CN104987279A - Methanol-making system and method through coal gasification integrating waste heat cooling and carbon trapping - Google Patents
Methanol-making system and method through coal gasification integrating waste heat cooling and carbon trapping Download PDFInfo
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- CN104987279A CN104987279A CN201510400928.3A CN201510400928A CN104987279A CN 104987279 A CN104987279 A CN 104987279A CN 201510400928 A CN201510400928 A CN 201510400928A CN 104987279 A CN104987279 A CN 104987279A
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- 239000002918 waste heat Substances 0.000 title claims abstract description 121
- 238000002309 gasification Methods 0.000 title claims abstract description 48
- 238000000034 method Methods 0.000 title claims abstract description 36
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 title claims abstract description 33
- 229910052799 carbon Inorganic materials 0.000 title claims abstract description 33
- 239000003245 coal Substances 0.000 title claims abstract description 20
- 238000001816 cooling Methods 0.000 title abstract description 14
- 239000007789 gas Substances 0.000 claims abstract description 176
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims abstract description 152
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 101
- 230000006835 compression Effects 0.000 claims abstract description 70
- 238000007906 compression Methods 0.000 claims abstract description 70
- 239000000498 cooling water Substances 0.000 claims abstract description 46
- 230000015572 biosynthetic process Effects 0.000 claims abstract description 36
- 238000003786 synthesis reaction Methods 0.000 claims abstract description 35
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 104
- 238000005057 refrigeration Methods 0.000 claims description 62
- 239000002253 acid Substances 0.000 claims description 58
- 229910021529 ammonia Inorganic materials 0.000 claims description 52
- 238000011084 recovery Methods 0.000 claims description 32
- 239000006200 vaporizer Substances 0.000 claims description 32
- 230000008569 process Effects 0.000 claims description 26
- 230000008676 import Effects 0.000 claims description 23
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims description 20
- 238000000926 separation method Methods 0.000 claims description 14
- 239000005864 Sulphur Substances 0.000 claims description 12
- 235000011114 ammonium hydroxide Nutrition 0.000 claims description 12
- 239000007788 liquid Substances 0.000 claims description 10
- 229910052717 sulfur Inorganic materials 0.000 claims description 8
- 239000011593 sulfur Substances 0.000 claims description 8
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical group [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 7
- 239000002826 coolant Substances 0.000 claims description 7
- 230000000694 effects Effects 0.000 claims description 7
- 238000005507 spraying Methods 0.000 claims description 5
- 230000006837 decompression Effects 0.000 claims description 4
- 239000002002 slurry Substances 0.000 claims description 4
- 239000006096 absorbing agent Substances 0.000 claims description 3
- -1 resorber Substances 0.000 claims description 2
- 230000008901 benefit Effects 0.000 abstract description 2
- 230000003247 decreasing effect Effects 0.000 abstract 3
- 238000005516 engineering process Methods 0.000 description 5
- 229910052760 oxygen Inorganic materials 0.000 description 5
- 239000001301 oxygen Substances 0.000 description 5
- 238000006243 chemical reaction Methods 0.000 description 4
- 238000005265 energy consumption Methods 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- 239000000047 product Substances 0.000 description 4
- 239000006227 byproduct Substances 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 238000010521 absorption reaction Methods 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 239000003250 coal slurry Substances 0.000 description 1
- 235000009508 confectionery Nutrition 0.000 description 1
- 238000005262 decarbonization Methods 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 210000004243 sweat Anatomy 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- 238000005406 washing Methods 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
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/46—Gasification of granular or pulverulent flues in suspension
- C10J3/48—Apparatus; Plants
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
- F25B15/00—Sorption machines, plants or systems, operating continuously, e.g. absorption type
- F25B15/02—Sorption machines, plants or systems, operating continuously, e.g. absorption type without inert gas
- F25B15/04—Sorption machines, plants or systems, operating continuously, e.g. absorption type without inert gas the refrigerant being ammonia evaporated from aqueous solution
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
- F25B27/00—Machines, plants or systems, using particular sources of energy
- F25B27/02—Machines, plants or systems, using particular sources of energy using waste heat, e.g. from internal-combustion engines
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0913—Carbonaceous raw material
- C10J2300/093—Coal
-
- 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
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A30/00—Adapting or protecting infrastructure or their operation
- Y02A30/27—Relating to heating, ventilation or air conditioning [HVAC] technologies
- Y02A30/274—Relating to heating, ventilation or air conditioning [HVAC] technologies using waste energy, e.g. from internal combustion engine
-
- 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
- Y02B—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO BUILDINGS, e.g. HOUSING, HOUSE APPLIANCES OR RELATED END-USER APPLICATIONS
- Y02B30/00—Energy efficient heating, ventilation or air conditioning [HVAC]
- Y02B30/62—Absorption based systems
- Y02B30/625—Absorption based systems combined with heat or power generation [CHP], e.g. trigeneration
-
- 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
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Organic Chemistry (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Industrial Gases (AREA)
- Oil, Petroleum & Natural Gas (AREA)
Abstract
The invention discloses a methanol-making system through coal gasification integrating waste heat cooling and carbon trapping. The methanol-making system is mainly composed of a Texaco gasfication unit, a dedusting and purifying unit, a water gas shifting unit, an acid-gas removing unit, a synthesis and rectification unit for methanol and a waste heat cooling unit, wherein the steam outlet of the water-gas shifting unit is connected with the steam-inlet of the waste heat cooling unit. The cold water outlet of the waste heat cooling system is connected with the cooling water inlet of the acid-gas removing unit, or the cold water outlet of the waste heat cooling system is connected with the cooling water inlet of a CO2 multistage compression unit and the cooling water inlet of the acid-gas removing unit at the same time. The superheated water outlet of the CO2 multistage compression unit is connected with the waste heat boiler water inlet of the water-gas shifting unit. The invention further provides a methanol-making method through coal gasification integrating the waste heat cooling and the carbon trapping. The methanol-making system and method through coal gasification integrating the waste heat cooling and the carbon trapping have the advantages that the emission of waste heat is decreased, the power consumption needed by additional cooling is decreased, and the emission of CO2 is decreased.
Description
Technical field
The present invention relates to gasification methyl alcohol technology, the gasification methyl alcohol system and method for a kind of integrated utilizing waste heat for refrigeration and carbon trapping specifically.
Background technology
Methyl alcohol is a kind of fuel of cleaning and the staple product of C1 chemical industry.The chemical industry wide by methyl alcohol and energy source use prospect attract, countries in the world all start to pay attention to the large-scale methyl alcohol technology processed of development.At present, generally adopt Sweet natural gas as the raw material of methanol in the world.China is subject to rich coal, resource structures that is oil-poor, weak breath limited, and therefore ammonia from coal technique (CTM) becomes the major way of China's methanol.
Ammonia from coal core is gasification, and this process produces synthetic gas by gasification, and synthetic gas is after treatment as the raw material of methanol-fueled CLC reaction; Specifically comprise with lower unit: gasification, synthesis gas washing, water-gas shift, desulfurization decarbonization purification (containing sulfur recovery), methanol-fueled CLC and rectifying etc.
The development of large-scale ammonia from coal technology is subject to that energy consumption is high, carbon emission amount these two factors large limited always.Generally believe, carbon trapping (CC) technology significantly can reduce the carbon emission of ammonia from coal process., the trapping energy consumption that the consumption of carbon trapping process need is extra, this makes the ammonia from coal process of high energy consumption make the matter worse.The ammonia from coal general flow chart of process is trapped as Fig. 1: coal water slurry produces crude synthesis gas through texaco gasification unit 1, and crude synthesis gas adjusts ratio of carbon-hydrogen through converter unit 3, the CO in synthetic gas with carbon
2and H
2s is removed by acid gas purifying unit 4, and multi-stage compression unit 6 is CO
2be compressed into liquid state be transported to other techniques or store, H
2s is recycled into sulphur byproduct by Claus unit 7, and clean synthetic gas produces methanol product through methanol-fueled CLC and rectification cell 5.
One of major reason that gasification methanol process energy consumption is large is, acid gas removal unit 4 and CO
2multi-stage compression unit 7 all needs cold energy extra in a large number to complete its technological process, and the former more needs the low temperature cold of-40 ~-50 DEG C.And general ammonia from coal flow process is as Fig. 1, compression refrigeration station 8 consumes a large amount of electric energy and produces cold to meet acid gas removal unit 4 and CO
2the cold consumption of multi-stage compression unit 6, therefore causes power consumption excessive.
Summary of the invention
The object of the invention is to the deficiency overcoming the existence of above prior art, provide a kind of load reducing cooling system, the gasification methyl alcohol system of the integrated utilizing waste heat for refrigeration of save energy and carbon trapping.Present invention also offers the method for the gasification alkaline methanol controlling methyl alcohol of a kind of integrated utilizing waste heat for refrigeration and carbon trapping simultaneously.
In order to achieve the above object, the present invention is by the following technical solutions: the gasification methyl alcohol system of a kind of integrated utilizing waste heat for refrigeration and carbon trapping, comprise texaco gasification unit, udst separation unit, water-gas shift unit, acid gas removal unit and the methanol-fueled CLC and rectification cell that connect successively, simultaneously the sulphur emissions mouth of described acid gas removal unit and CO
2discharge outlet is connected to sulfur recovery unit and CO
2multi-stage compression unit; Also comprise utilizing waste heat for refrigeration unit, the vapour outlet of described water-gas shift unit is connected with the steam-in of utilizing waste heat for refrigeration unit, the cooling water outlet of described utilizing waste heat for refrigeration unit be connected with the entrance of cooling water of acid gas removal unit or described utilizing waste heat for refrigeration unit cooling water outlet simultaneously and CO
2the entrance of cooling water of multi-stage compression unit, the entrance of cooling water of acid gas removal unit connect; Described CO
2the superheated water outlet of multi-stage compression unit is connected with the waste heat boiler water-in of water-gas shift unit.
Preferably, described utilizing waste heat for refrigeration unit comprises producer, condenser, cold recovery device, vaporizer, resorber, solution heat exchanger and pump; The steam-in of described producer is connected with the vapour outlet of water-gas shift unit, the cooling water outlet of described vaporizer be connected with the entrance of cooling water of acid gas removal unit or described vaporizer cooling water outlet simultaneously and CO
2the entrance of cooling water of multi-stage compression unit, the entrance of cooling water of acid gas removal unit connect;
The ammonia outlet of described producer is connected with the hot side inlet of condenser, the hot junction outlet of described condenser is connected with the hot-side inlet of cold recovery device, described cold recovery device is connected with the ammonia import of vaporizer by expansion valve, the ammonia outlet of described vaporizer is connected with the cold-side inlet of cold recovery device, the cold side outlet of described cold recovery device is connected with the ammonia import of resorber, the ammoniacal liquor outlet of described resorber is connected with the ammoniacal liquor import of solution heat exchanger by pump, and the ammoniacal liquor import of described solution heat exchanger is connected with the strong aqua import of producer; The weak ammonia outlet of described producer is connected with the hot-side inlet of solution heat exchanger, and the hot junction outlet of described solution heat exchanger is connected with the spraying head of resorber by solution decompression valve.
Preferably, absorber cooler is provided with in the device shell of described resorber or outside device shell.
Preferably, described water-gas shift unit comprises the first shift-converter, second shift-converter, primary waste heat boiler, secondary waste heat boiler, first drum and the second drum, the inlet mouth of described first shift-converter is connected with udst separation unit, the described air outlet of the first shift-converter is connected with the hot side inlet of primary waste heat boiler, the hot junction outlet of described primary waste heat boiler is connected with the inlet mouth of the second shift-converter, the described air outlet of the second shift-converter is connected with the hot side inlet of secondary waste heat boiler, the hot junction outlet of described secondary waste heat boiler is connected with the synthesis gas import of acid gas removal unit,
Described CO
2the superheated water outlet of multi-stage compression unit is connected with the water-in of secondary waste heat boiler, and the superheated water outlet of described secondary waste heat boiler is connected with the superheated water entrance of the first drum, and the described vapour outlet of the first drum is connected with the steam-in of producer; The described hot water outlet of the first drum is connected with the water-in of primary waste heat boiler, and the superheated water outlet of described primary waste heat boiler is connected with the superheated water entrance of the second drum, and the described vapour outlet of the second drum is connected with the steam-in of producer.
Preferably, described CO
2multi-stage compression unit comprises multiple CO
2compressor and and CO
2the compression cooler that number of compressors is equal, multiple described CO
2compressor and compression cooler are alternately connected successively, wherein, are positioned at the first CO
2the CO of compressor
2the CO of entrance and acid gas removal unit
2discharge outlet connects, and multiple cooling water inlet of described compression cooler is connected with the cooling water outlet of vaporizer.
Based on a methanol process processed for the gasification methyl alcohol system that above-mentioned integrated utilizing waste heat for refrigeration and carbon trap, comprise the following steps:
(1) coal water slurry and oxygen form synthetic gas after entering texaco gasification unit, and described synthetic gas is successively by entering acid gas purifying unit after purifying and dedusting unit and water-gas shift unit, and acid gas purifying unit is by the CO in synthetic gas
2gas delivery out, then the CO separated
2gas enters CO
2multi-stage compression unit; The Clean synthesis gas that acid gas purifying unit produces enters methanol-fueled CLC and rectification cell from the syngas outlet of acid gas purifying unit, thus obtained refined methanol;
(2) in step (1), CO is entered
2the CO of multi-stage compression unit
2gas is compressed into liquid CO
2, CO
2multi-stage compression unit compression CO
2a large amount of superheated water is produced during gas, this superheated water is by the effect of primary waste heat boiler, secondary waste heat boiler, the first drum and the second drum in water-gas shift unit, superheated water is transformed into low pressure water vapor, low pressure water vapor heats obtained ammonia to the strong aqua in producer, this ammonia is successively by being transformed into cold liquefied ammonia after condenser and cold recovery device, this cold liquefied ammonia freezes to the water in vaporizer, thus obtained water coolant, this water coolant is by entering CO after vaporizer cooling water outlet
2multi-stage compression unit and acid gas removal unit, thus the cold that water coolers contains can be supplied in CO
2multi-stage compression unit and acid gas removal unit.
Preferably, in step (2), before the strong aqua in producer and low pressure water vapor carry out heat exchange, before the strong aqua namely in producer is heated by low-pressure steam, the concentration of strong aqua is 25% ~ 45%.
Preferably, in step (2), after the effect of superheated water by primary waste heat boiler, secondary waste heat boiler, the first drum and the second drum in water-gas shift unit, the low pressure water vapor of generation is the low-pressure steam for 0.7-1.5MPa.
The present invention, relative to prior art, has following advantage and effect:
1, efficient recovery CO of the present invention
2multi-stage compression unit produces the low-grade exhaust heat that superheated water contains, and optimizes the Steam Utilization Way of water-gas shift unit simultaneously, decreases discharge and the required power consumption of extra cooling of used heat, arrives energy-saving and cost-reducing object.
2, the present invention adopts utilizing waste heat for refrigeration unit to replace traditional compression refrigeration station, avoids the power consumption reducing electric refrigeration plant, then reduces the CO of generating discharge
2.
3, the present invention adopts utilizing waste heat for refrigeration unit to replace traditional compression refrigeration station, and this regulates steam in production process and electric load effectively.
Accompanying drawing explanation
Process flow sheet when Fig. 1 is the methyl alcohol processed of the gasification methyl alcohol system of traditional a kind of integrated utilizing waste heat for refrigeration and carbon trapping; Wherein: 1 is texaco gasification unit, 2 is udst separation unit, and 3 is water-gas shift unit, and 4 is acid gas removal unit, and 5 is methanol-fueled CLC and rectification cell, and 6 is CO
2multi-stage compression unit, 7 is Claus unit, and 8 is conventional electric refrigeration unit, and 9 is water coal oar; 10 is oxygen, and 11,12 and 13 are crude synthesis gas, and 14 is H
2s gas, 15 is CO
2gas, 16 is superheated water, and 17 is the logistics of cold energy carrier, and 18 is high-pressure liquid CO
2, 19 is sulphur, and 20 is Clean synthesis gas, and 21 is refined methanol, and 22 is refrigeration electric energy used.
Process flow sheet when Fig. 2 is the methyl alcohol processed of a kind of integrated utilizing waste heat for refrigeration of the embodiment of the present invention 1 and the gasification methyl alcohol system of carbon trapping; Wherein: 1 is texaco gasification unit; 2 is udst separation unit; 3 is water-gas shift unit; 4 is acid gas removal unit; 5 is methanol-fueled CLC and rectification cell; 6 is CO
2multi-stage compression unit; 7 is Claus unit; 8 ' is utilizing waste heat for refrigeration unit; 9 is water coal oar; 10 is oxygen, and 11,12 and 13 are crude synthesis gas, and 14 is H
2s gas, 15 is CO
2gas, 16 is superheated water, and 17 is the logistics of cold energy carrier, and 18 is high-pressure liquid CO
2, 19 is sulphur, and 20 is Clean synthesis gas, and 21 is refined methanol; 61 is low pressure water vapor.
Fig. 3 is water-gas shift unit of the present invention and CO
2the structural representation of multi-stage compression unit; Wherein: 4 is acid gas removal unit; 8 ' is utilizing waste heat for refrigeration unit; 12,13,38,39 and 40 be crude synthesis gas, 14 is H
2s gas, 15 is CO
2gas, 16,41,42 and 43 are superheated water, and 17 is the logistics of cold energy carrier, and 18 is high-pressure liquid CO
2, 19 is sulphur, and 20 is Clean synthesis gas, and 23 is the first shift-converter, and 24 is primary waste heat boiler, and 25 is the second drum, and 26 is the second shift-converter, and 27 is the first drum, and 28 is secondary waste heat boiler, and 29 ~ 32 is CO
2compressor, 33 ~ 36 is compression cooler, and 37 is process steam.
Fig. 4 is the structural representation of utilizing waste heat for refrigeration unit of the present invention; Wherein, 17 is the logistics of cold energy carrier, and 44 is producer, 45 is condenser, and 46 is cold recovery device, and 47 is throttling valve, 48 is vaporizer, and 49 is resorber, and 50 is water cooler, 51 is reducing valve, and 52 is pump, and 53 is solution heat exchanger, 54,58 and 59 is ammonia, and 55 is weak ammonia, and 56 is liquefied ammonia, 57 is cold liquefied ammonia, and 60 is strong aqua.
Process flow sheet when Fig. 5 is the methyl alcohol processed of a kind of integrated utilizing waste heat for refrigeration of the present embodiment 2 and the gasification methyl alcohol system of carbon trapping; Wherein: 1 is texaco gasification unit; 2 is udst separation unit; 3 is water-gas shift unit; 4 is acid gas removal unit; 5 is methanol-fueled CLC and rectification cell; 6 is CO
2multi-stage compression unit; 7 is Claus unit; 8 ' is utilizing waste heat for refrigeration unit; 9 is water coal oar; 10 is oxygen, and 11,12 and 13 are crude synthesis gas, and 14 is H
2s gas, 15 is CO
2gas, 16 is superheated water, and 17 is the logistics of cold energy carrier, and 18 is high-pressure liquid CO
2, 19 is sulphur, and 20 is Clean synthesis gas, and 21 is refined methanol; 61 is low pressure water vapor.
Fig. 6 is water-gas shift unit of the present invention and CO
2the connection diagram of multi-stage compression unit; Wherein: 4 is acid gas removal unit; 8 ' is utilizing waste heat for refrigeration unit; 12,13,38,39 and 40 be crude synthesis gas, 14 is H
2s gas, 15 is CO
2gas, 16,41,42 and 43 are superheated water, and 17 is the logistics of cold energy carrier, and 18 is high-pressure liquid CO
2, 19 is sulphur, and 20 is Clean synthesis gas, and 23 is the first shift-converter, and 24 is primary waste heat boiler, and 25 is the second drum, and 26 is the second shift-converter, and 27 is the first drum, and 28 is secondary waste heat boiler, and 29 ~ 32 is CO
2compressor, 33 ~ 36 is compression cooler, and 37 is process steam.
Embodiment
For ease of it will be appreciated by those skilled in the art that the present invention is described in further detail below in conjunction with drawings and Examples.
Embodiment 1:
The standard energy carrier logistics of the cold energy carrier logistics 17 in the present embodiment is water coolant.
As shown in Figures 2 to 4, the gasification methyl alcohol system of a kind of integrated utilizing waste heat for refrigeration and carbon trapping, comprise texaco gasification unit 1, udst separation unit 2, water-gas shift unit 3, acid gas removal unit 4 and the methanol-fueled CLC and rectification cell 5 that connect successively, simultaneously the sulphur emissions mouth of described acid gas removal unit 4 and CO
2discharge outlet is connected to sulfur recovery unit 7 and CO
2multi-stage compression unit 6; Also comprise utilizing waste heat for refrigeration unit 8 ', the vapour outlet of described water-gas shift unit 3 is connected with the steam-in of utilizing waste heat for refrigeration unit 8 ', and the cooling water outlet of described utilizing waste heat for refrigeration unit 8 ' simultaneously and CO
2the entrance of cooling water of multi-stage compression unit 6, the entrance of cooling water of acid gas removal unit 4 connect; Described CO
2the superheated water outlet of multi-stage compression unit 6 is connected with the waste heat boiler water-in of water-gas shift unit 3.Texaco gasification unit 1, udst separation unit 2, water-gas shift unit 3, acid gas removal unit 4 and methanol-fueled CLC and rectification cell 5 all can be bought from market.
Described utilizing waste heat for refrigeration unit comprises producer 44, condenser 45, cold recovery device 46, vaporizer 48, resorber 49, solution heat exchanger 53 and pump 52; Be provided with absorber cooler 50 outside the device shell of described resorber 49, the steam-in of described producer 44 is connected with the vapour outlet of water-gas shift unit 3, and the cooling water outlet of described vaporizer 48 simultaneously and CO
2the entrance of cooling water of multi-stage compression unit, the entrance of cooling water of acid gas removal unit connect; The cooling water outlet of described utilizing waste heat for refrigeration unit 8 ' simultaneously and CO
2the entrance of cooling water of multi-stage compression unit 6, the entrance of cooling water of acid gas removal unit 4 connect;
The ammonia outlet of described producer 44 is connected with the hot side inlet of condenser 45, the hot junction outlet of described condenser 45 is connected with the hot-side inlet of cold recovery device 46, described cold recovery device 46 is connected with the ammonia import of vaporizer 48 by expansion valve 47, the ammonia outlet of described vaporizer 48 is connected with the cold-side inlet of cold recovery device 46, the cold side outlet of described cold recovery device 46 is connected with the ammonia import of resorber 49, the ammoniacal liquor outlet of described resorber 49 is connected with the ammoniacal liquor import of solution heat exchanger 53 by pump, the ammoniacal liquor import of described solution heat exchanger 53 is connected with the strong aqua import of producer 44, the weak ammonia outlet of described producer 44 is connected with the hot-side inlet of solution heat exchanger 53, and the hot junction outlet of described solution heat exchanger 53 is connected with the spraying head of resorber 49 by solution decompression valve 51.
Concrete, 1.2MPa low-pressure steam enters the producer 44 in utilizing waste heat for refrigeration unit 8 ', then low-pressure steam and 30% strong aqua generation heat exchange, then the ammonia of generation 50 to 55 DEG C, concentration more than 95% enters condenser 45 from the ammonia outlet on producer 44 top, is condensed into the liquefied ammonia of 35-40 DEG C subsequently; And the weak ammonia that concentration is 15%-30% flows out to solution heat exchanger 53 from the bottom of producer 44, then arrived the spraying head of resorber 49 by reducing valve 51.Liquefied ammonia enter cold recovery device enter 46 further cooling obtain cold liquefied ammonia, this cold liquefied ammonia then enters vaporizer 48 through throttling valve 47, under the condition of 0.03-0.3MPa, sweat cooling is carried out to the water in vaporizer, thus obtained cold water, this cold water flow to CO from the cooling water outlet of vaporizer again
2multi-stage compression unit and acid gas removal unit carry out cooling.The ammonia formed at vaporizer 48 enters in absorption tower 49, and the weak ammonia being 15%-30% by concentration absorbs formation strong aqua, and strong aqua enters producer 44 by pump 52 pressurization to be continued to participate in refrigeration cycle.Therefore utilizing waste heat for refrigeration unit 8 ' can continue to freeze to low-pressure steam, can be CO
2multi-stage compression unit 6 and acid gas removal unit answer cold for 4.
Described water-gas shift unit 3 comprises the first shift-converter 23, second shift-converter 26, primary waste heat boiler 24, secondary waste heat boiler 28, first drum 27 and the second drum 25, the inlet mouth of described first shift-converter 23 is connected with udst separation unit 2, the air outlet of described first shift-converter 23 is connected with the hot side inlet of primary waste heat boiler 24, the hot junction outlet of described primary waste heat boiler 24 is connected with the inlet mouth of the second shift-converter 26, the air outlet of described second shift-converter 26 is connected with the hot side inlet of secondary waste heat boiler 28, the hot junction outlet of described secondary waste heat boiler 28 is connected with the synthesis gas import of acid gas removal unit 4,
Described CO
2the superheated water outlet of multi-stage compression unit 6 is connected with the water-in of secondary waste heat boiler 28, the superheated water outlet of described secondary waste heat boiler 28 is connected with the superheated water entrance of the first drum 27, and the vapour outlet of described first drum 27 is connected with the steam-in of producer 44; The hot water outlet of described first drum 27 is connected with the water-in of primary waste heat boiler 24, the superheated water outlet of described primary waste heat boiler 24 is connected with the superheated water entrance of the second drum 25, and the vapour outlet of described second drum 25 is connected with the steam-in of producer 44.
From dust removing purifier crude synthesis gas out, successively by after the first shift-converter 23, primary waste heat boiler 24, second shift-converter 26 and secondary waste heat boiler 28, again by entering acid gas removal unit after a water cooler, then water-gas shift unit 3 can carry out two sections of high temperature sulfur resistant conversion process to crude synthesis gas; And CO
2the superheated water that multi-stage compression unit 6 produces is introduced into the secondary waste heat boiler 28 in water-gas shift unit 3, superheated water enters the first drum 27 from secondary waste heat boiler 28, superheated water is transformed into low pressure water vapor by the first drum 27, and the superheated water not completing transformation enters the second drum 25 from primary waste heat boiler 24, this superheated water is transformed into low pressure water vapor by the second drum 25, and the low pressure water vapor that the first drum 27 and the second drum 25 produce is transported in the producer 44 of utilizing waste heat for refrigeration unit 8 '.In order to ensure to make full use of superheated water, superheated water pipeline is provided with between second drum 27 and the first drum 25, namely the second drum is directly connected by superheated water pipeline with the first drum, this makes also can not sent back in the first drum by the superheated water changed in the second drum, thus ensures that superheated water completes and be transformed into low-pressure steam.
Described CO
2multi-stage compression unit 6 comprises multiple CO
2compressor and and CO
2the compression cooler that number of compressors is equal, multiple described CO
2compressor and compression cooler are alternately connected successively, wherein, are positioned at the first CO
2the CO of compressor 29
2the CO of entrance and acid gas removal unit 4
2discharge outlet connects, and multiple cooling water inlet of described compression cooler is connected with the cooling water outlet of vaporizer.
Concrete, adopt the gasification methyl alcohol system of this integrated utilizing waste heat for refrigeration and carbon trapping to utilize the process of synthesising gas systeming carbinol to be:
After water coal oar and oxygen enter texaco gasification unit 1, coal water slurry 9 and oxygen 10 in texaco gasification unit 1 Texaco gasifier in become after carrying out at the temperature of 1200-1400 DEG C, produce crude synthesis gas, after the temperature of this crude synthesis gas is reduced to about 300-400 DEG C, discharge from texaco gasification unit 1 and enter udst separation unit 2, udst separation unit 2 removes the impurity in crude synthesis gas;
By being gone deimpurity crude synthesis gas to enter water-gas shift unit 3 by udst separation unit 2; Water-gas shift unit 3 to this crude synthesis gas carry out two sections of high temperature and sulphur is exchanged work skill, namely carry out high temperature sulfur resistant conversion process with the temperature of 350-450 DEG C when crude synthesis gas enters the first shift-converter 23, when entering the second shift-converter 26, carry out high temperature sulfur resistant conversion process with the temperature of 300-400 DEG C; Acid gas removal unit 4 is entered successively by the crude synthesis gas of the first shift-converter 23 in water-gas shift unit 3, primary waste heat boiler 24, second shift-converter 26 and secondary waste heat boiler 28;
Crude synthesis gas is separated into three parts by acid gas removal unit, i.e. gas H
2s gas 14, CO
2gas 15 and Clean synthesis gas 20, wherein H
2s gas 14 enters Claus unit 7, H by outlet
2s gas 14 is reclaimed by Claus unit 7 and makes sulphur byproduct 19; And CO
2gas 15 enters CO
2multi-stage compression unit 6, CO
2multi-stage compression unit 6 is by CO
2the liquid CO of gas compression
2be delivered to other techniques after 8 or store, thus completing carbon trapping;
And Clean synthesis gas 20 enters methanol-fueled CLC and rectification cell 5 by the syngas outlet of acid gas removal unit 4, Clean synthesis gas is made refined methanol 21 by methanol-fueled CLC and rectification cell 5.
The gasification methyl alcohol system of this integrated utilizing waste heat for refrigeration and carbon trapping has also carried out heat recovery technique in the process manufacturing methyl alcohol, and its process is as described below:
Enter CO
2the CO of multi-stage compression unit 6
2gas 15 is compressed into liquid CO
218, CO
2multi-stage compression unit compression CO
2a large amount of superheated water is produced during gas, this superheated water is by the primary waste heat boiler 24 in water-gas shift unit, secondary waste heat boiler 28, the effect of the first drum 27 and the second drum 25, superheated water is transformed into low pressure water vapor 61, then low pressure water vapor 61 enters the producer 44 in utilizing waste heat for refrigeration unit 8 ', strong aqua in low pressure water vapor 61 pairs of producers 44 heats obtained ammonia, this ammonia is successively by being transformed into cold liquefied ammonia after condenser 45 and cold recovery device 46, this cold liquefied ammonia freezes to the water in vaporizer 48, thus obtained water coolant, this water coolant is by entering CO after vaporizer 48 cooling water outlet
2multi-stage compression unit 6 and acid gas removal unit 4, thus the cold that water coolers contains can be supplied in CO
2multi-stage compression unit 6 and acid gas removal unit 4.
In above process, after the effect of superheated water by primary waste heat boiler 24, secondary waste heat boiler 28, first drum 27 and the second drum 25 in water-gas shift unit, the low pressure water vapor 61 of generation is the low-pressure steam of 1.2MPa.Before strong aqua in producer 44 and low pressure water vapor carry out heat exchange, the concentration of strong aqua is 30%.
When the gasification methyl alcohol system that this integrated utilizing waste heat for refrigeration and carbon trap adopts raw water coal slurry flow to be 107.45t/h manufacture methyl alcohol, the tolerance of the crude synthesis gas made by texaco gasification unit is 292.71t/h, gasification temperature about 1400 DEG C, pressure is about 64bar.And the composition of crude synthesis gas is as table 1:
The composition of table 1 crude synthesis gas
The gasification methyl alcohol system of above-mentioned integrated utilizing waste heat for refrigeration and carbon trapping is in the process of manufacture methyl alcohol, and utilizing waste heat for refrigeration unit absorbs the remaining cold energy 100% produced of heat and meets required-40 DEG C of colds of low-temperature rectisol, reduces about power consumption 90%, and unit methanol product CO
2discharge can reduce 1.29t, compares existing process, unit product CO
2quantity discharged reduces 46%.
Embodiment 2
As shown in Figure 5 and Figure 6, the present embodiment difference from Example 1 is: the gasification methyl alcohol system of a kind of integrated utilizing waste heat for refrigeration and carbon trapping, comprise texaco gasification unit 1, udst separation unit 2, water-gas shift unit 3, acid gas removal unit 4 and the methanol-fueled CLC and rectification cell 5 that connect successively, simultaneously the sulphur emissions mouth of described acid gas removal unit 4 and CO
2discharge outlet is connected to sulfur recovery unit 7 and CO
2multi-stage compression unit 6; Also comprise utilizing waste heat for refrigeration unit 8 ', the vapour outlet of described water-gas shift unit 3 is connected with the steam-in of utilizing waste heat for refrigeration unit 8 ', and the cooling water outlet of described utilizing waste heat for refrigeration unit 8 ' is connected with the entrance of cooling water of acid gas removal unit 4; Described CO
2the superheated water outlet of multi-stage compression unit 6 is connected with the water-in of water-gas shift unit 3.
Described utilizing waste heat for refrigeration unit 8 ' comprises producer 44, condenser 45, cold recovery device 46, vaporizer 48, resorber 49, solution heat exchanger 53 and pump 52; The steam-in of described producer 44 is connected with the vapour outlet of water-gas shift unit 3, and the cooling water outlet of described vaporizer 44 is connected with the entrance of cooling water of acid gas removal unit 4;
The ammonia outlet of described producer 44 is connected with the hot side inlet of condenser 45, the hot junction outlet of described condenser 45 is connected with the hot-side inlet of cold recovery device 46, described cold recovery device 46 is connected with the ammonia import of vaporizer 48 by expansion valve 47, the ammonia outlet of described vaporizer 48 is connected with the cold-side inlet of cold recovery device 46, the cold side outlet of described cold recovery device 46 is connected with the ammonia import of resorber 49, the ammoniacal liquor outlet of described resorber 49 is connected with the ammoniacal liquor import of solution heat exchanger 53 by pump 52, the ammoniacal liquor import of described solution heat exchanger 53 is connected with the strong aqua import of producer 44, the weak ammonia outlet of described producer 44 is connected with the hot-side inlet of solution heat exchanger 53, and the hot junction outlet of described solution heat exchanger 53 is connected with the spraying head of resorber 49 by solution decompression valve 51.
Difference between the present embodiment and embodiment 1 is only that utilizing waste heat for refrigeration unit style must only be supplied to acid gas removal unit 4 by the cold water containing cold, instead of is supplied to CO simultaneously
2stage compression list, 6 and acid gas removal unit 4.
Above-mentioned embodiment is the preferred embodiments of the present invention, can not limit the present invention, and any of other does not deviate from technical scheme of the present invention and the substitute mode of the change made or other equivalence, is included within protection scope of the present invention.
Claims (8)
1. the gasification methyl alcohol system of an integrated utilizing waste heat for refrigeration and carbon trapping, comprise texaco gasification unit, udst separation unit, water-gas shift unit, acid gas removal unit and the methanol-fueled CLC and rectification cell that connect successively, simultaneously the sulphur emissions mouth of described acid gas removal unit and CO
2discharge outlet is connected to sulfur recovery unit and CO
2multi-stage compression unit; It is characterized in that: also comprise utilizing waste heat for refrigeration unit, the vapour outlet of described water-gas shift unit is connected with the steam-in of utilizing waste heat for refrigeration unit, the cooling water outlet of described utilizing waste heat for refrigeration unit be connected with the entrance of cooling water of acid gas removal unit or described utilizing waste heat for refrigeration unit cooling water outlet simultaneously and CO
2the entrance of cooling water of multi-stage compression unit, the entrance of cooling water of acid gas removal unit connect; Described CO
2the superheated water outlet of multi-stage compression unit is connected with the waste heat boiler water-in of water-gas shift unit.
2. the gasification methyl alcohol system of integrated utilizing waste heat for refrigeration according to claim 1 and carbon trapping, is characterized in that: described utilizing waste heat for refrigeration unit comprises producer, condenser, cold recovery device, vaporizer, resorber, solution heat exchanger and pump; The steam-in of described producer is connected with the vapour outlet of water-gas shift unit, the cooling water outlet of described vaporizer be connected with the entrance of cooling water of acid gas removal unit or described vaporizer cooling water outlet simultaneously and CO
2the entrance of cooling water of multi-stage compression unit, the entrance of cooling water of acid gas removal unit connect;
The ammonia outlet of described producer is connected with the hot side inlet of condenser, the hot junction outlet of described condenser is connected with the hot-side inlet of cold recovery device, described cold recovery device is connected with the ammonia import of vaporizer by expansion valve, the ammonia outlet of described vaporizer is connected with the cold-side inlet of cold recovery device, the cold side outlet of described cold recovery device is connected with the ammonia import of resorber, the ammoniacal liquor outlet of described resorber is connected with the ammoniacal liquor import of solution heat exchanger by pump, and the ammoniacal liquor import of described solution heat exchanger is connected with the strong aqua import of producer; The weak ammonia outlet of described producer is connected with the hot-side inlet of solution heat exchanger, and the hot junction outlet of described solution heat exchanger is connected with the spraying head of resorber by solution decompression valve.
3. the gasification methyl alcohol system of integrated utilizing waste heat for refrigeration according to claim 1 and carbon trapping, is characterized in that: be provided with absorber cooler in the device shell of described resorber or outside device shell.
4. the gasification methyl alcohol system of integrated utilizing waste heat for refrigeration according to claim 2 and carbon trapping, it is characterized in that: described water-gas shift unit comprises the first shift-converter, second shift-converter, primary waste heat boiler, secondary waste heat boiler, first drum and the second drum, the inlet mouth of described first shift-converter is connected with udst separation unit, the described air outlet of the first shift-converter is connected with the hot side inlet of primary waste heat boiler, the hot junction outlet of described primary waste heat boiler is connected with the inlet mouth of the second shift-converter, the described air outlet of the second shift-converter is connected with the hot side inlet of secondary waste heat boiler, the hot junction outlet of described secondary waste heat boiler is connected with the synthesis gas import of acid gas removal unit,
Described CO
2the superheated water outlet of multi-stage compression unit is connected with the water-in of secondary waste heat boiler, and the superheated water outlet of described secondary waste heat boiler is connected with the superheated water entrance of the first drum, and the described vapour outlet of the first drum is connected with the steam-in of producer; The described hot water outlet of the first drum is connected with the water-in of primary waste heat boiler, and the superheated water outlet of described primary waste heat boiler is connected with the superheated water entrance of the second drum, and the described vapour outlet of the second drum is connected with the steam-in of producer.
5. the gasification methyl alcohol system of integrated utilizing waste heat for refrigeration according to claim 4 and carbon trapping, is characterized in that: described CO
2multi-stage compression unit comprises multiple CO
2compressor and and CO
2the compression cooler that number of compressors is equal, multiple described CO
2compressor and compression cooler are alternately connected successively, wherein, are positioned at the first CO
2the CO of compressor
2the CO of entrance and acid gas removal unit
2discharge outlet connects, and multiple cooling water inlet of described compression cooler is connected with the cooling water outlet of vaporizer.
6., based on the methanol process processed of gasification methyl alcohol system for the integrated utilizing waste heat for refrigeration described in claim 4 or 5 and carbon trapping, it is characterized in that, comprise the following steps:
(1) coal water slurry and oxygen form synthetic gas after entering texaco gasification unit, and described synthetic gas is successively by entering acid gas purifying unit after purifying and dedusting unit and water-gas shift unit, and acid gas purifying unit is by the CO in synthetic gas
2gas delivery out, then the CO separated
2gas enters CO
2multi-stage compression unit; The Clean synthesis gas that acid gas purifying unit produces enters methanol-fueled CLC and rectification cell from the syngas outlet of acid gas purifying unit, thus obtained refined methanol;
(2) in step (1), CO is entered
2the CO of multi-stage compression unit
2gas is compressed into liquid CO
2, CO
2multi-stage compression unit compression CO
2a large amount of superheated water is produced during gas, this superheated water is by the effect of primary waste heat boiler, secondary waste heat boiler, the first drum and the second drum in water-gas shift unit, superheated water is transformed into low pressure water vapor, low pressure water vapor heats obtained ammonia to the strong aqua in producer, this ammonia is successively by being transformed into cold liquefied ammonia after condenser and cold recovery device, this cold liquefied ammonia freezes to the water in vaporizer, thus obtained water coolant, this water coolant is by entering CO after vaporizer cooling water outlet
2multi-stage compression unit and acid gas removal unit, thus the cold that water coolers contains can be supplied in CO
2multi-stage compression unit and acid gas removal unit.
7. the methanol process processed of the gasification methyl alcohol system of integrated utilizing waste heat for refrigeration according to claim 6 and carbon trapping, it is characterized in that: in step (2), before strong aqua in producer and low pressure water vapor carry out heat exchange, namely, before the strong aqua in producer is heated by low-pressure steam, the concentration of strong aqua is 25% ~ 45%.
8. the methanol process processed of the gasification methyl alcohol system of integrated utilizing waste heat for refrigeration according to claim 6 and carbon trapping, it is characterized in that: in step (2), after the effect of superheated water by primary waste heat boiler, secondary waste heat boiler, the first drum and the second drum in water-gas shift unit, the low pressure water vapor of generation is the low-pressure steam for 0.7-1.5MPa.
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107032954A (en) * | 2017-05-03 | 2017-08-11 | 中为(上海)能源技术有限公司 | The method that methanol and its derivative are produced using underground coal gasification(UCG) product gas |
| CN109467049A (en) * | 2018-11-22 | 2019-03-15 | 中石化南京工程有限公司 | A kind of transform method and device of energy coupling |
| CN110642675A (en) * | 2018-06-26 | 2020-01-03 | 万华化学集团股份有限公司 | Energy-saving process for preparing methanol from coal |
| CN110699135A (en) * | 2019-11-20 | 2020-01-17 | 廊坊泛华石化设备有限公司 | Decarbonization method for producing methanol synthesis gas |
| CN111426099A (en) * | 2019-11-22 | 2020-07-17 | 国电康能科技股份有限公司 | Waste heat recovery device of subcritical carbon dioxide working medium |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN201151710Y (en) * | 2007-10-27 | 2008-11-19 | 太原海力丰科技发展有限公司 | Grading coal gasification device |
| WO2013131042A1 (en) * | 2012-03-01 | 2013-09-06 | The Trustees Of Princeton University | Processes for producing synthetic hydrocarbons from coal, biomass, and natural gas |
| CN203240840U (en) * | 2013-04-25 | 2013-10-16 | 新奥科技发展有限公司 | Energy saving system integrated by conversion section waste heat recovery and rectisol process refrigeration station |
| CN104017606A (en) * | 2014-06-24 | 2014-09-03 | 中国神华能源股份有限公司 | Coal water slurry gasification process system |
| CN204138611U (en) * | 2014-06-24 | 2015-02-04 | 中国神华能源股份有限公司 | Coal-water slurry gasification system |
-
2015
- 2015-07-09 CN CN201510400928.3A patent/CN104987279B/en not_active Expired - Fee Related
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN201151710Y (en) * | 2007-10-27 | 2008-11-19 | 太原海力丰科技发展有限公司 | Grading coal gasification device |
| WO2013131042A1 (en) * | 2012-03-01 | 2013-09-06 | The Trustees Of Princeton University | Processes for producing synthetic hydrocarbons from coal, biomass, and natural gas |
| CN203240840U (en) * | 2013-04-25 | 2013-10-16 | 新奥科技发展有限公司 | Energy saving system integrated by conversion section waste heat recovery and rectisol process refrigeration station |
| CN104017606A (en) * | 2014-06-24 | 2014-09-03 | 中国神华能源股份有限公司 | Coal water slurry gasification process system |
| CN204138611U (en) * | 2014-06-24 | 2015-02-04 | 中国神华能源股份有限公司 | Coal-water slurry gasification system |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107032954A (en) * | 2017-05-03 | 2017-08-11 | 中为(上海)能源技术有限公司 | The method that methanol and its derivative are produced using underground coal gasification(UCG) product gas |
| CN110642675A (en) * | 2018-06-26 | 2020-01-03 | 万华化学集团股份有限公司 | Energy-saving process for preparing methanol from coal |
| CN110642675B (en) * | 2018-06-26 | 2022-08-02 | 万华化学集团股份有限公司 | Energy-saving process for preparing methanol from coal |
| CN109467049A (en) * | 2018-11-22 | 2019-03-15 | 中石化南京工程有限公司 | A kind of transform method and device of energy coupling |
| CN110699135A (en) * | 2019-11-20 | 2020-01-17 | 廊坊泛华石化设备有限公司 | Decarbonization method for producing methanol synthesis gas |
| CN111426099A (en) * | 2019-11-22 | 2020-07-17 | 国电康能科技股份有限公司 | Waste heat recovery device of subcritical carbon dioxide working medium |
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