CN209854029U - Device for preparing methanol from synthesis gas without conversion system - Google Patents
Device for preparing methanol from synthesis gas without conversion system Download PDFInfo
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- CN209854029U CN209854029U CN201822179632.5U CN201822179632U CN209854029U CN 209854029 U CN209854029 U CN 209854029U CN 201822179632 U CN201822179632 U CN 201822179632U CN 209854029 U CN209854029 U CN 209854029U
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- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 title claims abstract description 666
- 238000003786 synthesis reaction Methods 0.000 title claims abstract description 105
- 230000015572 biosynthetic process Effects 0.000 title claims abstract description 104
- 238000006243 chemical reaction Methods 0.000 title claims abstract description 26
- 239000007789 gas Substances 0.000 claims abstract description 241
- 239000001257 hydrogen Substances 0.000 claims abstract description 103
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 103
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 101
- 239000003245 coal Substances 0.000 claims abstract description 63
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 46
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 37
- 238000002309 gasification Methods 0.000 claims abstract description 37
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 37
- 239000001301 oxygen Substances 0.000 claims abstract description 37
- 238000010926 purge Methods 0.000 claims description 74
- 238000000746 purification Methods 0.000 claims description 64
- 230000006835 compression Effects 0.000 claims description 49
- 238000007906 compression Methods 0.000 claims description 49
- 238000000605 extraction Methods 0.000 claims description 44
- 238000000926 separation method Methods 0.000 claims description 28
- 239000007788 liquid Substances 0.000 claims description 4
- 239000012528 membrane Substances 0.000 claims description 4
- 101000863856 Homo sapiens Shiftless antiviral inhibitor of ribosomal frameshifting protein Proteins 0.000 claims 4
- 102100029950 Shiftless antiviral inhibitor of ribosomal frameshifting protein Human genes 0.000 claims 4
- 238000004519 manufacturing process Methods 0.000 abstract description 20
- 238000005868 electrolysis reaction Methods 0.000 abstract description 8
- 238000001179 sorption measurement Methods 0.000 abstract description 7
- 230000000295 complement effect Effects 0.000 abstract description 4
- 230000008878 coupling Effects 0.000 abstract description 4
- 238000010168 coupling process Methods 0.000 abstract description 4
- 238000005859 coupling reaction Methods 0.000 abstract description 4
- 238000000034 method Methods 0.000 description 19
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 16
- 230000008569 process Effects 0.000 description 15
- 229910052799 carbon Inorganic materials 0.000 description 14
- 238000002360 preparation method Methods 0.000 description 11
- 229910002091 carbon monoxide Inorganic materials 0.000 description 9
- 239000003546 flue gas Substances 0.000 description 8
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 7
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 7
- 229910002092 carbon dioxide Inorganic materials 0.000 description 7
- 239000002994 raw material Substances 0.000 description 7
- 230000008901 benefit Effects 0.000 description 5
- 238000010586 diagram Methods 0.000 description 5
- 238000010521 absorption reaction Methods 0.000 description 3
- 239000001569 carbon dioxide Substances 0.000 description 3
- 238000003795 desorption Methods 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 150000002431 hydrogen Chemical class 0.000 description 3
- 239000012535 impurity Substances 0.000 description 3
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 3
- 238000005406 washing Methods 0.000 description 3
- 239000002253 acid Substances 0.000 description 2
- 239000003054 catalyst Substances 0.000 description 2
- 239000003034 coal gas Substances 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 239000003344 environmental pollutant Substances 0.000 description 2
- 231100000719 pollutant Toxicity 0.000 description 2
- 238000003860 storage Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 1
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 239000000571 coke Substances 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 230000001276 controlling effect Effects 0.000 description 1
- 238000005262 decarbonization Methods 0.000 description 1
- 238000005261 decarburization Methods 0.000 description 1
- 229910001882 dioxygen Inorganic materials 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 238000010828 elution Methods 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 1
- 230000010354 integration Effects 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 125000001741 organic sulfur group Chemical group 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 239000010117 shenhua Substances 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 230000029305 taxis Effects 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Classifications
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
- Y02E60/30—Hydrogen technology
- Y02E60/36—Hydrogen production from non-carbon containing sources, e.g. by water electrolysis
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- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The utility model discloses a synthetic gas system methyl alcohol device of no transform system, the device adopt electrolysis water hydrogen manufacturing and oxygen and the complementary coupling of coal system gas production methyl alcohol. The device directly sends oxygen generated by electrolyzed water into the gasification unit, and hydrogen prepared by electrolyzed water is merged into purified synthesis gas, thereby replacing the situation of the original synthesis gas conversion unit and the pressure swing adsorption device, not only having high production efficiency of methanol, but also realizing comprehensive utilization of resources.
Description
Technical Field
The utility model relates to a methyl alcohol preparation technical field, and in particular to synthetic gas system methyl alcohol device of no transform system.
Background
In recent years, the industry for preparing methanol from coal in China develops rapidly. At present, the existing coal-to-methanol production factories taking coal gas as a core in China have more than 230 families, and the total annual energy can exceed 2200 million tons. The large coal-to-methanol projects which are put into production include 180 million tons of coal-based methanol projects produced by Shenhua Baotou, 167 million tons of coal-based methanol projects produced by Datang International and 120 million tons of coal-based methanol projects produced by Shenhuaning coal.
At present, the coal-to-methanol device generally adopts the process flow of gasification → carbon monoxide transformation → low-temperature methanol elution for removing acid gas → methanol synthesis. The raw syngas from the gasification unit is treated in a carbon monoxide shift unit to convert CO and H2Reaction of O to H2And CO2And controlling the depth of CO shift reaction to further control H in the synthesis gas2The mol ratio of/CO; then in the transform unit pair H2The mol ratio of the gas to the CO is further adjusted so that the crude synthesis gas is desulfurized and partially decarbonized by a low-temperature methanol washing deviceTo have an ideal H2Methanol synthesis gas in molar ratio/CO.
The flow is schematically shown as follows:
when the process flow is adopted, in a CO conversion unit, due to the reasons that the bed temperature, the reaction activity, the CO conversion reaction degree and the like of a catalyst of a conversion furnace are difficult to control and the like, the H in the synthesis gas cannot be ensured2The mol ratio of/CO meets the requirement of methanol synthesis. In addition, in the prior art, only one stream of feed gas is fed into the low-temperature methanol washing unit, namely the H-containing gas regulated in the CO conversion unit2Crude synthesis gas of/CO. Such a flow arrangement results in a large size of the absorption tower in a large-scale coal chemical plant, and one feed simultaneously means that only one absorption system is provided, the methanol circulation system of the low-temperature methanol washing absorption part cannot be optimized, and the cold consumption is high.
However, the hydrogen/carbon atomic ratio of coal is 0.2-1.0 in terms of the elemental composition of coal, and the hydrogen-to-carbon ratio (abbreviated as H/C) of synthesis gas required for methanol synthesis is about 2.1-2.2, so that the adjustment of the hydrogen-to-carbon ratio is accompanied with the preparation of methanol from coal. In the existing process of preparing methanol from coal, carbon monoxide in the synthesis gas is converted into hydrogen through water gas shift reaction, and the carbon monoxide is reacted into carbon dioxide with the same amount of substances in the shift process. The carbon dioxide is passed through an acid gas removal unit and is discharged directly to the environment. This not only results in the loss of a large amount of available carbon element, but also has a negative impact on the environment. In addition, the cost advantages of the coal-to-methanol process are no longer present if carbon taxes are introduced.
A scheme is found to reduce or avoid the component adjustment of the gasified synthesis gas at the minimum cost, and the energy conservation and emission reduction in the production process can be effectively realized. The combined supply system of various raw materials is a more effective way to solve the problems. The combined supply system has the advantages that carbon-rich resources such as coal and the like and hydrogen-rich resources such as natural gas, coke oven gas and the like can be reasonably matched with materials, energy and the production process in a process integration mode, and the hydrogen-carbon ratio of the synthesis gas is adjusted according to actual needs.
In the traditional coal-to-methanol process, oxygen and coal are needed to be gasified, the molar ratio of hydrogen to carbon monoxide in the generated synthesis gas is about 0.4, carbon monoxide and water vapor are needed to be subjected to conversion reaction, 1.6 tons of carbon dioxide are needed to be discharged per ton of methanol after conversion, the carbon emission of enterprises is increased, the environmental pressure is increased, and the resource waste is serious.
SUMMERY OF THE UTILITY MODEL
An object of the utility model is to provide a no transform system's synthetic gas system methyl alcohol device, the device overcome the not enough of current coal system methyl alcohol, provide a higher efficiency, more energy-conserving, safer environmental protection's coal system methyl alcohol apparatus for producing.
The technical problem of the utility model is solved and following technical scheme is adopted to realize.
The utility model provides a no transform system's synthetic gas preparation methyl alcohol device, include: the system comprises an electrolytic water unit, a coal gasification unit, a purification unit, a compression unit and a methanol synthesis unit, wherein an oxygen outlet of the electrolytic water unit is connected with an oxygen inlet of the coal gasification unit, a synthesis gas outlet of the coal gasification unit is connected with a synthesis gas inlet of the purification unit, a purified gas outlet of the purification unit is connected with a purified gas inlet of the compression unit, a hydrogen outlet of the electrolytic water unit is connected with a hydrogen inlet of the compression unit, and a compressed gas outlet of the compression unit is connected with a compressed gas inlet of the methanol synthesis unit.
The utility model has the advantages that:
the utility model provides a no transform system's synthetic gas system methyl alcohol device, the utility model discloses in with the hydrogen of electrolysis water system incorporate into the synthetic gas after the purification, band the situation that needs synthetic gas transform unit and pressure swing adsorption equipment in traditional coal system methyl alcohol device, utilize the device preparation methyl alcohol to be a green, environment-friendly type device.
Drawings
In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the drawings that are required to be used in the embodiments will be briefly described below, it should be understood that the following drawings only illustrate some embodiments of the present invention, and therefore should not be considered as limiting the scope, and for those skilled in the art, other related drawings can be obtained according to the drawings without inventive efforts.
FIG. 1 is a schematic diagram of a device for producing methanol from synthesis gas without a shift system in example 1 of the present invention;
FIG. 2 is a schematic diagram of a device for producing methanol from synthesis gas without a shift system in example 2 of the present invention;
FIG. 3 is a schematic diagram of a device for producing methanol from synthesis gas without a shift system according to example 3 of the present invention;
FIG. 4 is a schematic diagram of a device for producing methanol from synthesis gas without a shift system according to example 4 of the present invention;
FIG. 5 is a schematic diagram of a separation and purification unit of a syngas to methanol plant without a shift system in examples 2 and 4 of the present invention;
reference numerals: 100-an electrolytic water unit; 200-a coal gasification unit; 300-a purification unit; 400-a compression unit; a 500-methanol synthesis unit; 600-a separation purification unit; 610-a gas-liquid separator; 620-heat exchanger; 630-and membrane separator; 700-purge hydrogen stripping unit; 800-a boiler; 900-a methanol rectification unit; 1000-tank field.
Detailed Description
In order to make the objects, technical solutions and advantages of the embodiments of the present invention clearer, the technical solutions of the embodiments of the present invention will be clearly and completely described below. The examples, in which specific conditions are not specified, were conducted under conventional conditions or conditions recommended by the manufacturer. The reagents or instruments used are not indicated by the manufacturer, and are all conventional products available commercially.
The following describes a methanol preparation apparatus from syngas without shift system according to an embodiment of the present invention.
The embodiment of the utility model provides a no transform system's synthetic gas preparation methyl alcohol device, include: the coal gasification system comprises an electrolytic water unit 100, a coal gasification unit 200, a purification unit 300, a compression unit 400 and a methanol synthesis unit 500, wherein an oxygen outlet of the electrolytic water unit 100 is connected with an oxygen inlet of the coal gasification unit 200, a synthesis gas outlet of the coal gasification unit 200 is connected with a synthesis gas inlet of the purification unit 300, a purified gas outlet of the purification unit 300 is connected with a purified gas inlet of the compression unit 400, a hydrogen outlet of the electrolytic water unit 100 is connected with a hydrogen inlet of the compression unit 400, and a compressed gas outlet of the compression unit 400 is connected with a compressed gas inlet of the methanol synthesis unit 500.
The embodiment of the utility model provides a synthetic gas system methyl alcohol device of no transform system, the device adopt the electrolytic water hydrogen manufacturing and oxygen and coal system complementary coupling production methyl alcohol, carry the oxygen that the electrolytic water unit 100 made to coal gasification unit 200 in and carry out coal gasification reaction and produce the synthetic gas, reduce the air separation plant system oxygen scale; the hydrogen produced by the electrolytic water unit 100 is merged into the synthesis gas purified by the purification unit 300, the ratio of hydrogen to carbon monoxide in the synthesis gas is adjusted to produce methanol raw material gas with proper hydrogen-carbon ratio, the methanol raw material gas is compressed in the compression unit 400 and then is conveyed into the methanol synthesis unit 500, the process does not need a conversion system, a pressure swing adsorption and decarburization process, and discharged CO does not need to be converted into CO2The amounts are negligible.
Therefore, the embodiment of the utility model provides a system methyl alcohol device replaces the situation that needs empty oxygenerator, synthetic gas transform unit and pressure swing adsorption device among traditional coal system methyl alcohol device, greatly reduced the complexity and the corresponding technology degree of difficulty of device, especially traditional coal system methyl alcohol in-process, at the synthetic gas transform unit, because bed temperature, the activity of reaction, the difficult reasons such as degree of CO shift reaction of shift converter catalyst, can't guarantee in the synthetic gas H reasons such as difficult control such as bed temperature, the activity of reaction, CO shift reaction's degree2The mol ratio of/CO meets the requirement of methanol synthesis. The utility model discloses well greatly reduced the degree of difficulty of transform, simple high-efficient can not introduce new impurity, only need adjust hydrogen and carbon monoxide proportion in the synthetic gas, can obtain the raw material gas who is suitable for methyl alcohol preparation, improved the production efficiency of methyl alcohol, in addition, the hydrogen manufacturing is done to the brineelectrolysis, is a green hydrogen manufacturing method and environment-friendly technology, does not produce other pollutants in the electrolysis-process, and the protection protectsAnd (4) comprehensively utilizing carbon resources in the system.
Further, the apparatus for preparing methanol from synthesis gas further comprises a separation purification unit 600 and a purge gas hydrogen extraction unit 700, wherein the methanol purge gas outlet of the methanol synthesis unit 500 is connected with the inlet of the separation purification unit 600, and the outlet of the separation purification unit 600 is connected with the inlet of the purge gas hydrogen extraction unit 700.
Further, the separation purification unit 600 includes a gas-liquid separator 610, a heat exchanger 620, and a membrane separator 630, which are connected in sequence.
Further, a purge gas hydrogen extraction outlet of the purge gas hydrogen extraction unit 700 in the syngas methanol preparation plant is connected with a purge gas hydrogen extraction inlet of the compression unit 400.
Therefore, the embodiment of the utility model provides a no transform system's synthetic gas system methyl alcohol device is provided, should prepare methyl alcohol device still includes: the separation and purification unit 600 and the purge gas hydrogen extraction unit 700 are used for further processing purge gas generated after methanol synthesis, wherein a methanol purge gas outlet of the methanol synthesis unit 500 is connected with an inlet of the separation and purification unit 600, the purge gas is subjected to separation and purification treatment and then enters the purge gas hydrogen extraction unit 700, hydrogen generated by hydrogen extraction treatment of the purge gas hydrogen extraction unit 700 is merged into the compression unit 400 to serve as hydrogen raw material make-up gas, hydrogen in the methanol purge gas is effectively utilized, and the production efficiency is improved.
Further, the apparatus for preparing methanol from synthesis gas further comprises a methanol rectification unit 900, and a crude methanol outlet of the methanol synthesis unit 500 is connected with a crude methanol inlet of the methanol rectification unit 900.
Further, the device for preparing methanol from synthesis gas further comprises a boiler 800, flash steam discharged from the methanol rectification unit 900 and desorbed gas discharged from the purge gas hydrogen stripping unit 700 are mixed and enter a mixed gas pipeline, and the mixed gas pipeline is connected with the boiler 800.
Therefore, the embodiment of the utility model provides a no transform system's synthetic gas system methyl alcohol device is provided, should prepare methyl alcohol device still includes: the methanol rectification unit 900 is used for further processing the methanol generated after the methanol synthesis, wherein the crude methanol generated by the reaction of the methanol synthesis unit 500 is conveyed to the methanol rectification unit 900, a refined methanol finished product is separated and conveyed to a methanol tank area for storage or delivery, and flash steam generated by the methanol rectification unit 900 and residual desorption gas after hydrogen is extracted by the purge gas hydrogen extraction unit 700 are conveyed to the boiler 800 for combustion to generate steam, so that the comprehensive utilization of resources is realized.
Further, the device for preparing methanol from synthesis gas also comprises a conveying pipeline, and the conveying pipeline is arranged between the inlet and the outlet of different units.
Further, the device for preparing methanol from synthesis gas also comprises a pressure gauge, and the pressure gauge is arranged on the conveying pipeline between different units.
Further, the device for preparing methanol from synthesis gas also comprises a flow meter, and the gas flow meter is arranged on a conveying pipeline between different units.
Furthermore, the device for preparing methanol from synthesis gas also comprises a valve, and the valve is arranged on a conveying pipeline between different units.
The process for preparing the methanol by using the device for preparing the methanol from the synthesis gas without the shift system comprises the following steps:
the raw material coal and the oxygen gas prepared by the electrolytic water unit 100 are gasified and reacted in the coal gasification unit 200 to generate synthesis gas, the synthesis gas is purified in the purification unit 300 to obtain purified synthesis gas, the purified synthesis gas and the hydrogen gas prepared by the electrolytic water unit 100 are combined according to the hydrogen-carbon ratio required by methanol synthesis, then the compression unit 400 is compressed to obtain compressed gas, and the compressed gas is reacted in the methanol synthesis unit 500 to prepare crude methanol and methanol purge gas.
Methanol purge gas generated by the reaction of the methanol synthesis unit 500 is treated by the separation and purification unit 600, then enters the purge gas hydrogen extraction unit 700 to extract generated hydrogen as supplementary gas of hydrogen in the compression unit 400, desorbed gas generated after hydrogen extraction in the purge gas hydrogen extraction unit 700 and flash steam generated in the methanol rectification unit 900 are combined to generate mixed gas, the mixed gas is conveyed to the boiler 800 to be combusted to generate flue gas for discharging, crude methanol generated by the reaction of the methanol synthesis unit 500 is conveyed to the methanol rectification unit 900, and a refined methanol finished product generated in the methanol rectification unit 900 is stored or conveyed outside.
It can be seen that the process for the preparation of methanol using the above apparatus comprises the steps of: the coal and oxygen prepared by electrolyzing water are gasified to generate synthetic gas, the synthetic gas is purified and then is combined with hydrogen prepared by electrolyzing water according to the hydrogen-carbon ratio required by methanol synthesis, and the methanol is prepared by compression. Therefore, the process adopted by the embodiment produces the methanol by utilizing the hydrogen production by the electrolyzed water and the complementary coupling of the oxygen and the coal gas, fully utilizes the hydrogen and the oxygen produced by the electrolyzed water, does not contain impurities, avoids the complex processes of air separation oxygen production, pressure swing adsorption hydrogen production and the like required in the process of preparing the methanol by the coal at present, ensures that the preparation of the synthesis gas in the methanol preparation process is simple and efficient, has small impurity content, and obviously improves the purity and the yield of the prepared methanol.
The embodiment of the utility model provides an in the coal gasification unit 200 the synthetic gas that produces through purification unit 300 dust in the detached gas, tar, and pressure boost desorption hydrogen sulfide and organic sulfur, make the sulfur content of synthetic gas be less than 0.2ppm, the synthetic gas through purification treatment is sent into compression unit 400 again and is carried out compression treatment, the synthetic gas merges according to the required hydrocarbon proportion of methanol synthesis with the hydrogen that the brineelectrolysis made, and compressed to the required pressure 4.5 ~ 7Mpa of synthetic methanol together, be higher than or be less than foretell pressure and do not benefit to the make full use of synthetic gas and hydrogen, then carry out the methanol synthesis reaction with the gas after the compression in methanol synthesis unit 500, the hydrogen carbon proportion in this synthesis unit is 2.0-4.5.
The features and properties of the present invention are described in further detail below with reference to examples.
Example 1
Referring to fig. 1, a shift-system-free methanol plant from syngas comprises:
the coal gasification system comprises an electrolytic water unit 100, a coal gasification unit 200, a purification unit 300, a compression unit 400 and a methanol synthesis unit 500, wherein the electrolytic water unit 100 comprises an oxygen outlet and a hydrogen outlet, the coal gasification unit 200 comprises a coal inlet, an oxygen inlet and a synthesis gas outlet, the purification unit 300 comprises a synthesis gas inlet and a purified gas outlet, the compression unit 400 comprises a hydrogen inlet, a purified gas inlet and a compressed gas outlet, and the methanol synthesis unit 500 comprises a compressed gas inlet, a methanol purge gas outlet and a crude methanol outlet.
An oxygen inlet of the coal gasification unit 200 is connected with an oxygen outlet of the electrolytic water unit 100, a syngas outlet of the coal gasification unit 200 is connected with a syngas inlet of the purification unit 300, a purified gas outlet of the purification unit 300 and a hydrogen outlet of the electrolytic water unit 100 are respectively connected with a purified gas inlet and a hydrogen inlet of the compression unit 400, and a compressed gas outlet of the compression unit 400 is connected with a compressed gas inlet of the methanol synthesis unit 500.
Example 2
Referring to fig. 2 and 5, a syngas to methanol plant without shift system comprises:
the system comprises an electrolytic water unit 100, a coal gasification unit 200, a purification unit 300, a compression unit 400, a methanol synthesis unit 500, a separation purification unit 600, a purge gas hydrogen extraction unit 700 and a boiler 800, wherein the electrolytic water unit 100 comprises an oxygen outlet and a hydrogen outlet, the coal gasification unit 200 comprises a coal inlet, an oxygen inlet and a synthesis gas outlet, the purification unit 300 comprises a synthesis gas inlet and a purification gas outlet, the compression unit 400 comprises a hydrogen inlet, a purification gas inlet and a compressed gas outlet, the methanol synthesis unit 500 comprises a compressed gas inlet, a methanol purge gas outlet and a crude methanol outlet, the separation purification unit 600 comprises a methanol purge gas inlet and a methanol purge gas outlet, the purge gas hydrogen extraction unit 700 comprises a purified methanol purge gas inlet, a purified methanol purge gas hydrogen outlet and a purge gas outlet, and the boiler 800 comprises a mixed gas inlet and a flue gas outlet; referring to fig. 5, the separation purification unit 600 includes 610, 620, and 630 connected in sequence.
An oxygen inlet of the coal gasification unit 200 is connected with an oxygen outlet of the electrolytic water unit 100, a syngas outlet of the coal gasification unit 200 is connected with a syngas inlet of the purification unit 300, a purified gas outlet of the purification unit 300, a hydrogen outlet of the electrolytic water unit 100 and a purge gas hydrogen extraction gas outlet are respectively connected with a purified gas inlet, a hydrogen inlet and a purge gas hydrogen extraction gas inlet of the compression unit 400, and a compressed gas outlet of the compression unit 400 is connected with a compressed gas inlet of the methanol synthesis unit 500.
The methanol purge gas outlet of the methanol synthesis unit 500 is connected with the inlet of the separation and purification unit 600, the outlet of the separation and purification unit 600 is connected with the purified methanol purge gas inlet of the purge gas hydrogen extraction unit 700, the purified methanol purge gas hydrogen extraction outlet of the purge gas hydrogen extraction unit 700 is connected with the purge gas hydrogen extraction inlet of the compression unit 400, the desorption gas outlet of the purge gas hydrogen extraction unit 700 is connected with the mixed gas inlet of the boiler 800, and the flue gas outlet of the boiler 800 discharges flue gas.
Example 3
Referring to fig. 3, a shift-system-free methanol plant from syngas comprises:
the electrolytic water unit 100, the coal gasification unit 200, the purification unit 300, the compression unit 400, the methanol synthesis unit 500, the methanol rectification unit 900 and the tank field 1000, the electrolytic water unit 100 includes oxygen export and hydrogen export, the coal gasification unit 200 includes the coal entry, oxygen entry and synthetic gas export, the compression unit 400 includes the hydrogen entry, purify gas entry and compressed gas export, the methanol synthesis unit 500 includes compressed gas entry and methanol purge gas export, the crude methanol export, the methanol rectification unit 900 includes crude methanol entry and refined methanol finished product export, the tank field 1000 includes refined methanol finished product entry and refined methanol finished product export.
An oxygen inlet of the coal gasification unit 200 is connected with an oxygen outlet of the electrolytic water unit 100, a syngas outlet of the coal gasification unit 200 is connected with a syngas inlet of the purification unit 300, a purified gas outlet of the purification unit 300, a hydrogen outlet of the electrolytic water unit 100 and a purge gas hydrogen extraction gas outlet are respectively connected with a purified gas inlet, a hydrogen inlet and a purge gas hydrogen extraction gas inlet of the compression unit 400, and a compressed gas outlet of the compression unit 400 is connected with a compressed gas inlet of the methanol synthesis unit 500.
The crude methanol outlet of the methanol synthesis unit 500 is connected with the crude methanol inlet of the methanol rectification unit 900, the refined methanol finished product outlet of the methanol rectification unit 900 is connected with the refined methanol finished product inlet of the tank area 1000, and the refined methanol finished product outlet of the tank area 1000 obtains the refined methanol finished product.
Example 4
Referring to fig. 4 and 5, a syngas to methanol plant without shift system comprises:
the system comprises an electrolytic water unit 100, a coal gasification unit 200, a purification unit 300, a compression unit 400 and a methanol synthesis unit 500, a separation purification unit 600, a purge gas hydrogen extraction unit 700, a boiler 800, a methanol rectification unit 900 and a tank area 1000, wherein the electrolytic water unit 100 comprises an oxygen outlet and a hydrogen outlet, the coal gasification unit 200 comprises a coal inlet, an oxygen inlet and a synthesis gas outlet, the purification unit 300 comprises a synthesis gas inlet and a purified gas outlet, the compression unit 400 comprises a hydrogen inlet, a purified gas inlet, a purge gas hydrogen extraction inlet and a compressed gas outlet, the methanol synthesis unit 500 comprises a compressed gas inlet, a methanol purge gas outlet and a crude methanol outlet, the separation purification unit 600 comprises a methanol purge gas inlet and a methanol outlet, the purge gas hydrogen extraction unit 700 comprises a purified methanol purge gas inlet, a purified methanol purge gas hydrogen extraction outlet and a purge gas outlet, the boiler 800 comprises a mixed gas inlet and a flue gas outlet, the methanol rectification unit 900 comprises a crude methanol inlet, a refined methanol finished product outlet and a flash steam outlet, the tank area 1000 comprises a refined methanol finished product inlet and a refined methanol finished product outlet, and referring to fig. 5, the separation and purification unit 600 comprises 610, 620 and 630 which are connected in sequence.
An oxygen inlet of the coal gasification unit 200 is connected with an oxygen outlet of the electrolytic water unit 100, a syngas outlet of the coal gasification unit 200 is connected with a syngas inlet of the purification unit 300, a purified gas outlet of the purification unit 300, a hydrogen outlet of the electrolytic water unit 100, and a purge gas extraction hydrogen outlet of the purge gas hydrogen extraction unit 700 are respectively connected with a purified gas inlet, a hydrogen inlet, and a purge gas extraction hydrogen inlet of the compression unit 400, and a compressed gas outlet of the compression unit 400 is connected with a compressed gas inlet of the methanol synthesis unit 500.
The methanol purge gas outlet of the methanol synthesis unit 500 is connected with the inlet of the separation purification unit 600, the outlet of the separation purification unit 600 is connected with the purified methanol purge gas inlet of the purge gas hydrogen extraction unit 700, the purge gas hydrogen extraction outlet of the purge gas hydrogen extraction unit 700 is connected with the purge gas hydrogen extraction inlet of the compression unit 400, a mixed gas pipeline obtained by mixing desorbed gas generated after hydrogen extraction in the purge gas hydrogen extraction unit 700 and flash steam in the methanol rectification unit 900 is connected with the mixed gas inlet of the boiler 800, and the flue gas outlet of the boiler 800 discharges flue gas.
The crude methanol outlet of the methanol synthesis unit 500 is connected with the crude methanol inlet of the methanol rectification unit 900, the refined methanol finished product outlet of the methanol rectification unit 900 is connected with the refined methanol finished product inlet of the tank area 1000, and the refined methanol finished product outlet of the tank area 1000 obtains the refined methanol finished product.
The process for preparing the methanol by using the device for preparing the methanol by the synthesis gas without the shift system in the embodiment 4 of the utility model comprises the following steps:
the coal and the oxygen generated by the electrolytic water electrolysis unit 1 are subjected to gasification reaction in a coal gasification unit 200 to generate synthesis gas, wherein the mass ratio of the raw material coal to the oxygen is 0.8:2-1.5:2, and the synthesis gas is rich in CO and H2And CO2The synthesis gas of (2).
The synthesis gas is sent into a purification unit 300 for purification treatment, the temperature of the purification treatment is 200-260 ℃, the pressure is 3.5-5MpaG, the purified synthesis gas after the purification treatment and the hydrogen generated by the water electrolysis unit 100 enter a compression unit 400 together for compression treatment, the temperature of the compression treatment is 24-120 ℃, the pressure is 4.5-7MpaG, the purified synthesis gas after the compression treatment is sent into a methanol synthesis unit 500 for reaction, the hydrogen-carbon ratio is adjusted to be 2.0-4.5, and crude methanol and methanol purge gas are generated through the reaction.
The methanol purge gas generated by the reaction of the methanol synthesis unit 500 is sent to the separation purification unit 600 for separation and purification, and then is sent to the purge gas hydrogen extraction unit 700, the hydrogen extracted from the purge gas hydrogen extraction unit 700 is used as the make-up gas of the hydrogen in the compression unit 400, and about 120-160m per ton of methanol is generated in the methanol synthesis process3Purge gas (main component: H)2： 68-73％、CO：2-5％、CO2：0.5-2.3％、N2: 12-16.5% and CH4: 5.4-8.5%, etc.). The purge gas passes through a gas-liquid separator 610, a heat exchanger 620 and a membrane separator 630 in sequence, and then is subjected to pressure swing adsorption to extract hydrogen (namely PSA hydrogen extraction), and the extracted hydrogen (methanol is produced according to the year)150 ten thousand tons, the amount of the hydrogen extracted from the purge gas is 8000m and 5000-3/h) is incorporated into the compression unit 400 as a hydrogen feed make-up gas.
And (3) combining desorbed gas generated after hydrogen is extracted in the purge gas hydrogen extraction unit 700 with flash steam generated in the methanol rectification unit 900 to generate mixed gas, and conveying the mixed gas into the boiler 800 to be combusted to generate flue gas for discharging.
The crude methanol generated by the reaction of the methanol synthesis unit 500 is transported to the methanol rectification unit 900, and the refined methanol product generated in the methanol rectification unit 900 is transported to the tank area 1000 for storage or delivery.
To sum up, the embodiment of the utility model provides a synthetic gas system methyl alcohol device of no transform system, the device that this embodiment adopted utilizes electrolysis water hydrogen manufacturing and oxygen and the complementary coupling production methyl alcohol of coal system gas, the device need not the transform system, pressure swing adsorption and decarbonization system, utilize the device to carry out the methyl alcohol synthesis in-process, directly utilize oxygen and hydrogen that the electrolysis water produced, electrolysis water system oxygen and hydrogen, do not produce other pollutants in the electrolysis process, not only green, and obviously reduced complexity and the environmental pollution's of raw coal system methyl alcohol in-process problem, the purity and the productivity of methyl alcohol have been improved.
The embodiments described above are some, but not all embodiments of the present invention. The detailed description of the embodiments of the present invention 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 efforts belong to the protection scope of the present invention.
Claims (10)
1. A device for preparing methanol from synthesis gas without a shift system is characterized by comprising: the electrolytic water unit, coal gasification unit, the purification unit, compression unit and methyl alcohol synthesis unit, the oxygen export of electrolytic water unit with the oxygen entry of coal gasification unit is connected, the synthetic gas export of coal gasification unit with the synthetic gas entry of purification unit is connected, the purification gas export of purification unit with the purification gas entry of compression unit is connected, the hydrogen outlet of electrolytic water unit with the hydrogen entry of compression unit is connected, the compression gas export of compression unit with the compression gas entry of methyl alcohol synthesis unit is connected.
2. The shift-system-free synthesis gas-to-methanol device according to claim 1, further comprising a separation purification unit and a purge gas hydrogen-stripping unit, wherein the methanol purge gas outlet of the methanol synthesis unit is connected to the inlet of the separation purification unit, and the outlet of the separation purification unit is connected to the inlet of the purge gas hydrogen-stripping unit.
3. The device for preparing the methanol from the synthesis gas without the shift conversion system as claimed in claim 2, wherein the separation and purification unit comprises a gas-liquid separator, a heat exchanger and a membrane separator which are connected in sequence.
4. The shift-system-free syngas to methanol plant of claim 2 wherein the purge gas hydrogen-extraction outlet of the purge gas hydrogen-extraction unit is connected to the purge gas hydrogen-extraction inlet of the compression unit.
5. The shift-system-free synthesis gas methanol plant according to claim 4, further comprising a methanol rectification unit, wherein the crude methanol outlet of the methanol synthesis unit is connected with the crude methanol inlet of the methanol rectification unit.
6. The shift-less system synthesis gas methanol-making device according to claim 5, further comprising a boiler, wherein the flash steam discharged from the methanol rectification unit and the desorbed gas discharged from the purge gas hydrogen-stripping unit are mixed into a mixed gas line, and the mixed gas line is connected with the boiler.
7. The shift-system-less syngas to methanol plant of any one of claims 1-6 further comprising a transfer line disposed between the inlet and outlet of the different units.
8. The shift-less system syngas methanol plant of claim 7, further comprising a pressure gauge disposed on the transfer line between different units.
9. The shift-less system syngas to methanol plant of claim 7 further comprising a flow meter disposed on the transfer line between different units.
10. The shift-less system syngas to methanol plant of claim 7 further comprising valves disposed on the transfer lines between different units.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2021253370A1 (en) * | 2020-06-19 | 2021-12-23 | 周连惠 | System and method for preparing methanol |
| WO2023126620A1 (en) | 2021-12-30 | 2023-07-06 | Johnson Matthey Davy Technologies Limited | Method of producing methanol |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2021253370A1 (en) * | 2020-06-19 | 2021-12-23 | 周连惠 | System and method for preparing methanol |
| WO2023126620A1 (en) | 2021-12-30 | 2023-07-06 | Johnson Matthey Davy Technologies Limited | Method of producing methanol |
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