CN100503790C - Method of producing chemical product by double fuel reforming chemical system - Google Patents
Method of producing chemical product by double fuel reforming chemical system Download PDFInfo
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- 239000000126 substance Substances 0.000 title claims abstract description 108
- 239000000446 fuel Substances 0.000 title claims abstract description 77
- 238000002407 reforming Methods 0.000 title claims abstract description 44
- 238000000034 method Methods 0.000 title claims description 65
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 130
- 239000007789 gas Substances 0.000 claims abstract description 109
- 238000004519 manufacturing process Methods 0.000 claims abstract description 91
- 239000003245 coal Substances 0.000 claims abstract description 62
- 239000003345 natural gas Substances 0.000 claims abstract description 50
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims description 156
- 229910052739 hydrogen Inorganic materials 0.000 claims description 46
- 239000001257 hydrogen Substances 0.000 claims description 45
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 41
- 235000009508 confectionery Nutrition 0.000 claims description 38
- 238000006243 chemical reaction Methods 0.000 claims description 33
- 238000011084 recovery Methods 0.000 claims description 33
- 239000002918 waste heat Substances 0.000 claims description 32
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 27
- 238000006057 reforming reaction Methods 0.000 claims description 27
- 239000003546 flue gas Substances 0.000 claims description 24
- 239000002994 raw material Substances 0.000 claims description 22
- 239000000203 mixture Substances 0.000 claims description 21
- 150000002431 hydrogen Chemical class 0.000 claims description 18
- 238000000926 separation method Methods 0.000 claims description 16
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 12
- 238000010438 heat treatment Methods 0.000 claims description 9
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 8
- 230000006835 compression Effects 0.000 claims description 7
- 238000007906 compression Methods 0.000 claims description 7
- 238000000629 steam reforming Methods 0.000 claims description 7
- 229910021529 ammonia Inorganic materials 0.000 claims description 6
- 230000015572 biosynthetic process Effects 0.000 claims description 6
- 238000002485 combustion reaction Methods 0.000 claims description 6
- 238000000746 purification Methods 0.000 claims description 5
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 3
- 235000011089 carbon dioxide Nutrition 0.000 claims description 3
- 229910002091 carbon monoxide Inorganic materials 0.000 claims description 3
- 238000001816 cooling Methods 0.000 claims description 3
- 238000006477 desulfuration reaction Methods 0.000 claims description 3
- 230000023556 desulfurization Effects 0.000 claims description 3
- 239000003502 gasoline Substances 0.000 claims description 3
- 238000009434 installation Methods 0.000 claims description 3
- 238000003786 synthesis reaction Methods 0.000 claims description 3
- 239000012530 fluid Substances 0.000 claims description 2
- 238000011144 upstream manufacturing Methods 0.000 claims description 2
- 239000003034 coal gas Substances 0.000 abstract 1
- 239000002699 waste material Substances 0.000 abstract 1
- 238000005265 energy consumption Methods 0.000 description 18
- 230000009977 dual effect Effects 0.000 description 9
- 238000002309 gasification Methods 0.000 description 8
- 238000004140 cleaning Methods 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- 238000009841 combustion method Methods 0.000 description 2
- BZLVMXJERCGZMT-UHFFFAOYSA-N Methyl tert-butyl ether Chemical compound COC(C)(C)C BZLVMXJERCGZMT-UHFFFAOYSA-N 0.000 description 1
- 238000010795 Steam Flooding Methods 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 239000005864 Sulphur Substances 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 239000000654 additive Substances 0.000 description 1
- 230000000996 additive effect Effects 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 238000012824 chemical production Methods 0.000 description 1
- 230000000295 complement effect Effects 0.000 description 1
- 238000005261 decarburization Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000003317 industrial substance Substances 0.000 description 1
- 230000005764 inhibitory process Effects 0.000 description 1
- 230000010354 integration Effects 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/16—Combined cycle power plant [CCPP], or combined cycle gas turbine [CCGT]
- Y02E20/18—Integrated gasification combined cycle [IGCC], e.g. combined with carbon capture and storage [CCS]
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Abstract
The invention discloses a manufacturing method of double-fuel reforming chemical system, which is characterized by the following: utilizing coal and natural gas effectively; reforming natural gas through combust coal heat; preparing the clean synthetic gas without waste.
Description
Technical field
The present invention relates to chemical production technical field, is to be the method for raw material production Chemicals a kind of while with Sweet natural gas and coal.
Technical background
Methyl alcohol is the raw material of multiple Chemicals, the main raw material that it is produced as nonstaining property fuel, gasoline upgrading additive and methyl tertiary butyl ether and extremely people's attention.Follow the shortage of global petroleum resources, the utilization of Sweet natural gas has also produced the trend that promotes methanol production.
Sweet natural gas be cleaning, efficiently, the energy easily, its use is in development of world economy and improve in the environmental quality and play an important role.In recent years the China's natural gas reserve increasing is very fast, and " the West-east Gas engineering will be natural gas transport to 9 provinces and cities in the whole nation, for the China's natural gas industrial expansion has been created favourable condition.21 century China's natural gas output and consumption will be improved rapidly, its ratio in energy structure is formed will reach 6%～8%.The product that with the Sweet natural gas is raw material at present occupies critical role in chemical industry, be raw material production with the Sweet natural gas as the ammonia in the whole world 84% and 90% methyl alcohol.The gas chemical industry is with a long history, is doing a large amount of work aspect the production energy consumption reducing, and has reached in the 30GJ/t as the energy consumption advanced level of present international gas production methyl alcohol, and it is very difficult further to reduce production energy consumption on existing basis.
The methanol industry production that with the coal is raw material was also never interrupted.Since the eighties, having enlarged day by day and the industrial applications of advanced Coal Gasification Technology along with production-scale, is the synthetic Chemicals of raw material with the coal because cost will decrease and cause that again people pay attention to.In order to make full use of the abundant in coal resource, coal inhibition and generation chemical product also has industrial application always in China.Although Coal Gasification Technology has had bigger development, the process of energy consumption maximum remains gasification during as the feedstock production Chemicals with coal.And coal based synthetic gas contains sulphur etc. to the catalyzer objectionable impurities, and its ratio of carbon-hydrogen does not meet the needs of synthetic Chemicals yet, still needs synthetic gas following process processes such as desulfurization, conversion and decarburization, and this energy consumption that also causes preparing with coal Chemicals is higher.As at present advanced be that feedstock production methyl alcohol energy consumption is roughly 40～50GJ/t with the coal, be higher than Sweet natural gas and prepare methyl alcohol about 30%.In traditional Coal Chemical Industry industry, be unable to do without the coal gasification apparatus involve great expense, the ratio of coal gasification apparatus expense in total cost of equipment be up to 40%～50%, and causing with the coal be that the chemical plant investment of raw material is far longer than with the Sweet natural gas is the chemical plant of raw material.
Summary of the invention
The objective of the invention is to: at current be separately drawback and two kinds of fossil energies of coal/Sweet natural gas characteristics separately in the chemical producing system of raw material with coal and Sweet natural gas, provide a kind of coal and Sweet natural gas of using to be raw material production Chemicals method.This method significantly reduces the preparation raw material that Chemicals consumed under the prerequisite that does not increase existing equipment and investment, keep the characteristics of raw natural gas chemical industry cleaning simultaneously, thereby reach the purpose that cuts down the consumption of energy, and reduce investment.
Technical scheme of the present invention is as follows:
A kind of method of producing chemical product by double fuel reforming chemical system is provided, and is to utilize existing installation, uses Sweet natural gas and the coal method as raw material production simultaneously chemical product, its employed chemical system, comprise double fuel reforming reaction subsystem, waste heat recovery subsystem, Chemical Manufacture subsystem; It comprises following flow process:
A) double fuel reforming reaction subsystem flow process: steam and Sweet natural gas from the waste heat recovery subsystem mix back formation unstripped gas, enter preheater and arrived≤500 ℃ by flue gas heating, unstripped gas enters the reforming reaction pipe of reforming reactor then, be stacked with the required catalyzer of methane vapor reforming reaction in the reaction tubes, methane/steam reforming reaction takes place in unstripped gas in reaction tubes, simultaneously, the needed reaction heat of reforming reaction is by coal, the acquisition of in the burner hearth of reforming reactor, burning of off-gas and AIR MIXTURES, after the high-temperature flue gas that burning produces entered preheater heating raw gas subsequently, the middle temperature flue gas that is generated entered the waste heat recovery subsystem;
B) waste heat recovery subsystem flow process: high temperature unstripped gas, middle temperature flue gas that reforming process produces enter interchanger, in interchanger, be unstripped gas and low-temperature flue gas respectively with water heat exchange cooling, unstripped gas is supplied with the Chemical Manufacture subsystem, participate in the products production flow process, the steam that interchanger produces is divided into three strands, and one supplies with the reforming reaction subsystem, participates in reforming process, one is as outer defeated steam, and one enters steam turbine acting generating;
Flow process when C) the Chemical Manufacture subsystem is the methanol production subsystem: the unstripped gas that derives from the waste heat recovery subsystem boosts through the virgin gas compressor and with after circulation gas mixes, further be compressed to the synthetic required pressure of methyl alcohol through gas mixture compression machine again, form high pressure feed; High pressure feed enters methyl alcohol synthetic reactor through the regenerator preheating, and it is synthetic to carry out methyl alcohol, and synthetic product enters the separation and purification unit after the regenerator heat release, methyl alcohol is separated, and made with extra care and obtain methanol product; The isolated unreacting gas part in separation and purification unit enters gas mixture compression machine again as circulation gas, continues to participate in building-up reactions, and another part becomes and discharges gas and output to the reformation subsystem, acts as a fuel.
The method of described producing chemical product by double fuel reforming chemical system, the steam of its described waste heat recovery subsystem and Sweet natural gas mix, and ratio of mixture is 1:3～1:3.5.
The method of described producing chemical product by double fuel reforming chemical system, its described C) when the Chemical Manufacture subsystem is the hydrogen gas production subsystem: from the next unstripped gas of waste heat recovery subsystem, enter converter unit and generate hydrogen, enter hydrogen separation unit again, isolate hydrogen.
The method of described producing chemical product by double fuel reforming chemical system, the flow process of its described hydrogen gas production subsystem: the unstripped gas from the waste heat recovery subsystem comes, enter one section shift-converter or two sections shift-converters, CO in the synthetic gas is changed into CO
2, while generating portion hydrogen, the gas after conversion enters hydrogen separation unit, isolates hydrogen, and residual gas is supplied with the reformation subsystem and is acted as a fuel.
The method of described producing chemical product by double fuel reforming chemical system, its described residual gas, main component is unreacted methane, carbonic acid gas, carbon monoxide and small quantity of hydrogen, can supply with the reformation subsystem and act as a fuel.
The method of described producing chemical product by double fuel reforming chemical system, its described coal burns in burner hearth, adopts fixed bed, the combustion system of fluidized-bed or fluid injected bed, when adopting fluidized-bed, desulfurization in combustion processes.
The method of described producing chemical product by double fuel reforming chemical system, its described B) waste heat recovery subsystem flow process, also comprise after synthetic gas cools off condensed water is wherein reclaimed.
The method of described producing chemical product by double fuel reforming chemical system, its described C) Chemical Manufacture subsystem, be independent methanol production subsystem and independent hydrogen gas production subsystem or the series connection of the two, its series connection, be that the methanol production subsystem is the upstream equipment of hydrogen gas production subsystem, this moment, the unstripped gas unreacted that changes the methanol production subsystem into of hydrogen gas production subsystem discharged gas, and unreacted discharges gas and enters hydrogen separation unit, isolates hydrogen; Or enter one section shift-converter or two sections shift-converters, and enter hydrogen separation unit again, isolate hydrogen.
The method of described producing chemical product by double fuel reforming chemical system, its described C) the Chemical Manufacture subsystem, also can be with the synthetic gas is the anyon system of raw material, as DME (dme), ammonia and gasoline F-T (Fischer-Tropsch) synthetic subsystem.
The characteristics that the inventive method is different with Sweet natural gas according to coal are carried out the integrated complementary utilization with coal and Sweet natural gas, when making full use of clean energy (Sweet natural gas is all as industrial chemicals), rationally utilize coal.Double fuel chemical system of the present invention is to be the method for raw material production Chemicals a kind of while with Sweet natural gas and coal, this method combines the gas chemical industry's product production system and the coal of less energy-consumption, take into account the inexpensive characteristics of enriching of the cleaning of Sweet natural gas and coal, coal gasification and following process process have been avoided, realize cleaner production and the target that cuts down the consumption of energy, in the efficient utilization that realizes coal (comparing), keep lower cost of equipment (maintaining an equal level) with natural gas chemical plant with the use coal gasification apparatus.
The fuel dual system that the present invention proposes is compared with conventional system, and fractional energy savings can reach 5% at least.Under the prerequisite of not using expensive coal gasification apparatus, realize the efficient utilization of coal, reached the purpose that reduces cost of equipment.
The present invention is the method for the double fuel production chemical product of raw material with Sweet natural gas and coal, compare with the method for the production chemical product of a kind of raw material of existing simple usefulness, have following characteristics: (1) utilizes cheap coal, substitute in traditional Sweet natural gas steam reforming technology and account for Sweet natural gas total burn-off 1/3 and the higher fuel natural gas of price, reduce the production cost of synthetic gas; (2) with different chemical system organic integration, remedy the synthetic gas that exists when two systems produce separately and utilized unreasonable problem, capacity usage ratio is improved, save the energy and reduced production cost.
In sum,, rely on the price advantage of raw material, adopt the method for double fuel production chemical product of the present invention, the production cost of Chemicals and energy consumption are reduced significantly, practical prospect is arranged very much in coal and the abundant area of natural gas source.
Description of drawings
Fig. 1. for the present invention is the method flow synoptic diagram of the double fuel production chemical product of raw material with Sweet natural gas and coal;
Fig. 2. be double fuel reformation subsystem schematic flow sheet;
Fig. 3. be waste heat recovery subsystem process flow sheet
Fig. 4. be methanol production subsystem schematic flow sheet;
Fig. 5. be hydrogen gas production subsystem schematic flow sheet.
Embodiment
See also Fig. 1, Fig. 2, Fig. 3, the method for producing chemical product by double fuel reforming chemical system of the present invention is to utilize existing installation, does not increase under the situation of investment, uses Sweet natural gas and the coal method as raw material production simultaneously chemical product.Employed chemical system mainly comprises following three subsystems: double fuel reforming reaction subsystem 1, waste heat recovery subsystem 2, Chemical Manufacture subsystem 3.
Method provided by the invention is:
Use coal to replace Sweet natural gas as reformation thermal source fuel, in double fuel reformation subsystem 1, produce the synthetic gas of high-quality cleaning, high-temperature flue gas and synthetic gas from double fuel reformation subsystem 1 enter waste heat recovery subsystem 2 recovery heats, produce the compressor in the high pressure steam drive turbine drive system, and extract steam out from turbine and supply with reformation subsystem 1 reactant as the double fuel reforming reaction, unnecessary steam is defeated outward as product.Cooled synthetic gas is sent in the Chemical Manufacture subsystem 3, the production chemical product, then off-gas is sent in the reformation subsystem 1 and coal together as the fuel of reformation subsystem 1.
The double fuel reformation subsystem 1 that the present invention uses, its technical process is:
Mix the back with Sweet natural gas 4 from the steam 5 of waste heat recovery subsystem 2 and form unstripped gas, enter preheater 16 by about flue gas heating to 500 ℃.Unstripped gas enters reforming reactor 17 then, reforming reactor 17 is made up of reforming reaction pipe 18 and burner hearth, the catalyzer of placing in the reaction tubes 18 can be any methane vapor reforming catalyzer, methane/steam reforming reaction takes place in unstripped gas in reaction tubes 18, its reaction equation is as follows:
Methane/steam reforming reaction is a strong endothermic reaction, and the needed reaction heat of reforming reaction is by the acquisition of burning in the burner hearth of reforming reactor 17 of coal, off-gas and AIR MIXTURES.The also available CO of part methane in the unstripped gas
2Replace, this moment, reaction was carried out to the right.Use CO
2Can obtain the synthetic gas of high ratio of carbon-hydrogen behind the instead of part methane, by changing the synthetic gas that the amount of substituting can obtain to be used to prepare different Chemicals.The high-temperature flue gas 10 that burning produces in the burner hearth enters preheater 16 heating raw gas, enters waste heat recovery subsystem 2 then.Burning in the burner hearth can be adopted multiple mode, for example adopts the combustion method of the fluidized-bed of the NOx can effectively reduce in the flue gas and SOx content.
Chemicals provided by the invention are produced subsystem 3 can produce multiple Chemicals, can dispose the production system of a certain Chemicals according to demand, constitutes different Chemicals and produces subsystem.For example methyl alcohol system, dme system, hydrogen gas system and synthesis ammonia system etc.Also can produce two or more Chemicals simultaneously, for example methyl alcohol/hydrogen gas system, methyl alcohol/synthetic ammonia and dme/synthesis ammonia system etc.
Comprise steam turbine in the waste heat recovery subsystem 2 of the present invention.The high pressure superheated steam that waste heat recovery subsystem 2 is produced enters the compressor in the steam turbine drive system.Extract the part middle pressure steam out from steam turbine simultaneously, participate in methane reforming reaction.Unnecessary steam can be used as commodity and offers other user.
The present invention is further described below in conjunction with drawings and Examples.
Please again referring to Fig. 1, Fig. 2, Sweet natural gas 4 and (be generally 1:3-1:3.5) according to a certain percentage from the water vapor 5 of turbine subsystem and mix, in preheater 16, after high-temperature flue gas 10 preheatings, enter in the reaction tubes 18 of double fuel reforming reaction subsystem 1 catalyst surface generation reforming reaction in reaction tubes 18; Meanwhile, coal 9 and also enter reforming reactor 17 from the off-gas 15 of Chemical Manufacture subsystem 3, with air generation combustion reactions, the heat of high temperature that burning is emitted is supplied with reforming reaction in the furnace chamber outside reaction tubes 18.Warm flue gas 11 in becoming behind the high temperature unstripped gas 6 that reforming reaction produces and 10 preheating Sweet natural gases of the high-temperature flue gas behind the coal combustion and the water vapour, enter waste heat recovery subsystem 2, heating high-pressure water 13, produce high pressure superheated steam and drive turbine driving technology compressor, also extract part steam 5 out and be defeated by double fuel reformation subsystem 1 except that the drive compression machine in steam turbine, unnecessary steam 14 is defeated outward as product.Low-temperature flue gas 12 after the heat release directly is discharged in the environment, and the unstripped gas 7 that waste heat recovery subsystem 2 produces enters Chemical Manufacture subsystem 3.Chemical Manufacture subsystem 3 production chemical products 8 give off off-gas 15 simultaneously, and these off-gas 15 can enter reformation subsystem 1 as the fuel of reforming in double fuel reforming reaction subsystem 1, also can be used for other purposes, as hydrogen manufacturing.In the present embodiment as fuel reforming.
Fig. 2 is double fuel reformation subsystem 1 schema of the present invention.Mix the back from the steam 5 of waste heat recovery subsystem 2 and Sweet natural gas 4 and form unstripped gass, enter preheater 16 by flue gas heating to 500 ℃.Unstripped gas enters reforming reactor 17 then, reforming reactor 17 is made up of reforming reaction pipe 18 and burner hearth, be stacked with the required catalyzer of methane vapor reforming reaction in the reaction tubes 18, methane/steam reforming reaction takes place in unstripped gas in reaction tubes 18, methane/steam reforming reaction is a strong endothermic reaction, and the needed reaction heat of reforming reaction is by the acquisition of burning in the burner hearth of reforming reactor 17 of coal 9, off-gas 15 and AIR MIXTURES.The high-temperature flue gas 10 that burning produces enters preheater 16 heating raw gas subsequently, then in warm flue gas 11 enter waste heat recovery subsystem 2.The burning of coal 9 in burner hearth can be adopted multiple mode, and for example in order to reduce the pollution of coal 9 burning to air, the burning of coal 9 in burner hearth can be adopted the combustion method of fluidized-bed, effectively reduces NOx in the flue gas and the content of SOx.
Fig. 3 is waste heat recovery subsystem 2 process flow sheets.High temperature unstripped gas 6 that reforming process produces and middle temperature flue gas 11 are unstripped gas 7 and low-temperature flue gas 12 with water 13 heat exchange cooling respectively in interchanger 34.The steam that produces is divided into three strands, and one 5 supplies with reforming process, and one is 14 as outer defeated steam, and one 32 enters steam turbine 33 acting generatings.
Fig. 4 is a kind of for Chemical Manufacture subsystem 3 of the present invention: methanol production subsystem process flow sheet.Boost through virgin gas compressors 19 and, further be compressed to the synthetic required pressure of methyl alcohol, formation high pressure feed 25 through gas mixture compression machine 20 again by the unstripped gas that derives from waste heat recovery subsystem 27 shown in Figure 1 with after circulation gas 24 mixes.High pressure feed 25 enters methyl alcohol synthetic reactor 22 through regenerator 21 preheatings, carries out methyl alcohol and synthesizes.Synthetic product enters separation and purification unit 23 methyl alcohol is separated after regenerator 21 heat releases, and makes with extra care and obtain methanol product 8.Part unreacting gas continues to participate in building-up reactions as circulation gas 24, and another part discharges gas 15 and outputs to reformation subsystem 1, acts as a fuel.
Fig. 5 is the another kind of Chemical Manufacture subsystem 3 of the present invention: hydrogen gas production subsystem process flow sheet.Unstripped gas 7 from waste heat recovery subsystem 2 enters one section shift-converter 27 and two sections shift-converters 28 successively as shown in Figure 1, and CO in the synthetic gas is changed into CO
2, while generating portion hydrogen.In two sections shift-converters 28, the gas after conversion enters hydrogen separation unit 29, isolates hydrogen 30.Residual gas 31 main components are unreacted methane, carbonic acid gas, carbon monoxide and small quantity of hydrogen etc., can supply with reformation subsystem 1 and act as a fuel.When not pursuing maximum CO transformation efficiency, can be simplified to one section conversion or fully phase out conversion process.Hydrogen manufacturing this moment amount reduces, but can provide more fuel to reformation subsystem 1.
Methanol production subsystem and hydrogen gas production subsystem can be independent subsystem separately in the embodiments of the invention, also can be with these two subsystem series connection, this moment, the unstripped gas of hydrogen gas production subsystem discharged gas 15 by the 7 original unreacteds that change the methanol production subsystem into.Above subsystem can be selected when designing according to different production needs.
Embodiment:
Each logistics parameter in the inventive method, with reference to accompanying drawing, as shown in table 6.
Table 1 Sweet natural gas and synthetic gas state parameter
Table 2 reforming reactor outlet gas composition
Table 3 double fuel methyl alcohol system performance relatively
Table 4 conversion pneumatolytic branch
Table 5 double fuel hydrogen generating system performance relatively
Each logistics parameter of table 6
Claims (9)
1. the method for a producing chemical product by double fuel reforming chemical system is to utilize existing installation, uses Sweet natural gas and the coal method as raw material production simultaneously chemical product, its employed chemical system, comprise double fuel reforming reaction subsystem, waste heat recovery subsystem, Chemical Manufacture subsystem; It is characterized in that: comprise following flow process:
A) double fuel reforming reaction subsystem flow process: steam and Sweet natural gas from the waste heat recovery subsystem mix back formation unstripped gas, enter preheater by about flue gas heating to 500 ℃, unstripped gas enters the reforming reaction pipe of reforming reactor then, be filled with the required catalyzer of methane vapor reforming reaction in the reaction tubes, methane/steam reforming reaction takes place in unstripped gas in reaction tubes, simultaneously, the needed reaction heat of reforming reaction is by coal, the acquisition of in the burner hearth of reforming reactor, burning of off-gas and AIR MIXTURES, after the high-temperature flue gas that burning produces entered preheater heating raw gas subsequently, the middle temperature flue gas that is generated entered the waste heat recovery subsystem;
B) waste heat recovery subsystem flow process: high-temperature synthesis gas, middle temperature flue gas that reforming process produces enter interchanger, in interchanger, be synthetic gas and low-temperature flue gas respectively with water heat exchange cooling, synthetic gas is supplied with the Chemical Manufacture subsystem, the steam that interchanger produces is divided into three strands, one supplies with the reforming reaction process, one is as outer defeated steam, and one enters steam turbine work done generating;
Flow process when C) the Chemical Manufacture subsystem is the methanol production subsystem: the synthetic gas that derives from the waste heat recovery subsystem boosts through the virgin gas compressor and with after circulation gas mixes, further be compressed to the synthetic required pressure of methyl alcohol through gas mixture compression machine again, form the high pressure synthetic gas; The high pressure synthetic gas enters methyl alcohol synthetic reactor through the regenerator preheating, and it is synthetic to carry out methyl alcohol, and synthetic product enters the separation and purification unit after the regenerator heat release, methyl alcohol is separated, and made with extra care and obtain methanol product; The isolated unreacting gas part in separation and purification unit enters gas mixture compression machine again as circulation gas, continues to participate in building-up reactions, and another part becomes and discharges gas and output to the reformation subsystem, acts as a fuel.
2. according to the method for the described producing chemical product by double fuel reforming chemical system of claim 1, it is characterized in that: the steam of described waste heat recovery subsystem and Sweet natural gas mix, and ratio of mixture is 1:3～1:3.5.
3. according to the method for the described producing chemical product by double fuel reforming chemical system of claim 1, it is characterized in that: when described C) the Chemical Manufacture subsystem is the hydrogen gas production subsystem: from the next synthetic gas of waste heat recovery subsystem, enter converter unit and generate hydrogen, enter hydrogen separation unit again, isolate hydrogen.
4. according to the method for the described producing chemical product by double fuel reforming chemical system of claim 3, it is characterized in that: the flow process of described hydrogen gas production subsystem: from the next synthetic gas of waste heat recovery subsystem, enter one section shift-converter or two sections shift-converters, CO in the synthetic gas is changed into CO
2, while generating portion hydrogen, the gas after conversion enters hydrogen separation unit, isolates hydrogen, and residual gas is supplied with the reformation subsystem and is acted as a fuel.
5. according to the method for the described producing chemical product by double fuel reforming chemical system of claim 4, it is characterized in that: described residual gas, main component are unreacted methane, carbonic acid gas, carbon monoxide and small quantity of hydrogen, can supply with the reformation subsystem and act as a fuel.
6. according to the method for the described producing chemical product by double fuel reforming chemical system of claim 1, it is characterized in that: described coal burns in burner hearth, adopts fixed bed, the combustion system of fluidized-bed or fluid injected bed, and when adopting fluidized-bed, desulfurization in combustion processes.
7. according to the method for the described producing chemical product by double fuel reforming chemical system of claim 1, it is characterized in that: waste heat recovery subsystem flow process described B) also comprises after synthetic gas cools off condensed water is wherein reclaimed.
8. according to the method for claim 1,3 or 4 described producing chemical product by double fuel reforming chemical system, it is characterized in that: Chemical Manufacture subsystem described C), be independent methanol production subsystem and independent hydrogen gas production subsystem or the series connection of the two, its series connection, be that the methanol production subsystem is the upstream equipment of hydrogen gas production subsystem, this moment, the unstripped gas unreacted that changes the methanol production subsystem into of hydrogen gas production subsystem discharged gas, unreacted discharges gas and enters hydrogen separation unit, isolates hydrogen; Or enter one section shift-converter or two sections shift-converters, and enter hydrogen separation unit again, isolate hydrogen.
9. according to the method for the described producing chemical product by double fuel reforming chemical system of claim 1, it is characterized in that: Chemical Manufacture subsystem described C), also for being DME, ammonia or the gasoline F-T synthetic subsystem of raw material with the synthetic gas.
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| CN101285004B (en) * | 2007-04-11 | 2010-12-15 | 中国科学院工程热物理研究所 | Multifunctional energy resource system |
| WO2011017630A1 (en) * | 2009-08-06 | 2011-02-10 | Greatpoint Energy, Inc. | Processes for hydromethanation of a carbonaceous feedstock |
| CN101993730B (en) * | 2009-08-12 | 2013-01-02 | 中国科学院工程热物理研究所 | Multifunctional energy system based on appropriate conversion of chemical energy of fossil fuel |
| CN102071062B (en) * | 2010-07-02 | 2013-04-24 | 陕西神木化学工业有限公司 | Method for Texaco gasification process oven |
| CN102173974B (en) * | 2010-12-22 | 2013-03-20 | 中国石油化工集团公司 | Method for heating alkane by heating furnace hot smoke |
| CN103939933A (en) * | 2013-01-21 | 2014-07-23 | 王宜祥 | High-pressure large boiler without smoke and heat losses |
| EP3018094A1 (en) * | 2014-11-06 | 2016-05-11 | Casale SA | Process for producing a synthesis gas |
| CN108865285A (en) * | 2018-07-16 | 2018-11-23 | 西南石油大学 | It is a kind of using coal and natural gas as the oil of raw material-Electricity Federation production. art |
| CN111484394B (en) * | 2020-04-08 | 2022-01-25 | 华南农业大学 | Method and system for synthesizing methanol by in-situ catalytic gas preparation of combustible ice |
| CN115011981A (en) * | 2022-05-11 | 2022-09-06 | 浦江思欣通科技有限公司 | Hydrogen production equipment and hydrogen production method by coupling electrolyzed water with methane-rich gas |
| CN117000186B (en) * | 2023-09-27 | 2024-01-05 | 内蒙古东景生物环保科技有限公司 | Energy-saving natural gas steam reformer |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2003238973A (en) * | 2001-09-28 | 2003-08-27 | Ebara Corp | Method for reforming combustible gas, apparatus for reforming combustible gas and apparatus for gasification |
| CN1557694A (en) * | 2004-01-16 | 2004-12-29 | 东南大学 | Method and apparatus for producing hydrogen by natural gas using two-stage fluid bed reformer |
-
2005
- 2005-09-01 CN CN 200510093689 patent/CN100503790C/en active Active
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2003238973A (en) * | 2001-09-28 | 2003-08-27 | Ebara Corp | Method for reforming combustible gas, apparatus for reforming combustible gas and apparatus for gasification |
| CN1557694A (en) * | 2004-01-16 | 2004-12-29 | 东南大学 | Method and apparatus for producing hydrogen by natural gas using two-stage fluid bed reformer |
Non-Patent Citations (2)
| Title |
|---|
| Exergy analysis of coal-based polygeneration systerm forpower and chemical production. Lin Gao, Hongguang Jin, Zelong Liu, Danxing Zheng.Energy,Vol.29 . 2004 * |
| 新型双燃料重整联合循环发电***. 韩巍，徐威，金红光.中国工程热物理学会第十一届年会工程热力学与能源利用学术会议. 2004 * |
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