbon ratio of about 2. The heat-exchanged synthetic gas is 28600Nm from the compressor3The/h circulating gas is mixed to become tower inlet gas, the tower inlet gas enters the second heat exchanger 4 to exchange heat with tower outlet gas from the methanol synthesis tower 5, the temperature is 195-225 ℃ after heat exchange, then the tower inlet gas enters the methanol synthesis tower 5, the temperature of the methanol synthesis outlet gas is 215-255 ℃, the tower inlet gas enters the second heat exchanger 4 to exchange heat, the temperature of the synthesis gas after heat exchange is 80-100 ℃, then the synthesis gas is cooled to about 40 ℃ through the cooler 6, then the synthesis gas enters the gas-liquid separator 7, the flow of the separated crude methanol liquid is about 2786kg/h, the concentration of the methanol is about 91%, and the crude methanol is purified by a purification unit of a crude methanol device. Tail gas pressure about 5.85MPa (G) and flow rate 32410NNm3H, divided into two parts, one part being the recycle gas, flow rate 28600Nm3The reaction product is compressed by a compressor 9 and returns to a methanol system for circulation; part of the fuel gas is used as fuel gas, and the flow rate is 3810Nm3And h, delivering the fuel to a fuel pipe network after pressure control. The methanol synthesis tower is merged into a byproduct steam pipe network of the original methanol device through a steam drum 8 with the byproduct saturated steam flow of about 800 kg/h.
In the embodiment, the non-permeable gas subjected to low-temperature methanol washing is adopted to produce methanol, and the emission of carbon (converted into carbon dioxide) is reduced by 2.75 ten thousand tons every year compared with the case that the non-permeable gas is used as fuel gas; the byproduct methanol is 2 million tons every year, and the byproduct steam is 6400 tons every year.
Example 2
As shown in fig. 2, in the apparatus of example 1, the non-permeate gas inlet line 1 is divided into two feeding branches by a splitter, wherein one feeding branch is connected with the hot source inlet of the first heat exchanger 1, and the other feeding branch is merged to the cold source outlet line of the first heat exchanger 1. The hydrogen-carbon ratio of the synthesis gas is changed by changing the flow dividing rate of the two feeding branches.
The specific implementation process of this embodiment is as follows, taking 80 ten thousand tons/year coal-to-methanol as an example, the pressure of the non-permeable gas after the methanol purge gas is separated by the membrane separation unit is about 7.0mpa (g), the non-permeable gas flow rate is 15000Nm3/h at 40 ℃, and the non-permeable gas composition is: h2：55％、N2：10％、CH4：4％、CO：17％、 CO2: 14% and a hydrogen to carbon ratio of about 1.32.
The non-permeable gas separated by the membrane is divided into two parts, one part is non-permeable gas, and the flow rate is 7000Nm3H, not passing through the first heat exchanger 1 and the absorption tower 2; a part of non-permeable gas with a flow rate of 8000Nm3H, entering a first heat exchanger 1 for heat exchange, reducing the temperature to about-30 ℃, then entering an absorption tower 2, and absorbing most of carbon dioxide in non-permeable gas in the absorption tower 2 by low-temperature methanol which is added from the upper part and comes from an existing low-temperature methanol washing device, wherein the absorption rate is about 1040Nm3The/h carbon dioxide is absorbed, and the methanol liquid after absorbing the carbon dioxide is discharged from the bottom of the absorption tower 2 and sent to the existing low-temperature methanol washing device for regeneration. The non-permeable gas after removing the carbon dioxide enters a first heat exchanger 1 for heat exchange from the top of an absorption tower 2, the temperature is raised to about 20 ℃, the pressure is about 6.95Mpa (G), and the non-permeable gas is mixed with another non-permeable gas, the flow rate is about 13960Nm3Hydrogen/carbon ratio of about 2, 41880Nm of the mixed syngas from compressor 93The circulation gas is mixed to become tower inlet gas, the tower inlet gas enters a second heat exchanger 4 to exchange heat with tower outlet gas from a methanol synthesis tower 5, the temperature after heat exchange is 195-225 ℃, and then the tower inlet gas enters the methanol synthesis tower 5, the temperature of the methanol synthesis outlet gas is 215-255 ℃, and the tower inlet gas enters second heat exchangeAnd (3) exchanging heat by the device 4, cooling the synthesis gas to about 40 ℃ by the cooler 6 after heat exchange, then feeding the synthesis gas into the methanol separator 7, wherein the flow rate of the separated crude methanol liquid is about 4328kg/h, the concentration of the methanol is about 91%, and removing the crude methanol from a flash tank of the original methanol device. Tail gas pressure of about 6.75MPa (G) and flow rate of about 46890Nm3H, divided into two parts, one part as circulating gas, flow rate 41880Nm3The reaction product is compressed by a compressor 9 and returns to a methanol system for circulation; a part of the fuel gas is used as fuel gas, and the flow rate is 5010Nm3And h, delivering the fuel to a fuel pipe network after pressure control. The flow rate of the byproduct saturated steam of the methanol synthesis tower is about 900kg/h, and the byproduct saturated steam is merged into a byproduct steam pipe network of the original methanol device.
In the embodiment, the non-permeable gas treated by low-temperature methanol washing is adopted to produce methanol, and the emission of carbon (converted into carbon dioxide) is reduced by about 4.26 ten thousand tons every year compared with the non-permeable gas as fuel gas; about 3.1 million tons of methanol are byproduct every year, and 7200 tons of vapor are byproduct every year.
The above description is only exemplary of the present invention and should not be taken as limiting the scope of the present invention, as any modifications, equivalents, improvements and the like made within the spirit and principles of the present invention are intended to be included within the scope of the present invention.
Claims (7)
1. A system for preparing methanol from non-permeable gas by utilizing low-temperature methanol washing processing membrane separation, which is taken as an auxiliary device of a main device for preparing methanol from synthesis gas, is characterized by comprising:
the low-temperature methanol washing unit comprises a first heat exchanger and an absorption tower filled with low-temperature methanol, wherein a heat source inlet of the first heat exchanger is connected with a non-permeation gas inlet pipeline, a heat source outlet is connected with a gas inlet of the absorption tower, and a gas outlet of the absorption tower is connected with a cold source inlet of the first heat exchanger;
the methanol synthesis unit comprises a second heat exchanger, a methanol synthesis tower, a cooler and a methanol separator, wherein a cold source outlet of the first heat exchanger is connected with a cold source inlet of the second heat exchanger, a cold source outlet of the second heat exchanger is connected with a reaction inlet of the methanol synthesis tower, a reaction outlet of the methanol synthesis tower is connected with a heat source inlet of the second heat exchanger, a heat source outlet of the second heat exchanger is sequentially connected with the cooler and the methanol separator, and the methanol separator comprises a crude methanol discharge port and a tail gas discharge port.
2. The system for preparing methanol by separating non-permeate gas through the membrane by low-temperature methanol washing treatment according to claim 1, wherein two branch lines are arranged at the tail gas discharge port, wherein a branch portion of tail gas of one branch line is fed into a fuel pipe network as combustion gas, and the other branch line branches the rest of tail gas and is fed into a compressor and then is connected with a cold source inlet line of the second heat exchanger in a return way to be converged.
3. The system for producing methanol by using the low-temperature methanol washing processing membrane to separate the non-permeable gas according to claim 1, wherein a steam drum is connected to the methanol synthesis tower, and the heat generated in the methanol synthesis is recovered as steam.
4. The system for producing methanol by separating non-permeate gas through the membrane by using low-temperature methanol washing as claimed in claim 1, wherein the non-permeate gas inlet line is divided into two feeding branches by a splitter, one feeding branch is connected with the heat source inlet of the first heat exchanger, and the other feeding branch is merged to the cold source outlet line of the first heat exchanger.
5. The system for separating non-permeate gas into methanol by using the low-temperature methanol washing processing membrane as claimed in claim 1, wherein the liquid outlet of the absorption tower is connected to the low-temperature methanol washing system of the main device for preparing methanol from synthesis gas.
6. The system for processing membrane separation non-permeate gas to produce methanol using low temperature methanol scrubbing of claim 1, wherein the crude methanol discharge of the methanol separator is connected to the purification unit of the syngas to methanol main device.
7. A production system for preparing methanol from coal or coke oven gas comprises a first methanol production system and a second methanol production system, wherein the first methanol production system is a main device for preparing methanol from synthesis gas, a methanol purge gas generated by the main device for preparing methanol from synthesis gas is connected with a membrane separation device, a membrane separation non-permeable gas generated by the membrane separation device is connected with the second methanol production system, and the second methanol production system is the system for preparing methanol from non-permeable gas by utilizing low-temperature methanol washing treatment membrane separation according to any one of claims 1 to 6.
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| CN202020217470.4U CN212425918U (en) | 2020-02-27 | 2020-02-27 | Utilize low temperature methanol to wash processing membrane separation non-permeate gas system methanol system and including its methanol production system |
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Effective date of registration: 20240710 Address after: No. 2 Shulong Street, Xihanggang, Shuangliu District, Chengdu City, Sichuan Province 610000 Patentee after: Jian Xingzhe Country or region after: China Address before: Floor 1, building 1, No.50, North Zijing Road, hi tech Zone, Chengdu, Sichuan 610000 Patentee before: CHENGDU ZEJIA HUAFEI TECHNOLOGY CO.,LTD. Country or region before: China |