CN115849400B - Ammonia synthesis process taking mixed gas as raw material - Google Patents
Ammonia synthesis process taking mixed gas as raw material Download PDFInfo
- Publication number
- CN115849400B CN115849400B CN202211695593.9A CN202211695593A CN115849400B CN 115849400 B CN115849400 B CN 115849400B CN 202211695593 A CN202211695593 A CN 202211695593A CN 115849400 B CN115849400 B CN 115849400B
- Authority
- CN
- China
- Prior art keywords
- methanol
- gas
- ammonia
- synthesis
- raw material
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 title claims abstract description 171
- 238000000034 method Methods 0.000 title claims abstract description 122
- 229910021529 ammonia Inorganic materials 0.000 title claims abstract description 75
- 239000002994 raw material Substances 0.000 title claims abstract description 47
- 230000015572 biosynthetic process Effects 0.000 title claims abstract description 36
- 238000003786 synthesis reaction Methods 0.000 title claims abstract description 36
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims abstract description 336
- 239000007789 gas Substances 0.000 claims abstract description 132
- HSFWRNGVRCDJHI-UHFFFAOYSA-N alpha-acetylene Natural products C#C HSFWRNGVRCDJHI-UHFFFAOYSA-N 0.000 claims abstract description 35
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 34
- 125000002534 ethynyl group Chemical group [H]C#C* 0.000 claims abstract description 32
- 238000005984 hydrogenation reaction Methods 0.000 claims abstract description 25
- 238000000746 purification Methods 0.000 claims abstract description 21
- 238000001179 sorption measurement Methods 0.000 claims abstract description 14
- 239000003245 coal Substances 0.000 claims abstract description 13
- 238000005406 washing Methods 0.000 claims abstract description 13
- 238000006243 chemical reaction Methods 0.000 claims abstract description 12
- 239000003345 natural gas Substances 0.000 claims abstract description 12
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 10
- 238000005261 decarburization Methods 0.000 claims abstract description 10
- 239000001257 hydrogen Substances 0.000 claims abstract description 8
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 8
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 7
- 238000000197 pyrolysis Methods 0.000 claims abstract description 7
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 5
- 230000023556 desulfurization Effects 0.000 claims abstract description 5
- 238000002309 gasification Methods 0.000 claims abstract description 5
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 5
- 238000002360 preparation method Methods 0.000 claims abstract description 4
- 239000002002 slurry Substances 0.000 claims abstract description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 4
- 230000006835 compression Effects 0.000 claims abstract description 3
- 238000007906 compression Methods 0.000 claims abstract description 3
- 230000001105 regulatory effect Effects 0.000 claims description 9
- 230000002194 synthesizing effect Effects 0.000 claims description 9
- 239000000203 mixture Substances 0.000 claims 4
- 230000009286 beneficial effect Effects 0.000 abstract description 2
- 239000003034 coal gas Substances 0.000 description 8
- FFBHFFJDDLITSX-UHFFFAOYSA-N benzyl N-[2-hydroxy-4-(3-oxomorpholin-4-yl)phenyl]carbamate Chemical compound OC1=C(NC(=O)OCC2=CC=CC=C2)C=CC(=C1)N1CCOCC1=O FFBHFFJDDLITSX-UHFFFAOYSA-N 0.000 description 6
- 238000004519 manufacturing process Methods 0.000 description 5
- 238000011144 upstream manufacturing Methods 0.000 description 4
- 239000006227 byproduct Substances 0.000 description 3
- 238000005265 energy consumption Methods 0.000 description 3
- 239000012535 impurity Substances 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 238000005336 cracking Methods 0.000 description 1
- 238000005520 cutting process Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 230000002035 prolonged effect Effects 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
A synthesis ammonia process using mixed gas as raw material relates to the technical field of synthesis ammonia process, which comprises the following steps: the method comprises a methanol process and a synthetic ammonia process, wherein the methanol process takes coal as a raw material, and the coal is prepared into methanol through the working procedures of coal water slurry preparation, gasification, conversion, low-temperature methanol washing and methanol synthesis; the synthesis ammonia process takes acetylene tail gas prepared by natural gas pyrolysis as a raw material, high-purity hydrogen is prepared by compression of the acetylene tail gas, desulfurization, hydrogenation, medium-low temperature conversion, decarburization and pressure swing adsorption processes, liquid ammonia is prepared by methanation and synthesis processes of the high-purity hydrogen and the pure nitrogen, and the hydrogenation comprises primary hydrogenation and secondary hydrogenation; the methanol purification gas is obtained after the low-temperature methanol washing procedure of the methanol process and is merged into a first-stage hydrogenation inlet of the synthetic ammonia process through a pipeline. The invention has the beneficial effects that: the methanol process and the ammonia synthesis process can be effectively combined, the ton ammonia feed gas consumption of the liquid ammonia product can be greatly reduced, and the productivity is improved.
Description
Technical Field
The invention relates to the technical field of ammonia synthesis processes, in particular to an ammonia synthesis process taking mixed gas as a raw material.
Background
In the chemical industry, the raw material of the ammonia synthesis process is generally coal or natural gas, the synthesis gas is prepared by coal gasification or natural gas conversion, and the synthesis gas is purified and synthesized to prepare ammonia. In the joint production of synthetic ammonia and methanol, the synthetic ammonia is generally adopted to co-produce the methanol, and a part of process gas is separated from a conversion procedure of the synthetic ammonia process and used as methanol synthesis gas to produce the methanol, so that the conversion gas meets the process requirements of the synthetic ammonia and the methanol, and the operation difficulty of the conversion procedure is high, the equipment investment is high, and a synthetic ammonia process system and a methanol process system are seriously affected with each other; the traditional synthetic ammonia process and the methanol process are single in raw materials, generally coal or natural gas is used as raw materials, by-product tail gas of acetylene is used as raw materials for preparing ammonia by cracking natural gas, liquid ammonia product raw material gas is high in ton ammonia consumption of acetylene tail gas, and the method is generally as follows: 2350-2395NM 3/ton ammonia.
Disclosure of Invention
Aiming at the defects of the prior art, the invention provides a synthesis ammonia process using mixed gas as a raw material, so as to solve the technical problems.
The invention provides a synthesis ammonia process using mixed gas as a raw material, which comprises the following steps: the method comprises a methanol process and a synthetic ammonia process, wherein the methanol process takes coal as a raw material, and the coal is prepared into methanol through the working procedures of coal water slurry preparation, gasification, conversion, low-temperature methanol washing and methanol synthesis; the synthesis ammonia process takes acetylene tail gas prepared by natural gas pyrolysis as a raw material, high-purity hydrogen is prepared by compression of the acetylene tail gas, desulfurization, hydrogenation, medium-low temperature conversion, decarburization and pressure swing adsorption processes, liquid ammonia is prepared by methanation and synthesis processes of the high-purity hydrogen and the pure nitrogen, and the hydrogenation comprises primary hydrogenation and secondary hydrogenation; the methanol purification gas is obtained after the low-temperature methanol washing procedure of the methanol process and is merged into a first-stage hydrogenation inlet of the synthetic ammonia process through a pipeline.
Thus, the mixed gas of acetylene tail gas and methanol purified gas with any proportion can be used as raw materials to produce liquid ammonia, and the acetylene tail gas or the methanol purified gas can be independently used to produce liquid ammonia.
The pipeline of the methanol purification gas is provided with a flowmeter, a separator, an emptying valve, a cut-off valve, a pressure regulating valve, a manual gate valve, a check valve and a heater, wherein the separator is arranged behind the flowmeter and used for separating liquid entrained in the methanol purification gas; an air release valve is arranged behind the separator and is used for releasing pressure of a methanol purification gas pipeline; a cut-off valve is arranged behind the emptying valve and is used for cutting off the synthetic ammonia raw material; a pressure regulating valve is arranged behind the cut-off valve and can control the pressure of the methanol purification gas so as to meet the process requirement of the synthetic ammonia; a manual valve is arranged behind the pressure regulating valve, a check valve is arranged behind the manual valve, and the check valve is used for preventing acetylene tail gas from flowing back to the methanol gas pipeline after the pressure of the methanol gas pipeline is relieved;
the back of the check valve on the methanol purification gas line is provided with a heater which is used for improving the temperature of the methanol purification gas and meeting the requirements of the synthetic ammonia process.
The pressure swing adsorption process of the synthetic ammonia process is provided with a bypass pipeline, the main task of the pressure swing adsorption process of the synthetic ammonia process is to remove CH 4, a small amount of CO, CO 2、C2H6、H2O、N2 and other impurity gases in the purification gas of the upstream decarburization process, when the raw material of the synthetic ammonia process is methanol purification gas, the H 2 content in the purification gas of the decarburization process is up to more than 98.5%, and because the methane content in the methanol purification gas is low, the synthetic ammonia process can cross the pressure swing adsorption process, and the purification gas of the decarburization process of the synthetic ammonia process is directly sent to the methanation process through the newly added bypass pipeline, so that the energy consumption of the synthetic ammonia can be greatly reduced.
The methanol purifying gas obtained after the low-temperature methanol washing procedure of the methanol process comprises the following components: 0.14% of H 2:66.29％、CO:30.71％、CO2:2.50％、CH4:0.03％、N2% and 0.32% of Ar. The pressure of the methanol purification gas after the low-temperature methanol washing process of the coal gas methanol process is 4.6-5.4MPa.G, and the temperature is 0-30 ℃;
the acetylene tail gas prepared by natural gas pyrolysis comprises the following components in percentage by weight ：H2:62.569％、CO:30.156％、CO2:3.57％、CH4:2.67％、N2:0.13％、Ar:0.104％、O2:0.204％、H2O:0.34％、C2H4:0.217％、C2H2:0.018％;
The components of the acetylene tail gas and the components of the methanol purified gas are similar, the methanol purified gas pressure meets the requirements of the synthetic ammonia process, but the temperature of the methanol purified gas is lower, and the part of the methanol purified gas after the temperature is improved is integrated into a first-stage hydrogenation inlet of the synthetic ammonia process, so that the production of liquid ammonia by taking the mixed gas of any proportion of the acetylene tail gas and the methanol purified gas as raw materials can be realized, and the liquid ammonia can also be produced by independently using the acetylene tail gas or the methanol purified gas; according to the operation condition of the upstream raw material device for synthesizing ammonia, the liquid ammonia can be produced by switching raw materials at any time, the operation elasticity of the device is improved, and an acetylene tail gas ammonia synthesis process system and a coal gas methanol process system are not affected.
The invention has the beneficial effects that:
1. The mixed gas of the acetylene tail gas and the coal gas methanol purified gas is used as the raw material to produce the liquid ammonia, so that the methanol process and the synthetic ammonia process can be effectively combined, the ton ammonia raw material gas consumption of a liquid ammonia product can be greatly reduced, and the productivity is improved;
2. According to the price of coal or natural gas raw materials, more economic raw materials can be selected to produce liquid ammonia, so that the production cost is reduced, and the economic benefit is maximized;
3. the device has high operation flexibility, two raw materials of acetylene tail gas and methanol purified gas can be prepared in any proportion, when the supply of one raw material is interrupted in production, the device can not stop the raw material, and the continuous operation period of the device is prolonged;
4. When the methanol purified gas is used as raw material in the ammonia synthesis process, the pressure swing adsorption process of the local unit can be selected to greatly reduce the energy consumption of the ammonia synthesis.
Drawings
FIG. 1 is a process flow diagram of the present invention;
In the figure: 1. methanol process, 2, ammonia synthesis process, 3, methanol purified gas, 4, flowmeter, 5, separator, 6, blow-down valve, 7, cut-off valve, 8, pressure regulating valve, 9, manual gate valve, 10, check valve, 11, heater.
Detailed Description
Example 1
As shown in fig. 1, the present invention provides a process 2 for synthesizing ammonia using a mixed gas as a raw material, which comprises the following steps: the method comprises a methanol process 1 and a synthetic ammonia process 2, wherein the methanol process 1 takes coal as a raw material, and the coal is prepared into methanol through the working procedures of coal water slurry preparation, gasification, conversion, low-temperature methanol washing and methanol synthesis; the synthesis ammonia process 2 takes acetylene tail gas prepared by natural gas pyrolysis as a raw material, the acetylene tail gas is subjected to the procedures of desulfurization, hydrogenation, medium-low temperature conversion, decarburization and pressure swing adsorption to prepare high-purity hydrogen, the high-purity hydrogen and the pure nitrogen are subjected to the procedures of methanation and synthesis to prepare liquid ammonia, and the hydrogenation comprises primary hydrogenation and secondary hydrogenation; the low-temperature methanol washing procedure of the methanol process 1 is carried out to obtain methanol purified gas 3, and the methanol purified gas 3 is merged into a first-stage hydrogenation inlet of the synthetic ammonia process 2 through a pipeline; the mixed gas of acetylene tail gas and methanol purifying gas 3 with any proportion is used as a raw material to produce liquid ammonia, and the acetylene tail gas or the methanol purifying gas 3 can be independently used to produce liquid ammonia;
The pipeline of the methanol purification gas 3 is provided with a flowmeter 4, a separator 5, a vent valve 6, a cut-off valve 7, a pressure regulating valve 8, a manual gate valve 9, a check valve 10 and a heater, the separator 5 is arranged behind the flowmeter 4, and the separator 5 separates liquid entrained in the methanol purification gas 3; a vent valve 6 and a cut-off valve 7 are arranged behind the separator 5, and the vent valve 6 is used for pressure relief of a pipeline of the methanol purified gas 3; the shut-off valve 7 is used for shutting off the synthetic ammonia raw material; the pressure regulating valve 8 is arranged behind the cut-off valve 7, and the pressure regulating valve 8 can control the pressure of the methanol purifying gas 3 so as to meet the requirement of the ammonia synthesis process 2; a manual valve 9 is arranged behind the pressure regulating valve 8, a check valve 10 is arranged behind the manual valve 9, and the check valve 10 is used for preventing acetylene tail gas from flowing back to the methanol gas pipeline after the methanol gas pipeline is depressurized;
A heater is arranged behind the check valve 10 on the pipeline of the methanol purifying gas 3 and is used for increasing the temperature of the methanol purifying gas 3 and meeting the requirement of the synthetic ammonia process 2;
The pressure swing adsorption process of the synthetic ammonia process 2 is provided with a bypass pipeline, the main task of the pressure swing adsorption process of the synthetic ammonia process 2 is to remove CH 4, a small amount of CO, CO 2、C2H6、H2O、N2 and other impurity gases in the purifying gas of the upstream decarburization process, when the raw material of the synthetic ammonia process 2 is the methanol purifying gas 3, the H 2 content in the purifying gas of the decarburization process is up to more than 98.5%, and because the methane content in the methanol purifying gas 3 is low, the synthetic ammonia process 2 can cross the pressure swing adsorption process, and the purifying gas of the decarburization process of the synthetic ammonia process 2 is directly sent to the methanation process through the newly added bypass pipeline, so that the energy consumption of the synthetic ammonia can be greatly reduced;
The methanol purified gas 3 obtained after the low-temperature methanol washing procedure of the methanol process 1 comprises the following components: 0.14% of H 2:66.29％、CO:30.71％、CO2:2.50％、CH4:0.03％、N2% and 0.32% of Ar. The pressure of the methanol purifying gas 3 after the low-temperature methanol washing procedure of the coal gas methanol process 1 is 4.6-5.4MPa.G, and the temperature is 0-30 ℃;
The acetylene tail gas component prepared by natural gas pyrolysis is as follows ：H2:62.569％、CO:30.156％、CO2:3.57％、CH4:2.67％、N2:0.13％、Ar:0.104％、O2:0.204％、H2O:0.34％、C2H4:0.217％、C2H2:0.018％;
The components of the acetylene tail gas and the components of the methanol purified gas 3 are similar, the pressure of the methanol purified gas 3 meets the requirement of the synthesis ammonia process 2, but the temperature of the methanol purified gas 3 is lower, and a part of the methanol purified gas 3 after the temperature is increased is integrated into a first-stage hydrogenation inlet of the synthesis ammonia process 2, so that the production of liquid ammonia by taking the mixed gas of any proportion of the acetylene tail gas and the methanol purified gas 3 as raw materials can be realized, and the liquid ammonia can also be produced by independently using the acetylene tail gas or the methanol purified gas 3; according to the operation condition of an upstream raw material device for synthesizing ammonia, the liquid ammonia can be produced by switching raw materials at any time, the operation elasticity of the device is improved, and an acetylene tail gas ammonia synthesis process 2 system and a coal gas methanol process 1 system are not affected;
Specifically, when the methanol purified gas 3 is used as a raw material to produce liquid ammonia, a raw material gas compressor of the synthesis ammonia process 2 is required to be stopped, an inlet of a desulfurization tank is closed, the methanol purified gas 3 is prevented from flowing back to the raw material gas compressor, and overpressure of a low-pressure cylinder of the raw material gas compressor occurs; the temperature of the first-stage hydrogenation inlet of the ammonia synthesis process 2 is lower, and a heater for the methanol purifying gas 3 is used to ensure the temperature of the first-stage hydrogenation inlet.
In the process 2 for synthesizing ammonia by taking the mixed gas of acetylene tail gas and methanol purified gas 3 as raw materials, the content of H 2 in the pressure swing adsorption byproduct tail gas is increased, and a proper amount of low-pressure nitrogen is required to be added into the pressure swing adsorption byproduct tail gas, so that the safety risk is reduced.
Claims (5)
1. A process for synthesizing ammonia by using mixed gas as a raw material is characterized in that: the method comprises a methanol process and a synthetic ammonia process, wherein the methanol process takes coal as a raw material, and the coal is prepared into methanol through the working procedures of coal water slurry preparation, gasification, conversion, low-temperature methanol washing and methanol synthesis; the synthesis ammonia process takes acetylene tail gas prepared by natural gas pyrolysis as a raw material, high-purity hydrogen is prepared by compression of the acetylene tail gas, desulfurization, hydrogenation, medium-low temperature conversion, decarburization and pressure swing adsorption processes, liquid ammonia is prepared by methanation and synthesis processes of the high-purity hydrogen and the pure nitrogen, and the hydrogenation comprises primary hydrogenation and secondary hydrogenation; the low-temperature methanol washing process of the methanol process is followed by obtaining methanol purified gas, and the methanol purified gas is merged into a first-stage hydrogenation inlet of the synthetic ammonia process through a pipeline; the components of the acetylene tail gas are similar to the components of the methanol purification gas, the methanol purification gas is integrated into a first-stage hydrogenation inlet of the synthetic ammonia process after the temperature of the methanol purification gas is increased, and the mixed gas of the acetylene tail gas and the methanol purification gas is used as a raw material to produce liquid ammonia.
2. The process for synthesizing ammonia from a gas mixture according to claim 1, wherein: the methanol purifying device comprises a methanol purifying gas pipeline, a flow meter, a separator, an emptying valve, a shut-off valve, a pressure regulating valve, a manual gate valve, a check valve and a heater, wherein the separator is arranged behind the flow meter; and a heater is arranged behind the check valve on the methanol purification gas pipeline.
3. The process for synthesizing ammonia from a gas mixture according to claim 1, wherein: the pressure swing adsorption process of the ammonia synthesis process is provided with a bypass pipeline.
4. The process for synthesizing ammonia from a gas mixture according to claim 1, wherein: the components of the methanol purified gas obtained after the low-temperature methanol washing procedure of the methanol process are as follows: 0.14% of H 2:66.29％、CO:30.71％、CO2:2.50％、CH4:0.03％、N2% and 0.32% of Ar.
5. The process for synthesizing ammonia from a gas mixture according to claim 4, wherein: the components of the acetylene tail gas prepared by natural gas pyrolysis are as follows ：H2:62.569％、CO:30.156％、CO2:3.57％、CH4:2.67％、N2:0.13％、Ar:0.104％、O2:0.204％、H2O:0.34％、C2H4:0.217％、C2H2:0.018％.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202211695593.9A CN115849400B (en) | 2022-12-28 | 2022-12-28 | Ammonia synthesis process taking mixed gas as raw material |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202211695593.9A CN115849400B (en) | 2022-12-28 | 2022-12-28 | Ammonia synthesis process taking mixed gas as raw material |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN115849400A CN115849400A (en) | 2023-03-28 |
| CN115849400B true CN115849400B (en) | 2024-04-26 |
Family
ID=85655458
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202211695593.9A Active CN115849400B (en) | 2022-12-28 | 2022-12-28 | Ammonia synthesis process taking mixed gas as raw material |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN115849400B (en) |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2014127913A2 (en) * | 2013-02-21 | 2014-08-28 | Faramarz Bairamijamal | High pressure process for co2 capture, utilization for heat recovery, power cycle, super-efficient hydrogen based fossil power generation and conversion of liquid co2 with water to syngas and oxygen |
| CN106672898A (en) * | 2017-01-17 | 2017-05-17 | 青海盐湖工业股份有限公司 | Method for synthesizing ammonia by taking byproduct tail gas in process of producing acetylene by pyrolyzing natural gas as raw material |
-
2022
- 2022-12-28 CN CN202211695593.9A patent/CN115849400B/en active Active
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2014127913A2 (en) * | 2013-02-21 | 2014-08-28 | Faramarz Bairamijamal | High pressure process for co2 capture, utilization for heat recovery, power cycle, super-efficient hydrogen based fossil power generation and conversion of liquid co2 with water to syngas and oxygen |
| CN106672898A (en) * | 2017-01-17 | 2017-05-17 | 青海盐湖工业股份有限公司 | Method for synthesizing ammonia by taking byproduct tail gas in process of producing acetylene by pyrolyzing natural gas as raw material |
Non-Patent Citations (3)
| Title |
|---|
| 600kt/a醇氨联产装置净化工艺方案比较及选择;许慎永;宋玉国;周梦远;曹广法;;化工设计通讯(第05期);第9-14页 * |
| 天然气裂解制乙炔尾气用于生产合成氨工艺改进;李辉林;高雁;李光辉;吴泽培;;大氮肥(第02期);第123-125页 * |
| 榆林60×10~4t/a煤制甲醇工艺技术;王明峰;陈立新;;煤气与热力(第06期);第68-71页 * |
Also Published As
| Publication number | Publication date |
|---|---|
| CN115849400A (en) | 2023-03-28 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN104449920B (en) | The method utilizing coke-stove gas and blast furnace gas Joint Production natural gas with liquefied ammonia | |
| CN103524299B (en) | A kind of synthesizing methanol and synthesizing methane cogeneration facility | |
| CN102942972B (en) | Method for producing liquefied natural gas by coke oven gas | |
| CN109020780B (en) | System and method for preparing methanol by coal gasification coupled coal coking | |
| CN102517086A (en) | Method for using carbon dioxide as delivery gas and back flushing gas of coal powder instead of nitrogen in coal gasification methanol preparation process | |
| CN113735060A (en) | System for regulating hydrogen-carbon ratio of synthesis gas and simultaneously producing hydrogen by coupling membrane separation and pressure swing adsorption | |
| CN107446635B (en) | Novel coke oven gas utilization method | |
| CN115849400B (en) | Ammonia synthesis process taking mixed gas as raw material | |
| CN108384572B (en) | Method and system for adjusting hydrogen-carbon ratio of Fischer-Tropsch synthesis gas co-production hydrogen | |
| CN104193585A (en) | System and process for preparing methyl alcohol through coke-oven gas-assisted coal gasification | |
| CN102180767A (en) | Method and device for jointly producing methanol, ammonia and acetic acid by using coal and natural gas | |
| CN103881780A (en) | Process of preparing liquefied natural gas by supplementing carbon dioxide with coke-oven gas | |
| CN209854029U (en) | Device for preparing methanol from synthesis gas without conversion system | |
| CN212374896U (en) | System for retrieve low temperature methyl alcohol washing air | |
| CN110002954B (en) | Technological method and device for preparing methanol and co-producing acid or ester by coal gasification coupled coal coking | |
| CN108046986B (en) | Recycling system and recycling method for effective gas in coal-to-ethylene glycol process | |
| CN211921378U (en) | System for steel mill tail gas comprehensive utilization system ethanol | |
| CN110002956B (en) | Process method and device for preparing methanol and co-producing ethanol and LNG from coal-based synthesis gas and coke oven gas | |
| CN204058302U (en) | A kind of coke(oven)gas assists the system of gasification methyl alcohol | |
| CN111017956B (en) | System for recycling low-temperature methanol washing air and operation method | |
| CN216512858U (en) | System for regulating hydrogen-carbon ratio of synthesis gas by coupling membrane separation and pressure swing adsorption | |
| CN210595854U (en) | Process device for preparing methanol coproduction acid or ester by coal gasification coupled coal coking | |
| CN109776261B (en) | Method and system for directly preparing alcohol from coke oven gas | |
| CN109847555B (en) | Device and method for recovering multiple gases in catalytic dry gas based on hydrate method | |
| CN113860991A (en) | Ammonia and alcohol co-production method for realizing low-carbon emission by combining photocatalysis with coal gas production |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |