CN109553508B - Device and method for producing methanol by directly reforming raw coke oven gas with water vapor - Google Patents
Device and method for producing methanol by directly reforming raw coke oven gas with water vapor Download PDFInfo
- Publication number
- CN109553508B CN109553508B CN201910045582.8A CN201910045582A CN109553508B CN 109553508 B CN109553508 B CN 109553508B CN 201910045582 A CN201910045582 A CN 201910045582A CN 109553508 B CN109553508 B CN 109553508B
- Authority
- CN
- China
- Prior art keywords
- gas
- pipeline
- heat exchange
- temperature
- enters
- 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
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 title claims abstract description 207
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 59
- 239000000571 coke Substances 0.000 title claims abstract description 50
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 32
- 238000002407 reforming Methods 0.000 title claims abstract description 10
- 239000007789 gas Substances 0.000 claims abstract description 231
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 89
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 89
- 239000001301 oxygen Substances 0.000 claims abstract description 89
- 230000003197 catalytic effect Effects 0.000 claims abstract description 47
- 230000015572 biosynthetic process Effects 0.000 claims abstract description 39
- 238000003786 synthesis reaction Methods 0.000 claims abstract description 39
- 238000000034 method Methods 0.000 claims abstract description 37
- 238000000746 purification Methods 0.000 claims abstract description 22
- 229910052799 carbon Inorganic materials 0.000 claims abstract description 15
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 13
- 239000002994 raw material Substances 0.000 claims abstract description 10
- 239000002351 wastewater Substances 0.000 claims abstract description 8
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 4
- 230000023556 desulfurization Effects 0.000 claims abstract description 4
- 238000001833 catalytic reforming Methods 0.000 claims description 33
- 239000002918 waste heat Substances 0.000 claims description 21
- 239000000047 product Substances 0.000 claims description 19
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims description 18
- 229910052717 sulfur Inorganic materials 0.000 claims description 18
- 239000011593 sulfur Substances 0.000 claims description 18
- 239000000428 dust Substances 0.000 claims description 16
- 239000006227 byproduct Substances 0.000 claims description 13
- 238000006057 reforming reaction Methods 0.000 claims description 13
- 229920006395 saturated elastomer Polymers 0.000 claims description 12
- 150000001875 compounds Chemical class 0.000 claims description 9
- XFXPMWWXUTWYJX-UHFFFAOYSA-N Cyanide Chemical compound N#[C-] XFXPMWWXUTWYJX-UHFFFAOYSA-N 0.000 claims description 6
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N phenol group Chemical group C1(=CC=CC=C1)O ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 claims description 6
- 239000008234 soft water Substances 0.000 claims description 6
- 238000000629 steam reforming Methods 0.000 claims description 6
- 239000011449 brick Substances 0.000 claims description 3
- 238000002485 combustion reaction Methods 0.000 claims description 3
- 229910052739 hydrogen Inorganic materials 0.000 claims description 3
- 239000005416 organic matter Substances 0.000 claims description 3
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 abstract description 18
- UFWIBTONFRDIAS-UHFFFAOYSA-N Naphthalene Chemical compound C1=CC=CC2=CC=CC=C21 UFWIBTONFRDIAS-UHFFFAOYSA-N 0.000 abstract description 8
- 238000006243 chemical reaction Methods 0.000 abstract description 6
- 239000011280 coal tar Substances 0.000 abstract description 5
- 239000000126 substance Substances 0.000 abstract description 5
- 238000012824 chemical production Methods 0.000 abstract 1
- 239000000203 mixture Substances 0.000 description 7
- 239000011269 tar Substances 0.000 description 7
- 239000003054 catalyst Substances 0.000 description 6
- 238000004939 coking Methods 0.000 description 6
- 230000006835 compression Effects 0.000 description 5
- 238000007906 compression Methods 0.000 description 5
- 230000003009 desulfurizing effect Effects 0.000 description 4
- 238000010438 heat treatment Methods 0.000 description 4
- 231100000572 poisoning Toxicity 0.000 description 3
- 230000000607 poisoning effect Effects 0.000 description 3
- 238000002360 preparation method Methods 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- 238000001035 drying Methods 0.000 description 2
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 1
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 238000013459 approach Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000008021 deposition Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 229910001882 dioxygen Inorganic materials 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 150000004820 halides Chemical class 0.000 description 1
- 229910052736 halogen Inorganic materials 0.000 description 1
- 150000002367 halogens Chemical class 0.000 description 1
- 239000010842 industrial wastewater Substances 0.000 description 1
- 239000010808 liquid waste Substances 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 238000011027 product recovery Methods 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 230000004083 survival effect Effects 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/15—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively
- C07C29/151—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases
- C07C29/152—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases characterised by the reactor used
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
- C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/02—Processes for making hydrogen or synthesis gas
- C01B2203/0205—Processes for making hydrogen or synthesis gas containing a reforming step
- C01B2203/0211—Processes for making hydrogen or synthesis gas containing a reforming step containing a non-catalytic reforming step
- C01B2203/0216—Processes for making hydrogen or synthesis gas containing a reforming step containing a non-catalytic reforming step containing a non-catalytic steam reforming step
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/06—Integration with other chemical processes
- C01B2203/061—Methanol production
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/08—Methods of heating or cooling
- C01B2203/0805—Methods of heating the process for making hydrogen or synthesis gas
- C01B2203/0811—Methods of heating the process for making hydrogen or synthesis gas by combustion of fuel
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/12—Feeding the process for making hydrogen or synthesis gas
- C01B2203/1205—Composition of the feed
- C01B2203/1211—Organic compounds or organic mixtures used in the process for making hydrogen or synthesis gas
- C01B2203/1235—Hydrocarbons
-
- 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
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
-
- 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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
Abstract
The invention discloses a device and a method for producing methanol by directly reforming raw coke oven gas by steam. Directly feeding the high-temperature raw gas from the coke oven into a non-catalytic reformer, firstly reacting with oxygen to raise the temperature to 1300-1500 ℃, and then reforming with water vapor to generate H 2 The synthesis gas mainly containing CO is used for producing methanol after being subjected to purification treatment such as desulfurization and the like. The invention fully utilizes the sensible heat and the high-temperature steam resources of the raw gas, and realizes the complete conversion of coal tar, benzene, naphthalene and other carbon-containing organic matters in the raw gas at high temperature to produce the synthesis gas, thereby solving the problems of complex process flow, large amount of phenol-cyanogen-containing wastewater which is difficult to treat and the like in the traditional chemical production process. In addition, after the raw coke oven gas is used as raw materials by a non-catalytic conversion method, redundant carbon in chemical products such as coal tar, benzene and the like can make up for the problem of insufficient carbon in the clean gas, and the hydrogen-carbon ratio is improved, so that the methanol yield is improved.
Description
Technical Field
The invention belongs to the field of energy and chemical industry, and particularly relates to a device and a method for producing methanol by directly reforming raw coke oven gas by water vapor.
Background
China is the largest coke production and export country in the world, and coke oven gas which is a byproduct in the coking industry is already a large-tonnage energy source and chemical industry resource. How to carry out high-value comprehensive utilization on raw coke oven gas has become a key problem for survival and development of coking enterprises. At present, the preparation of synthesis gas from coke oven gas and the production of methanol become one of the modes of comprehensive utilization of coke oven gas in China. Reforming reactions for producing synthesis gas from coke oven gas generally have two approaches. Firstly, steam reforming and secondly carbon dioxide reforming, but both the two process routes need to purify the coke oven raw gas, namely, the raw gas is firstly cooled and then subjected to the procedures of electrical tar capturing, ammonia removal, naphthalene removal, benzene washing, desulfurization and the like. Sulfide, halide, tar and the like in the purified gas are reduced to very low levels. So as to prevent carbon precipitation, sulfur and halogen poisoning of the catalyst. The purification and chemical product recovery process of the raw coke oven gas is the most important pollutant emission source of a coke oven plant, particularly the generated phenolic cyanide-containing wastewater, has complex components and is the most difficult industrial wastewater to treat. In a word, the two processes have the defects of long process flow, large equipment investment, large environmental pollution and low energy utilization efficiency.
The prior purifying process flow for preparing the synthetic gas from the conventional coke oven gas is long, and the high-temperature sensible heat of the raw coke oven gas and the latent heat of steam in the raw coke oven gas are not effectively utilized, so that huge waste of energy is caused. The non-catalytic conversion method is used for preparing the synthesis gas from the coke oven raw gas, so that the high temperature and water vapor resources can be fully utilized. Directly converting the coal tar, benzene, naphthalene and other carbon-containing organic matters in the raw gas into useful components such as synthesis gas. The problems of long process flow, serious pollution, carbon deposition poisoning of the catalyst in the catalytic conversion process and the like existing in the conventional preparation of the synthesis gas are avoided. In addition, after the raw coke oven gas is used as raw materials by a non-catalytic conversion method, redundant carbon in chemical products such as coal tar, benzene and the like can make up for the problem of insufficient carbon in the clean gas, and the hydrogen-carbon ratio is improved, so that the methanol yield is improved.
Disclosure of Invention
A device for producing methanol by directly reforming raw coke oven gas through steam comprises a non-catalytic reforming furnace, a heat exchange device, a dust removal device and a methanol production device; the side surface of the top of the non-catalytic reforming furnace is connected with a raw gas collecting pipe, the top of the non-catalytic reforming furnace is connected with a high-temperature steam and oxygen mixed gas pipeline, and the side surface of the bottom of the non-catalytic reforming furnace is connected with a high-temperature gas inlet of a heat exchange device; the low-temperature gas outlet of the heat exchange device is connected with a tangential gas inlet at the side surface of the top of the dust removal device; the gas outlet at the top of the dust removing device is connected with an inlet pipeline of the methanol production device; the outlet of the methanol production device is connected with a methanol product pipeline;
the heat exchange device comprises a heat exchange superheater and a waste heat boiler heat exchange preheater, the heat exchange superheater is connected with a high-temperature steam and oxygen mixed gas pipeline through a superheated steam pipeline and a high-temperature oxygen pipeline, is connected with the waste heat boiler through a saturated steam pipeline and is connected with the heat exchange preheater through a preheated oxygen pipeline, the waste heat boiler is connected with the heat exchange preheater through a preheated boiler water supply pipeline, the heat exchange preheater is respectively connected with a boiler water supply pipeline and an oxygen pipeline, the superheated steam pipeline is connected with the high-temperature steam and oxygen mixed gas pipeline through a pressure reducing valve, and is connected with a byproduct steam pipeline through an adjusting valve;
the methanol production device comprises a cooler, a fan, a purification device, a compressor and a methanol synthesis device, wherein a gas inlet of the cooler is connected with an inlet pipeline, a gas outlet of the cooler is connected with an inlet of the fan, an outlet of the fan is connected with a gas inlet of the purification device, a gas outlet of the purification device is connected with an inlet of the compressor, an outlet of the compressor is connected with a gas inlet of the methanol synthesis device, and an outlet of the methanol synthesis device is connected with a methanol product pipeline.
Preferably, the non-catalytic reforming furnace is internally lined with refractory bricks, the outer wall is of a water jacket structure, the height is 10-30 m, and the ratio of the height to the inner diameter is 2.0-10.0:1.0.
Preferably, the fan in the methanol production device is a Roots fan.
Preferably, the purifying device is a wet desulfurizing device or a dry desulfurizing device.
A method for producing methanol by using the coke oven raw gas to directly steam reform comprises the following process steps:
a. raw coke oven gas with the temperature of 600-800 ℃ from a gas collecting pipe of raw coke oven gas enters the non-catalytic reforming furnace from the top side surface of the non-catalytic reforming furnace, is quickly mixed with steam and oxygen mixed gas sprayed from the top of the non-catalytic reforming furnace and generates high-temperature combustion reaction, so that the temperature in the non-catalytic reforming furnace reaches 1300-1500 ℃ instantly, and carbon-containing organic matters in the raw coke oven gas and steam generate reforming reaction to generate CO and H 2 A predominately syngas;
the residence time of the high-temperature gas in the non-catalytic reformer for reforming reaction is 1.0-10.0 s;
b. the boiler feed water with the pressure of 4MPa from a boiler feed water pipeline firstly enters a heat exchange preheater, is heated to 170-200 ℃ through indirect heat exchange, enters a waste heat boiler through a preheating boiler feed water pipeline to generate saturated water vapor with the pressure of 3-4 MPa, enters a heat exchange superheater through a saturated vapor pipeline to obtain superheated vapor with the pressure of 3-4 MPa and 400-600 ℃ through indirect heat exchange, wherein part of the superheated vapor enters a high-temperature vapor and oxygen mixed gas pipeline through a pressure reducing valve to serve as a raw material for non-catalytic reforming, and the rest of the high-pressure superheated vapor is sent to a required process through an outward-sending byproduct vapor pipeline;
c. oxygen with the pressure of 0.5-2 MPa is conveyed by an oxygen pipeline, firstly enters a heat exchange preheater, is heated to 150-200 ℃ through indirect heat exchange, then enters a heat exchange superheater through a preheating oxygen pipeline, is continuously heated to 400-600 ℃ through indirect heat exchange, and then enters a high-temperature steam and oxygen mixed gas pipeline after passing through a pressure reducing valve;
d. high-temperature synthesis gas coming out of the side surface of the bottom of the non-catalytic reforming furnace enters a heat exchange device, sequentially passes through a heat exchange superheater, a waste heat boiler and a heat exchange preheater, is cooled to 200-250 ℃, and then enters a dust removal device;
e. the synthesis gas at 200-250 ℃ from the dust removing device enters a cooler, and the temperature is reduced to 30-50 ℃ to obtain low-temperature synthesis gas;
f. the low-temperature synthetic gas from the cooler enters a fan to introduce and output the gasDelivering the mixture into a purifying device to remove and purify sulfur-containing compounds in the gas so that the sulfur content in the gas is less than 1mg/m 3 Obtaining ultra-clean gas;
g. the ultra-purified gas from the purification device enters a compressor to be pressurized to 5MPa, then enters a methanol synthesis device to obtain a methanol product, and is sent to the next working procedure through a product pipeline;
preferably, the residence time of the high temperature gas in the non-catalytic reformer in the step (a) is 1.0 to 10.0s.
Preferably, the purity of the oxygen in the step (a) is 99-99.9%, and the molar ratio of steam injected from the top of the non-catalytic reforming furnace to the oxygen is 0.3-5.0:1.
Preferably, the oxygen content of the non-catalytic reformer outlet gas is less than 0.01%.
Preferably, the organic matter content in the outlet gas of the non-catalytic reformer is less than 0.01%.
Preferably, the boiler feed water in step (b) is soft water or coked phenolic cyanide-containing wastewater.
Compared with the prior art, the invention has the beneficial effects that:
1. the raw coke oven gas is adopted to replace the clean coke oven gas, and the coal tar, benzene, naphthalene and other carbon-containing organic matters in the raw coke oven gas are directly and completely converted into useful components such as synthetic gas, so that the complicated coke oven gas production and recovery process is eliminated, and the problems of the generation of coking phenol-cyanogen-containing wastewater and the pollution to the environment are avoided from the source.
2. The invention fully utilizes the high temperature and water vapor resources of the raw coke oven gas and solves the problems of long process flow, serious pollution and carbon deposit poisoning of the catalyst in the catalytic conversion process in the preparation of the synthetic gas by the prior coking process.
3. The invention has the characteristics of short process flow, small equipment investment, high energy utilization efficiency, small pollution, no liquid waste, no need of catalyst, mild common operation condition and the like.
Drawings
FIG. 1 is a schematic diagram of the system of the present invention;
in the figure: 1. a non-catalytic reformer; 2. a heat exchange device; 3. a dust removal device; 4. a superheated steam pipeline; 5. a methanol production device; 6. a blower; 7. a high temperature oxygen pipeline; 8. a cooler; 9-a purifying device, 10, a compressor; 11. preheating a boiler water supply pipeline; 12. a heat exchange superheater; 13. a waste heat boiler; 14. a heat exchange preheater; 15. a methanol synthesis device; 16. raw gas collecting pipe; 17. a high temperature steam and oxygen gas mixture pipeline; 18. a high temperature synthesis gas pipeline; 19. a low temperature synthesis gas pipeline; 20. a saturated steam pipe; 21. preheating an oxygen pipeline; 22. an inlet pipe of the methanol production device 5; 23. a methanol product outlet duct; 24. a boiler feed water pipe; 25. an oxygen pipe; 26. and a byproduct steam pipeline is externally sent.
Detailed Description
A specific embodiment of the present invention will be described in detail with reference to fig. 1.
A device for producing methanol by directly reforming raw coke oven gas by steam comprises a non-catalytic reforming furnace 1, a heat exchange device 2, a dust removal device 3 and a methanol production device 5; the side surface of the top of the non-catalytic reformer 1 is connected with a raw gas collecting pipe 16, the top of the non-catalytic reformer is connected with a high-temperature steam and oxygen mixed gas pipeline 17, and the side surface of the bottom of the non-catalytic reformer is connected with a high-temperature gas inlet 18 of the heat exchange device 2; the low-temperature gas outlet 19 of the heat exchange device 2 is connected with a tangential gas inlet at the side surface of the top of the dust removal device 3; the gas outlet at the top of the dust removing device 3 is connected with an inlet pipeline 22 of the methanol production device 5; the outlet of the methanol production device 5 is connected with a methanol product pipeline 23;
the heat exchange device 2 comprises a heat exchange superheater 12 and a waste heat boiler 13 and heat exchange preheater 14, wherein the heat exchange superheater 12 is connected with a high-temperature steam and oxygen mixed gas pipeline 17 through a superheated steam pipeline 4 and a high-temperature oxygen pipeline 7, is connected with the waste heat boiler 13 through a saturated steam pipeline 20, is connected with the heat exchange preheater 14 through a preheated oxygen pipeline 21, the waste heat boiler 13 is connected with the heat exchange preheater 14 through a preheating boiler water supply pipeline 11, the heat exchange preheater 14 is respectively connected with a boiler water supply pipeline 24 and an oxygen pipeline 25, the superheated steam pipeline 4 is connected with the high-temperature steam and oxygen mixed gas pipeline 17 through a pressure reducing valve, and is connected with a byproduct steam pipeline 26 through an adjusting valve;
the methanol production device 5 comprises a cooler 8, a fan 6, a purification device 9, a compressor 10 and a methanol synthesis device 15, wherein a gas inlet of the cooler 8 is connected with an inlet pipeline 22, a gas outlet of the cooler 8 is connected with an inlet of the fan 6, an outlet of the fan 6 is connected with a gas inlet of the purification device 9, a gas outlet of the purification device 9 is connected with an inlet of the compressor 10, an outlet of the compressor 10 is connected with a gas inlet of the methanol synthesis device 15, and an outlet of the methanol synthesis device 15 is connected with a methanol product pipeline 23.
Preferably, the non-catalytic reforming furnace 1 is internally lined with refractory bricks, the outer wall is of a water jacket structure, the height is 10-30 m, and the ratio of the height to the inner diameter is 2.0-10.0:1.0.
Preferably, the fan 6 in the methanol production device 5 is a Roots blower.
Preferably, the purifying device 9 is a wet desulfurizing device or a dry desulfurizing device.
A method for producing methanol by using the coke oven raw gas to directly steam reform comprises the following process steps:
a. raw coke oven gas with the temperature of 600-800 ℃ from a raw coke gas collecting pipe 16 enters the non-catalytic reformer 1 from the top side surface of the non-catalytic reformer 1, is quickly mixed with steam and oxygen mixed gas sprayed from the top of the non-catalytic reformer 1 and generates high-temperature combustion reaction, so that the temperature in the non-catalytic reformer 1 reaches 1300-1500 ℃ instantly, and carbon-containing organic matters in the raw coke oven gas and steam generate reforming reaction to generate CO and H 2 A predominately syngas;
the residence time of the high-temperature gas in the non-catalytic reformer 1 for reforming reaction is 1.0-10.0 s;
b. the boiler feed water with the pressure of 4MPa from the boiler feed water pipeline 24 firstly enters the heat exchange preheater 14, is heated to 170-200 ℃ through indirect heat exchange, enters the waste heat boiler 13 through the preheating boiler feed water pipeline 11 to generate saturated water vapor with the pressure of 3-4 MPa, enters the heat exchange superheater 12 through the saturated steam pipeline 20 to obtain superheated steam with the pressure of 3-4 MPa and 400-600 ℃ through indirect heat exchange, wherein part of the superheated steam enters the high-temperature steam and oxygen mixed gas pipeline 17 through the pressure reducing valve to serve as a raw material for non-catalytic reforming, and the rest of the high-pressure superheated steam is sent to a required process through the byproduct steam pipeline 26;
c. oxygen with the pressure of 0.5-2 MPa is conveyed by an oxygen pipeline 25, firstly enters a heat exchange preheater 14, is heated to 150-200 ℃ through indirect heat exchange, then enters a heat exchange superheater 12 through a preheating oxygen pipeline 21, is continuously heated to 400-600 ℃ through indirect heat exchange, and then enters a high-temperature steam and oxygen mixed gas pipeline 17 through a pressure reducing valve;
d. the high-temperature synthesis gas coming out of the side surface of the bottom of the non-catalytic reforming furnace 1 enters a heat exchange device 2, sequentially passes through a heat exchange superheater 12, a waste heat boiler 13 and a heat exchange preheater 14, is cooled to 200-250 ℃, and then enters a dust removal device 3;
e. the synthesis gas with the temperature of 200-250 ℃ from the dust removing device 3 enters a cooler 8, and the temperature is reduced to 30-50 ℃ to obtain low-temperature synthesis gas;
f. the low-temperature synthetic gas from the cooler 8 enters the fan 6 to introduce and convey the gas, then enters the purifying device 9 to remove and purify the sulfur-containing compounds in the gas, so that the sulfur content in the gas is less than 1mg/m 3 Obtaining ultra-clean gas;
g. the ultra-purified gas from the purification device 9 enters a compressor 10 to be pressurized to 5MPa, then enters a methanol synthesis device 15 to obtain a methanol product, and is sent to the next working procedure through a product pipeline 23;
preferably, the residence time of the high temperature gas in the step (a) in the non-catalytic reformer 1 for the reforming reaction is 1.0 to 10.0s.
Preferably, the purity of the oxygen in the step (a) is 99-99.9%, and the molar ratio of steam injected into the top of the non-catalytic reformer 1 to the oxygen is 0.3-5.0:1.
Preferably, the oxygen content of the outlet gas of the non-catalytic reformer 1 is less than 0.01%.
Preferably, the organic matter content in the outlet gas of the non-catalytic reformer 1 is less than 0.01%.
Preferably, the boiler feed water in step (b) is soft water or coked phenolic cyanide-containing wastewater.
Example 1
Raw gas at 800 ℃ from a coke oven, dry gas flow rate of 50000Nm 3 And/h, the flow rate of the contained water vapor is 13t/h, and the water vapor directly enters the non-catalytic reforming furnace 1. The non-catalytic reformer 1 had a height of 16m and an inner diameter of 4m. Oxygen line 25 delivers oxygen at a pressure of 0.5MPa and an oxygen flow of 12000Nm 3 And/h, firstly, the mixture enters a heat exchange preheater 14, is heated to 150 ℃ through indirect heat exchange, then enters a heat exchange superheater 12 through a preheated oxygen pipeline 21, is continuously heated to 400 ℃ through indirect heat exchange, and then enters a high-temperature steam and oxygen mixed gas pipeline 17 through a pressure reducing valve. Soft water 120t/h with the pressure of 4MPa from a boiler water supply pipeline 24 firstly enters a heat exchange preheater 14, is heated to 170 ℃ through indirect heat exchange, enters a waste heat boiler 13 through a preheating boiler water supply pipeline 11 to generate saturated water vapor with the pressure of 3MPa, then enters a heat exchange superheater 12 through a saturated steam pipeline 20 to obtain superheated steam with the pressure of 3MPa and 400 ℃ through indirect heat exchange, wherein part of the superheated steam enters high-temperature steam (4 t/h) and an oxygen mixed gas pipeline 17 after passing through a pressure reducing valve to serve as raw materials for non-catalytic reforming, and the rest of the high-pressure superheated steam is sent to a required process through an outward-sending byproduct steam pipeline 26.
After being mixed with oxygen in a pipeline 17, the high-temperature superheated steam directly enters a non-catalytic reformer 1 to reform with raw gas to prepare the synthesis gas with 1300 ℃, the oxygen content in the outlet synthesis gas is less than 0.01%, and the tar content is less than 0.01%. The residence time of the high temperature gas in the non-catalytic reformer 1 for the reforming reaction was 1.5s.
The synthetic gas cooled to 200 ℃ by the heat exchange device 2 is dedusted by the dedusting device 3, and the dedusted synthetic gas at 200 ℃ enters the cooler 8 to reduce the temperature to 30 ℃ to obtain low-temperature synthetic gas. The low-temperature synthetic gas with the temperature of 30 ℃ from the cooler 8 enters the fan 6 to introduce and convey the gas, then enters the purification device 9 to remove and purify the sulfur-containing compound in the gas by wet method, so that the sulfur content in the gas is less than 1mg/m 3 Obtaining the superPurifying the gas. The ultra-purified gas from the purification device 9 enters a compressor 10 for secondary compression to be pressurized to 5MPa, then enters a methanol synthesis device 15 for preparing methanol, and is sent to the next process through a product pipeline 23.
Example 2
Raw gas at 600 ℃ from a coke oven, dry gas flow rate of 60000Nm 3 And/h, the flow rate of the contained water vapor is 27t/h, and the water vapor directly enters the non-catalytic reforming furnace 1. The non-catalytic reformer 1 had a height of 30m and an inner diameter of 6m. Oxygen line 25 delivers oxygen at a pressure of 2MPa and an oxygen flow of 22000Nm 3 And/h, firstly, the mixture enters a heat exchange preheater 14, is heated to 200 ℃ through indirect heat exchange, then enters a heat exchange superheater 12 through a preheated oxygen pipeline 21, is continuously heated to 600 ℃ through indirect heat exchange, and then enters a high-temperature steam and oxygen mixed gas pipeline 17 through a pressure reducing valve. The coking phenolic cyanide-containing wastewater with the pressure of 4MPa from a boiler water supply line 24 enters a heat exchange preheater 14 at first, is heated to 200 ℃ through indirect heat exchange, enters a waste heat boiler 13 through a preheating boiler water supply line 11 to generate saturated water vapor with the pressure of 4MPa, enters a heat exchange superheater 12 through a saturated steam line 20 to obtain superheated steam with the pressure of 4MPa and 600 ℃ through indirect heat exchange, wherein part of the superheated steam enters high-temperature steam (6 t/h) and an oxygen mixed gas line 17 after passing through a pressure reducing valve to serve as raw materials for non-catalytic reforming, and the rest of the high-pressure superheated steam is sent to a required process through an outward byproduct steam pipeline 26.
After being mixed with oxygen in a pipeline 17, the high-temperature superheated steam directly enters a non-catalytic reformer 1 to reform with raw gas to prepare synthetic gas at 1500 ℃, the oxygen content in the outlet synthetic gas is less than 0.01%, and the tar content is less than 0.01%. The residence time of the high temperature gas in the non-catalytic reformer 1 for the reforming reaction was 3.8s.
The synthetic gas cooled to 250 ℃ by the heat exchange device 2 is dedusted by the dedusting device 3, and the dedusted synthetic gas at 250 ℃ enters the cooler 8 to reduce the temperature to 50 ℃ to obtain low-temperature synthetic gas. The low-temperature synthesis gas with the temperature of 50 ℃ from the cooler 8 enters the fan 6 to introduce and convey the gas, then enters the purifying device 9 to dry-process remove and purify the sulfur-containing compounds in the gas, so that the sulfur content in the gas is less than 1mg/m 3 Obtaining ultra-clean gas. The ultra-purified gas from the purification device 9 enters a compressor 10 for secondary compression to be pressurized to 5MPa, then enters a methanol synthesis device 15 for preparing methanol, and is sent to the next process through a product pipeline 23.
Example 3
Raw gas at 700 ℃ from a coke oven, dry gas flow rate of 55000Nm 3 And/h, the flow rate of the contained water vapor is 20t/h, and the water vapor directly enters the non-catalytic reforming furnace 1. The non-catalytic reformer 1 had a height of 24m and an inner diameter of 3.5m. Oxygen line 25 delivers oxygen at a pressure of 0.8MPa and an oxygen flow of 18500Nm 3 And/h, firstly, the mixture enters a heat exchange preheater 14, is heated to 170 ℃ through indirect heat exchange, then enters a heat exchange superheater 12 through a preheated oxygen pipeline 21, is continuously heated to 500 ℃ through indirect heat exchange, and then enters a high-temperature steam and oxygen mixed gas pipeline 17 through a pressure reducing valve. The coking phenolic cyanide-containing wastewater 160t/h with the pressure of 4MPa from a boiler water supply pipeline 24 firstly enters a heat exchange preheater 14, is heated to 170 ℃ through indirect heat exchange, enters a waste heat boiler 13 through a preheating boiler water supply pipeline 11 to generate saturated water vapor with the pressure of 3.5MPa, enters a heat exchange superheater 12 through a saturated steam pipeline 20 to obtain superheated steam with the pressure of 3.5MPa and 500 ℃ through indirect heat exchange, wherein part of the superheated steam enters high-temperature steam (5 t/h) and an oxygen mixed gas pipeline 17 after passing through a pressure reducing valve to serve as raw materials for non-catalytic reforming, and the rest of the high-pressure superheated steam is sent to a required process through an outward byproduct steam pipeline 26.
After being mixed with oxygen in a pipeline 17, the high-temperature superheated steam directly enters a non-catalytic reformer 1 to reform with raw gas to prepare 1400 ℃ synthetic gas, the oxygen content in the outlet synthetic gas is less than 0.01%, and the tar content is less than 0.01%. The residence time of the high temperature gas in the non-catalytic reformer 1 for the reforming reaction was 1.3s.
The synthetic gas cooled to 220 ℃ by the heat exchange device 2 is dedusted by the dedusting device 3, and the dedusted synthetic gas at 220 ℃ enters the cooler 8 to reduce the temperature to 40 ℃ to obtain low-temperature synthetic gas. The low-temperature synthetic gas with the temperature of 40 ℃ from the cooler 8 enters the fan 6 to introduce and convey the gas, then enters the purifying device 9 to dry-process remove and purify the sulfur-containing compounds in the gas, so that the sulfur-containing compounds in the gas are purifiedThe sulfur content in the catalyst is less than 1mg/m 3 Obtaining ultra-clean gas. The ultra-purified gas from the purification device 9 enters a compressor 10 for secondary compression to be pressurized to 5MPa, then enters a methanol synthesis device 15 for preparing methanol, and is sent to the next process through a product pipeline 23.
Example 4
Raw gas at 650 ℃ from coke oven, dry gas flow rate of 52000Nm 3 And/h, the flow rate of the contained water vapor is 17t/h, and the water vapor directly enters the non-catalytic reforming furnace 1. The non-catalytic reformer 1 had a height of 24m and an inner diameter of 6.5m. Oxygen line 25 delivers oxygen at a pressure of 1MPa and an oxygen flow of 17000Nm 3 And/h, firstly, entering a heat exchange preheater 14, heating to 190 ℃ through indirect heat exchange, then entering a heat exchange superheater 12 through a preheated oxygen pipeline 21, continuously heating to 450 ℃ through indirect heat exchange, and then entering a high-temperature steam and oxygen mixed gas pipeline 17 through a pressure reducing valve. Soft water 150t/h with the pressure of 4MPa from a boiler water supply pipeline 24 firstly enters a heat exchange preheater 14, is heated to 180 ℃ through indirect heat exchange, enters a waste heat boiler 13 through a preheating boiler water supply pipeline 11 to generate saturated water vapor with the pressure of 3.4MPa, enters a heat exchange superheater 12 through a saturated steam pipeline 20 to obtain superheated steam with the pressure of 3.4MPa and 500 ℃ through indirect heat exchange, wherein part of the superheated steam enters high-temperature steam (4.5 t/h) and an oxygen mixed gas pipeline 17 after passing through a pressure reducing valve to serve as raw materials for non-catalytic reforming, and the rest of the high-pressure superheated steam is sent to a required process through an outward byproduct steam pipeline 26.
After being mixed with oxygen in a pipeline 17, the high-temperature superheated steam directly enters a non-catalytic reformer 1 to reform with raw gas to prepare 1350 ℃ synthetic gas, wherein the oxygen content in the outlet synthetic gas is less than 0.01%, and the tar content is less than 0.01%. The residence time of the high temperature gas in the non-catalytic reformer 1 for the reforming reaction was 5.0s.
The synthetic gas cooled to 210 ℃ by the heat exchange device 2 is dedusted by the dedusting device 3, and the dedusted synthetic gas at 210 ℃ enters the cooler 8 to reduce the temperature to 37 ℃ to obtain low-temperature synthetic gas. The low-temperature synthetic gas with the temperature of 37 ℃ from the cooler 8 enters the fan 6 to introduce and convey the gas, then enters the purification device 9 to remove the sulfur-containing compounds in the gas by a wet methodAnd (3) converting the mixture into a mixture with a sulfur content of less than 1mg/m 3 Obtaining ultra-clean gas. The ultra-purified gas from the purification device 9 enters a compressor 10 for secondary compression to be pressurized to 5MPa, then enters a methanol synthesis device 15 for preparing methanol, and is sent to the next process through a product pipeline 23.
Example 5
Raw gas at 780 ℃ from the coke oven, dry gas flow is 51000Nm 3 And/h, the flow rate of the contained water vapor is 15t/h, and the water vapor directly enters the non-catalytic reforming furnace 1. The non-catalytic reformer 1 had a height of 20m and an inner diameter of 5m. Oxygen line 25 delivers oxygen at a pressure of 1.2MPa and an oxygen flow of 15000Nm 3 And/h, firstly, entering a heat exchange preheater 14, heating to 180 ℃ through indirect heat exchange, then entering a heat exchange superheater 12 through a preheated oxygen pipeline 21, continuously heating to 480 ℃ through indirect heat exchange, and then entering a high-temperature steam and oxygen mixed gas pipeline 17 through a pressure reducing valve. Soft water 135t/h with the pressure of 4MPa from a boiler water supply pipeline 24 firstly enters a heat exchange preheater 14, is heated to 180 ℃ through indirect heat exchange, enters a waste heat boiler 13 through a preheating boiler water supply pipeline 11 to generate saturated water vapor with the pressure of 3.6MPa, enters a heat exchange superheater 12 through a saturated steam pipeline 20 to obtain superheated steam with the pressure of 3.6MPa and 540 ℃ through indirect heat exchange, wherein part of the superheated steam enters high-temperature steam (4.5 t/h) and an oxygen mixed gas pipeline 17 after passing through a pressure reducing valve to serve as raw materials for non-catalytic reforming, and the rest of the high-pressure superheated steam is sent to a required process through an outward byproduct steam pipeline 26.
After being mixed with oxygen in a pipeline 17, the high-temperature superheated steam directly enters a non-catalytic reformer 1 to reform with raw gas to prepare 1420 ℃ synthetic gas, the oxygen content in the outlet synthetic gas is less than 0.01%, and the tar content is less than 0.01%. The residence time of the high temperature gas in the non-catalytic reformer 1 for the reforming reaction was 2.5s.
The synthetic gas cooled to 230 ℃ by the heat exchange device 2 is dedusted by the dedusting device 3, and the dedusted synthetic gas at 230 ℃ enters the cooler 8 to reduce the temperature to 42 ℃ to obtain low-temperature synthetic gas. The 42 ℃ low-temperature synthetic gas from the cooler 8 enters the fan 6 to introduce and convey the gas, and then enters the purifying device 9 to dry the sulfur-containing compounds in the gasRemoving and purifying by a method to ensure that the sulfur content in the catalyst is less than 1mg/m 3 Obtaining ultra-clean gas. The ultra-purified gas from the purification device 9 enters a compressor 10 for secondary compression to be pressurized to 5MPa, then enters a methanol synthesis device 15 for preparing methanol, and is sent to the next process through a product pipeline 23.
Claims (7)
1. The device for producing the methanol by directly reforming the raw coke oven gas by water vapor is characterized by comprising a non-catalytic reforming furnace (1), a heat exchange device (2), a dust removal device (3) and a methanol production device (5); the side surface of the top of the non-catalytic reforming furnace (1) is connected with a raw gas collecting pipe (16), the top of the non-catalytic reforming furnace is connected with a high-temperature steam and oxygen mixed gas pipeline (17), and the side surface of the bottom of the non-catalytic reforming furnace is connected with a high-temperature gas inlet (18) of the heat exchange device (2); the low-temperature gas outlet (19) of the heat exchange device (2) is connected with a tangential gas inlet at the side surface of the top of the dust removal device (3); the top gas outlet of the dust removing device (3) is connected with an inlet pipeline (22) of the methanol production device (5); the outlet of the methanol production device (5) is connected with a methanol product pipeline (23);
the heat exchange device (2) comprises a heat exchange superheater (12) and a waste heat boiler (13) and a heat exchange preheater (14), wherein the heat exchange superheater (12) is connected with a high-temperature steam and oxygen mixed gas pipeline (17) through a superheated steam pipeline (4) and a high-temperature oxygen pipeline (7), is connected with the waste heat boiler (13) through a saturated steam pipeline (20), is connected with the heat exchange preheater (14) through a preheated oxygen pipeline (21), the waste heat boiler (13) is connected with the heat exchange preheater (14) through a preheated boiler water supply pipeline (11), the heat exchange preheater (14) is connected with a boiler water supply pipeline (24) and an oxygen pipeline (25) respectively, and the superheated steam pipeline (4) is connected with the high-temperature steam and oxygen mixed gas pipeline (17) through a pressure reducing valve and is connected with a byproduct steam pipeline (26) through an adjusting valve;
the methanol production device (5) comprises a cooler (8), a fan (6), a purification device (9), a compressor (10) and a methanol synthesis device (15), wherein a gas inlet of the cooler (8) is connected with an inlet pipeline (22), a gas outlet of the cooler (8) is connected with an inlet of the fan (6), an outlet of the fan (6) is connected with a gas inlet of the purification device (9), a gas outlet of the purification device (9) is connected with an inlet of the compressor (10), an outlet of the compressor (10) is connected with a gas inlet of the methanol synthesis device (15), and an outlet of the methanol synthesis device (15) is connected with a methanol product pipeline (23);
the non-catalytic reforming furnace (1) is internally lined with refractory bricks, the outer wall is of a water jacket structure, the height is 10-30 m, and the ratio of the height to the inner diameter is 2.0-10.0:1.0;
the fan (6) in the methanol production device (5) is a Roots blower;
the purification device (9) is a wet desulfurization device or a dry desulfurization device.
2. A method for producing methanol by direct steam reforming of coke oven raw gas according to claim 1, comprising the following steps:
a. raw coke oven gas with the temperature of 600-800 ℃ from a raw coke oven gas collecting pipe (16) enters the non-catalytic reformer (1) from the top side surface of the non-catalytic reformer (1), is quickly mixed with steam and oxygen mixed gas sprayed from the top of the non-catalytic reformer (1) and generates high-temperature combustion reaction, so that the temperature in the non-catalytic reformer (1) reaches 1300-1500 ℃ instantly, and carbon-containing organic matters in the raw coke oven gas and water steam generate reforming reaction to generate CO and H 2 A predominately syngas;
the residence time of the high-temperature gas in the non-catalytic reformer (1) for reforming reaction is 1.0-10.0 s;
b. the boiler feed water with the pressure of 4MPa from a boiler feed water pipeline (24) firstly enters a heat exchange preheater (14), is heated to 170-200 ℃ through indirect heat exchange, enters a waste heat boiler (13) through a preheating boiler feed water pipeline (11) to generate saturated water vapor with the pressure of 3-4 MPa, enters a heat exchange superheater (12) through a saturated steam pipeline (20) to obtain superheated steam with the pressure of 3-4 MPa and 400-600 ℃ through indirect heat exchange, wherein part of the superheated steam enters a high-temperature steam and oxygen mixed gas pipeline (17) through a pressure reducing valve to serve as a raw material for non-catalytic reforming, and the rest of the high-pressure superheated steam is sent to a required process through an external byproduct steam pipeline (26);
c. oxygen with the pressure of 0.5-2 MPa is conveyed by an oxygen pipeline (25), firstly enters a heat exchange preheater (14), is heated to 150-200 ℃ through indirect heat exchange, then enters a heat exchange superheater (12) through a preheated oxygen pipeline (21), is continuously heated to 400-600 ℃ through indirect heat exchange, and then enters a high-temperature steam and oxygen mixed gas pipeline (17) through a pressure reducing valve;
d. high-temperature synthesis gas coming out of the side surface of the bottom of the non-catalytic reforming furnace (1) enters a heat exchange device (2), sequentially passes through a heat exchange superheater (12), a waste heat boiler (13) and a heat exchange preheater (14), is cooled to 200-250 ℃, and then enters a dust removal device (3);
e. the synthesis gas at 200-250 ℃ from the dust removing device (3) enters a cooler (8) to reduce the temperature to 30-50 ℃ to obtain low-temperature synthesis gas;
f. the low-temperature synthetic gas from the cooler (8) enters a fan (6) to introduce and convey the gas, and then enters a purifying device (9) to remove and purify sulfur-containing compounds in the gas, so that the sulfur content in the gas is less than 1mg/m 3 Obtaining ultra-clean gas;
g. the ultra-purified gas from the purification device (9) enters a compressor (10) to be pressurized to 5MPa, then enters a methanol synthesis device (15) to obtain a methanol product, and is sent to the next working procedure through a product pipeline (23).
3. The method for producing methanol by direct steam reforming of raw coke oven gas according to claim 2, wherein the residence time of the high temperature gas in the step (a) in the non-catalytic reformer (1) is 1.0 to 10.0s.
4. The method for producing methanol by direct steam reforming of coke oven raw gas according to claim 2, wherein the purity of oxygen in the step (a) is 99-99.9%, and the molar ratio of steam injected from the top of the non-catalytic reformer (1) to oxygen is 0.3-5.0:1.
5. The method for producing methanol by direct steam reforming of coke oven raw gas according to claim 2, wherein the oxygen content in the outlet gas of the non-catalytic reformer 1 is less than 0.01%.
6. The method for producing methanol by directly reforming raw coke oven gas with steam according to claim 2, wherein the organic matter content in the outlet gas of the non-catalytic reformer (1) is less than 0.01%.
7. The method for producing methanol by direct steam reforming of coke oven raw gas according to claim 2, wherein the boiler feed water in the step (b) is soft water or coked phenolic cyanide-containing wastewater.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910045582.8A CN109553508B (en) | 2019-01-17 | 2019-01-17 | Device and method for producing methanol by directly reforming raw coke oven gas with water vapor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910045582.8A CN109553508B (en) | 2019-01-17 | 2019-01-17 | Device and method for producing methanol by directly reforming raw coke oven gas with water vapor |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN109553508A CN109553508A (en) | 2019-04-02 |
| CN109553508B true CN109553508B (en) | 2024-03-29 |
Family
ID=65873241
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201910045582.8A Active CN109553508B (en) | 2019-01-17 | 2019-01-17 | Device and method for producing methanol by directly reforming raw coke oven gas with water vapor |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN109553508B (en) |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1644661A (en) * | 2004-12-16 | 2005-07-27 | 太原理工大学 | Oven gas generation of plasma gasified coke oven |
| CN101112970A (en) * | 2007-07-04 | 2008-01-30 | 山西科灵催化净化技术发展公司 | Technical method for preparing menthol synthetic gas by coke oven gas conversion without catalytic oxidation |
| CN103804138A (en) * | 2014-03-11 | 2014-05-21 | 太原理工大学 | Technology for producing methanol through coke oven gas |
| CN104593079A (en) * | 2015-01-15 | 2015-05-06 | 太原理工大学 | Process for producing clean synthesis gas from crushed coal |
| CN105062591A (en) * | 2015-07-31 | 2015-11-18 | 赛鼎工程有限公司 | Technology for production of gasoline and combined production of natural gas and hydrogen through methanol synthesis of coke oven gas |
| CN106699508A (en) * | 2016-12-22 | 2017-05-24 | 赛鼎工程有限公司 | Process for high-efficiency and environment-friendly synthesis of methanol by coke oven gas |
-
2019
- 2019-01-17 CN CN201910045582.8A patent/CN109553508B/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1644661A (en) * | 2004-12-16 | 2005-07-27 | 太原理工大学 | Oven gas generation of plasma gasified coke oven |
| CN101112970A (en) * | 2007-07-04 | 2008-01-30 | 山西科灵催化净化技术发展公司 | Technical method for preparing menthol synthetic gas by coke oven gas conversion without catalytic oxidation |
| CN103804138A (en) * | 2014-03-11 | 2014-05-21 | 太原理工大学 | Technology for producing methanol through coke oven gas |
| CN104593079A (en) * | 2015-01-15 | 2015-05-06 | 太原理工大学 | Process for producing clean synthesis gas from crushed coal |
| CN105062591A (en) * | 2015-07-31 | 2015-11-18 | 赛鼎工程有限公司 | Technology for production of gasoline and combined production of natural gas and hydrogen through methanol synthesis of coke oven gas |
| CN106699508A (en) * | 2016-12-22 | 2017-05-24 | 赛鼎工程有限公司 | Process for high-efficiency and environment-friendly synthesis of methanol by coke oven gas |
Also Published As
| Publication number | Publication date |
|---|---|
| CN109553508A (en) | 2019-04-02 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN106536681B (en) | Gasification-based energy efficient poly-generation apparatus employing advanced process schemes and related methods | |
| CN102181315B (en) | Process for producing natural gas by coal coking and pyrolysis coal gas thereof | |
| CN108946661B (en) | Method and system for preparing hydrogen through biomass gasification | |
| CN101041120A (en) | Device for the recovery and diffluence of sulfur dioxide and the system and method thereof | |
| CN107777663B (en) | A kind of coupling process of lighter hydrocarbons hydrogen manufacturing and hydrogen from methyl alcohol | |
| CN1974732A (en) | Process of preparing synthesized gas with gasified gas and pyrolyzed gas | |
| CN204211707U (en) | Utilize the device of coke-oven gas and blast furnace gas combination producing Sweet natural gas and liquefied ammonia | |
| CN110951508A (en) | Device and process for preparing methane by coal chemical-looping catalytic gasification based on calcium oxide | |
| CN100579896C (en) | Method and system for preparing synthetic gas with appropriate hydrogen-carbon ratio from lurgi furnace outlet coal gas through non-catalytic partial oxidation by pure oxygen | |
| CN104495749A (en) | Device and method for producing hydrogen by utilizing coke oven crude gas | |
| CN106800955B (en) | Method for producing tar and co-producing LNG (liquefied natural gas) by coupling pulverized coal pyrolysis and coke breeze gasification | |
| CN109485016A (en) | A kind of system and method for the direct steam reformation hydrogen making of coal oven dithio-gas or ammonia | |
| CN106947541B (en) | Combined method and system for hydrogen production based on low-rank coal pyrolysis water vapor coke quenching water gas | |
| CN106241735B (en) | A kind of carbide slag prepares the system and method for hydrogen-rich gas and calcium carbide | |
| CN209854029U (en) | Device for preparing methanol from synthesis gas without conversion system | |
| CN109553508B (en) | Device and method for producing methanol by directly reforming raw coke oven gas with water vapor | |
| CN217459483U (en) | Energy gradient utilization system for coupling production of gas-based shaft furnace and coke oven | |
| US9631553B2 (en) | Process and equipment for coal gasification, and power generation system and power generation process thereof | |
| CN113060704B (en) | Organic solid clean high-efficiency hydrogen production device and method | |
| CN216445007U (en) | High-temperature raw gas non-catalytic partial oxidation direct reforming system | |
| CN104164257A (en) | Fischer-Tropsch reactor pure-oxygen continuous gasification apparatus and gasification technology | |
| CN210261658U (en) | System for preparing coal gas by pyrolyzing crude coke water vapor in thermal power plant | |
| CN114657305A (en) | Energy gradient utilization system and method for coupling production of gas-based shaft furnace and coke oven | |
| CN102585905A (en) | Bituminous coal fixed bed continuous gasification method | |
| CN203096005U (en) | Carbon-hydrogen-component-staged-conversion gasification system for coal |
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 |