CN201109766Y - Equipment system for producing dimethyl ether by garbage and biomass raw material - Google Patents
Equipment system for producing dimethyl ether by garbage and biomass raw material Download PDFInfo
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- CN201109766Y CN201109766Y CNU2007201833234U CN200720183323U CN201109766Y CN 201109766 Y CN201109766 Y CN 201109766Y CN U2007201833234 U CNU2007201833234 U CN U2007201833234U CN 200720183323 U CN200720183323 U CN 200720183323U CN 201109766 Y CN201109766 Y CN 201109766Y
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- 239000002028 Biomass Substances 0.000 title claims abstract description 42
- 239000010813 municipal solid waste Substances 0.000 title claims description 55
- LCGLNKUTAGEVQW-UHFFFAOYSA-N Dimethyl ether Chemical compound COC LCGLNKUTAGEVQW-UHFFFAOYSA-N 0.000 title abstract description 34
- 239000002994 raw material Substances 0.000 title abstract description 27
- 239000007789 gas Substances 0.000 claims abstract description 134
- 239000001257 hydrogen Substances 0.000 claims abstract description 90
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 90
- 230000015572 biosynthetic process Effects 0.000 claims abstract description 79
- 238000003786 synthesis reaction Methods 0.000 claims abstract description 79
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 73
- 238000009272 plasma gasification Methods 0.000 claims abstract description 60
- 239000002918 waste heat Substances 0.000 claims abstract description 35
- 238000010521 absorption reaction Methods 0.000 claims abstract description 32
- 238000002309 gasification Methods 0.000 claims abstract description 32
- 238000002485 combustion reaction Methods 0.000 claims abstract description 30
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims description 102
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 84
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 74
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- 239000007788 liquid Substances 0.000 claims description 47
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- 239000000463 material Substances 0.000 claims description 16
- 238000005325 percolation Methods 0.000 claims description 11
- 238000005984 hydrogenation reaction Methods 0.000 claims description 9
- 238000006555 catalytic reaction Methods 0.000 claims description 8
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- 210000001015 abdomen Anatomy 0.000 claims description 7
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- 239000005416 organic matter Substances 0.000 claims description 3
- 238000006243 chemical reaction Methods 0.000 abstract description 31
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- 150000002013 dioxins Chemical class 0.000 abstract description 14
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- 238000012545 processing Methods 0.000 abstract description 6
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- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 20
- 150000002431 hydrogen Chemical class 0.000 description 16
- 239000003795 chemical substances by application Substances 0.000 description 13
- 238000000034 method Methods 0.000 description 13
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- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 11
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- 238000007599 discharging Methods 0.000 description 10
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- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 5
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- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 5
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- 239000001301 oxygen Substances 0.000 description 5
- 229910052760 oxygen Inorganic materials 0.000 description 5
- 239000002956 ash Substances 0.000 description 4
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- 235000011089 carbon dioxide Nutrition 0.000 description 4
- 239000000571 coke Substances 0.000 description 4
- 238000006298 dechlorination reaction Methods 0.000 description 4
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- 238000003860 storage Methods 0.000 description 4
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 3
- 239000001569 carbon dioxide Substances 0.000 description 3
- 235000009508 confectionery Nutrition 0.000 description 3
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- ODINCKMPIJJUCX-UHFFFAOYSA-N Calcium oxide Chemical compound [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 description 2
- 241000196324 Embryophyta Species 0.000 description 2
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 2
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- 235000017491 Bambusa tulda Nutrition 0.000 description 1
- 241001330002 Bambuseae Species 0.000 description 1
- VYZAMTAEIAYCRO-UHFFFAOYSA-N Chromium Chemical compound [Cr] VYZAMTAEIAYCRO-UHFFFAOYSA-N 0.000 description 1
- KRHYYFGTRYWZRS-UHFFFAOYSA-N Fluorane Chemical compound F KRHYYFGTRYWZRS-UHFFFAOYSA-N 0.000 description 1
- 235000014676 Phragmites communis Nutrition 0.000 description 1
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- 125000004435 hydrogen atom Chemical group [H]* 0.000 description 1
- 229910000041 hydrogen chloride Inorganic materials 0.000 description 1
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 description 1
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- QSHDDOUJBYECFT-UHFFFAOYSA-N mercury Chemical compound [Hg] QSHDDOUJBYECFT-UHFFFAOYSA-N 0.000 description 1
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Abstract
An equipment system for producing dimethyl ether by waste and biomass raw material relates to an equipment system for processing waste incineration and producing dimethyl ether, and is mainly composed of a plasma gasification reacting furnace, a waste heat boiler, an absorption reactor, a dust catcher, a synthesis reactor, a knockout tower and a dimethyl ether store tank. The waste and biomass raw material are fed in the plasma gasification reacting furnace to realize combustion reaction in the furnace in the condition of air isolation, so that the waste and biomass raw material are transferred into hydrogen-rich synthesis gas by pyrogenation and gasification reactions. After temperature reduction, dechloridation/desulphurization and dust abatement, the hydrogen-rich synthesis gas is fed in the synthesis reactor to synthesize dimethyl ether once. The system does not have smoke gas exhaust, efficiently eliminates violent toxic dioxins, really realizes harmless, reducing and resourceful processing of waste, and has outstanding environment-friendly and ecological effects. The scale of the equipment system can be large or small. All towns and cities of town, countries, cities, as well as cities above province level can establish product lines so as to have easy popularization.
Description
Affiliated technical field
The utility model relates to the production equipment system of incineration treatment of garbage and dme.
Background technology
Current, energy shortage, the situation is tense in environmental protection, and rubbish overflows.Rubbish is along with the continuous expansion of the development of Chinese national economy and city size just increases sharply with 10% speed, and the content of its objectionable constituent is also more and more higher, as handle bad, to pollute the environment, threaten people health, the progress that this not only can restrict society also can have influence on the Sustainable development of national economy.Current, China adopts landfill method to handle domestic waste in the major part area, and this not only need take a large amount of soils, waste resource, and easy leakage of nuisance caused secondary pollution; Burning method can be accomplished minimizing, recycling treatment domestic refuse, but the major objective that burning method processing domestic refuse is pursued is can be rubbish fully burning in incinerator, next is only the recovery of energy, water content is big, hydrogen cloride concentration is high because the consumer waste incineration flue gas has, material there is bigger corrodibility, can not be arranged on heat-energy recovering apparatus the severe radiation district and heat energy recovery rate is affected, so the resource utilization level of application of burning method processing domestic refuse is limited; Domestic waste is handled with waste incineration and generating electricity in some area, but there is following shortcoming in waste incineration and generating electricity: 1. flue gas, CO2 emissions are big, pollutent has dust, hydrogenchloride, hydrogen fluoride, oxysulfide, oxynitride, carcinogenic violent in toxicity (Dioxins, furans), heavy metal (mercury, lead, chromium etc.) in the flue gas, though flue gas purification system is arranged, but be difficult to eliminate fully, particularly carcinogenic violent in toxicity (Dioxins, the furans) discharging that exceeds standard also lacks the reliable NO of technology at present
xTerminal purification process with Dioxins etc.; 2. need to add auxiliary fuel, consume petroleum or coal resources; 3. be major objective with the treating refuse, energy conversion rate is low, only is about 20%, and 80% resource is wasted, thereby resource utilization degree is low; 4. can only build garbage incinerating power plant in economically developed big city, the waste resources amount of small and medium-sized cities is not suitable for building refuse-burning plant, thereby can not popularization and application.
China is a large agricultural country, and biomass resource is very abundant, and only non-wood-fibers such as straw, wheat straw, reed, bamboo are just produced per year and surpassed 1,000,000,000 tons, add a large amount of wood machining residues, all are the huge energy " warehouse ".Yet the present agricultural surplus materials wasting of resources of China is surprising, except that the small portion rural area is used for the fermentation and biogas production, major part all by directly burning, landfill, rotted.
Dme acts as a fuel and uses is to put forward recent years, dme is easy to liquefaction, press a little and be liquid and easily store, alternative fuel as domestic fuel and fuel oil for vehicles, the character of dme liquefied gas is more superior than oil liquefied gas, himself contains oxygen dme, and the not over-emitting black exhaust that can fully burn is not analysed carbon, no raffinate, pollutent and CO
2Discharge capacity is low, harmless to ozonosphere, is a kind of ideal clean fuel.Current, the use of oil liquefied gas is quite universal, substitutes the field as automobile fuel and domestic fuel, and dme has very fine market outlook.Current, producing dme both at home and abroad mainly is transformed by Nonrenewable energy resources such as coal, Sweet natural gases, in switching process, wasted nearly half energy, still do not break away from dependence to fossil energies such as coal, Sweet natural gases, the consumption pressure of following coal or Sweet natural gas will strengthen, thereby can't fundamentally solve energy problem.As being the raw material dme with rubbish, biomass, just can obtain dual beneficial effect, the one, can solve problem of environmental pollution, because of dme does not in use have SO
2Discharging, the CO of generation
2Need a large amount of CO of absorbing in gas and the growing process
2Quantitatively keep balance, can be described as CO
2Zero release, environmental protection and ecological effect are outstanding, to improving the atmosphere acid rain environment, reduce carbon dioxide content in the atmosphere, thereby alleviate Greenhouse effect great benefit are arranged all; The 2nd, can replace fossil oil, can break away from dependence to the oil coal resources.But because the characteristics of domestic refuse biomass are moisture oxygen height, many violent in toxicity Dioxins that easily generate of low, the chloride thing of calorific value of containing, can only produce not high synthetic gas of calorific value or bio oil, not reach the quality requirements of producing dme with general processing unit.
The utility model content
The purpose of this utility model is the shortcoming that will overcome prior art and equipment, is raw material production clean energy dme with rubbish, biomass.Described rubbish, biomass material comprise: domestic waste, medical waste, people's domestic animals manure, animal corpse, the wooden matrix waste material in architectural decoration building site, industrial high molecular waste material, agricultural wastes, forestry waste, wood working waste, waterplant.In order to achieve the above object, the utility model is with rubbish, biomass are that the device systems of raw material production dme is mainly by crusher (6), winnowing machine (7), feeding screw (9), plasma gasification Reaktionsofen (10), plasma burner (44), plasma body working power (13), waste heat boiler (15), induced draft fan (40), absorption reactor thermally (18), fly-ash separator (20), feed gas compressor (22), synthesis reactor (23), knockout tower (28), return liquid compressor (27), compressor (29), water cooler (30), dme basin (31) is formed, wherein: the discharge port of crusher (6) is connected winnowing machine (7), the organic matter rubbish outlet of winnowing machine (7) faces the hopper (8) on the feeding screw (9), and the discharge port of feeding screw (9) puts in the abdomen of plasma gasification Reaktionsofen (10); Plasma burner (44) is installed in the side, combustion chamber of gasification reacting furnace (10) bottom, and the power output end of plasma body working power (13) is connected to the power input interface of plasma burner (44) by supply lead; The synthetic gas output interface of plasma gasification Reaktionsofen (10) is connected to waste heat boiler (15), and waste heat boiler (15) is by the air suction inlet of pipe connection to induced draft fan (40); The air outlet of induced draft fan (40) is by the inlet of pipe connection to absorption reactor thermally (18), and the outlet of absorption reactor thermally (18) is connected to the import of fly-ash separator (20), and the outlet of fly-ash separator (20) is connected to the suction port of feed gas compressor (22); The outlet of feed gas compressor (22) is connected to the unstripped gas inlet of synthesis reactor (23), the product outlet of synthesis reactor (23) is connected to the product inlet of knockout tower (28), the methyl alcohol of knockout tower (28) returns the suction port that the liquid outlet is connected to go back to liquid compressor (27), and the outlet of returning liquid compressor (27) is connected to time liquid input interface of synthesis reactor (23) by liquid returning tube (25); The product outlet of knockout tower (28) is connected to the suction port of compressor (29), and the outlet of compressor (29) is connected to the product inlet of water cooler (30), and the product outlet of water cooler (30) is connected to dme basin (31).
The utility model is with agricultural wastes, forestry waste, the wood working waste, the biomass of waterplant and so on are that the device systems of raw material production dme is mainly by feeding screw (9), plasma gasification Reaktionsofen (10), plasma burner (44), plasma body working power (13), waste heat boiler (15), induced draft fan (40), fly-ash separator (20), feed gas compressor (22), synthesis reactor (23), knockout tower (28), return liquid compressor (27), compressor (29), water cooler (30), dme basin (31) is formed, wherein: hopper (8) is arranged on the feeding screw (9), and the discharge port of feeding screw (9) puts in the abdomen of plasma gasification Reaktionsofen (10); Plasma burner (44) is installed in the lower combustion chamber side of gasification reacting furnace (10), and the power output end of plasma body working power (13) is connected to the power input interface of plasma burner (44) by supply lead; The synthetic gas output interface of plasma gasification Reaktionsofen (10) is connected to waste heat boiler (15), and waste heat boiler (15) is by the air suction inlet of pipe connection to induced draft fan (40); The air outlet of induced draft fan (40) is by the import of pipe connection to fly-ash separator (20), and the outlet of fly-ash separator (20) is connected to the suction port of feed gas compressor (22); The outlet of feed gas compressor (22) is connected to the unstripped gas inlet of synthesis reactor (23), the product outlet of synthesis reactor (23) is connected to the product inlet of knockout tower (28), the methyl alcohol of knockout tower (28) returns the suction port that the liquid outlet is connected to go back to liquid compressor (27), and the outlet of returning liquid compressor (27) is connected to time liquid input interface of synthesis reactor (23) by liquid returning tube (25); The product outlet of knockout tower (28) is connected to the suction port of compressor (29), and the outlet of compressor (29) is connected to the product input aperture of water cooler (30), and the product outlet of water cooler (30) is connected to dme basin (31).
Above-mentioned device systems is characterized in that described plasma burner (44) is more than one, at least one.
The utility model also takes to be connected to by flue gas recirculation pipe (11) at the exhanst gas outlet on plasma gasification Reaktionsofen (10) top the air compartment of plasma gasification Reaktionsofen (10) bottom; Or being connected to the air suction inlet of flue gas recirculation blower fan (43) by flue gas recirculation pipe (11) at the exhanst gas outlet on plasma gasification Reaktionsofen (10) top, the air outlet of flue gas recirculation blower fan (43) is connected to the air compartment of plasma gasification Reaktionsofen (10) bottom.By smoke circulating device, the flue gas that generates in the stove, water vapor, methane, pyrolysis gas, steam state tar are delivered to the combustion zone of stove bottom and carried out gasification reaction and reformation, disintegrate the violent in toxicity Dioxins simultaneously.Be in the device systems of raw material production dme with rubbish, biomass, the utility model also also is equipped with catalysis deodorization device (12) on the pipeline of flue gas recirculation pipe (11), heat energy with circulating flue gas heats catalysis deodorization device (12), by vacuum fan (3), (63) mephitic air of refuse pit (55) and rubbish discharging platform (61) top is sent into then and is carried out in the catalysis deodorization device (12) entering atmosphere after deodorizing sterilizing is handled.In the biomass with agricultural wastes, forestry waste, wood working waste, waterplant and so on is in the device systems of raw material production dme, the utility model also also is equipped with heat exchanger (12b) on the pipeline of flue gas recirculation pipe (11), be used for reclaiming heat energy.
In the above-mentioned device systems, go up return-air outlet in addition at knockout tower (28), the return-air outlet of knockout tower (28) is connected to the suction port of return-air compressor (26), the outlet of return-air compressor (26) is connected to the return-air input aperture of synthesis reactor (23) by muffler (24), after unreacted synthetic gas is separated in knockout tower (28), turns back in the synthesis reactor (23) by return-air compressor (26), muffler (24) and to carry out circulating reaction; Top in synthesis reactor (23) also is connected to the combustion zone of plasma gasification Reaktionsofen (10) bottom or the work gas interface of plasma burner (44) by muffler (21), with the work gas of unreacted synthetic gas, can also send the carbonic acid gas of system's end back to Reaktionsofen and carry out circular treatment as plasma burner.
Also have water pump (53) in the described system, the suction port of water pump (53) extend in the garbage percolation water (52) by water absorption tube (54), and the water outlet of water pump (53) is by the water jet of pipe connection to plasma gasification Reaktionsofen (10) internal upper part.Garbage percolation water is sprayed in the gasification reacting furnace (10), make the garbage percolation water vapor with the high temperature in the stove, the water vapor of vaporization uses as vaporized chemical, has promptly handled garbage percolation water, makes again and has obtained vaporized chemical in the stove.
Also has hydrogen manufacturing workshop (46) in the described system, device for producing hydrogen (49), hydrogen container (47) are arranged in the hydrogen manufacturing workshop (46), hydrogen container (47) is connected to the work gas interface of plasma burner (44) by hydrogen feeding pipe (48), or is connected to the hydrogenation mixing tank of fly-ash separator (20) back level.The hydrogen of hydrogen manufacturing Workshop Production offers the working gas of plasma burner (44), be transported to the hydrogenation mixing tank of fly-ash separator (20) back level simultaneously, hydrogen is joined in the hydrogen-rich synthetic gas, make synthesis reactor (23) obtain best unstripped gas prescription, with hydrogenation method raw material being adjusted to optimum formula can reducing emission of carbon dioxide; Hydrogen feedstock water or coal when water is hydrogen feedstock, can adopt conventional electric current to come water electrolysis hydrogen production, also can adopt advanced plasma technique to come hydrogen manufacturing.The Technology of coal hydrogen manufacturing is quite ripe, and its shortcoming is to consume coal resource in short supply.When the device systems scale hour, the hydrogen manufacturing workshop can be set, and the outsourcing hydrogen product is used.
Also have turbine driven set (16) in the described system, the vapour outlet of the vapour outlet of waste heat boiler (15) and synthesis reactor (23) is connected to steam distributor (14) by steam-pipe respectively, is connected to turbine driven set (16) by steam distributor (14) again.Utilize the waste heat of gasification reacting furnace and the heat energy power-generating that synthesis reactor shifts out, plenum system and plasma burner use, to reduce production costs.
Also have magnetic separator (58) in the described system, magnetic separator (58) is installed in the top of conveying belt (57).Magnetic separator sorts out the ferromagnetic metal in the raw material, recycles.
The technological process of production of device systems of the present utility model is: rubbish, biomass are grasped with grab bucket (1) knock down crusher (6), rubbish after fragmentation, biomass enter winnowing machine (7), inorganics is separated, organic solid waste that selection by winnowing is come out and biomass enter into hopper (8) as raw material, enter in the plasma gasification Reaktionsofen (10) by feeding screw (9); Solid-state raw material is reverse and descend with hot gas flow in gasification reacting furnace (10), through oven dry, pyrolysis, and generation gas (vapour) attitude thing and solid-state charcoal, the composition of gas (vapour) attitude thing has flue gas, water vapor, carbon monoxide, hydrogen, C
nH
mWith steam state tar, gas (vapour) attitude thing up moves, top outlet by stove is forced to send into the air compartment of plasma gasification Reaktionsofen (10) bottom by flue gas recirculation pipe (11) by flue gas recirculation blower fan (43), enters combustion zone and red-hot coke again and carries out gasification reaction; Solid-state charcoal in the stove down moves, and enters into the combustion zone, with plasma burner solid-state charcoal is carried out just generating carbon monoxide or methane after red-hot, red-hot charcoal touches vaporized chemical, finishes burning until the carbon residue reaction, and lime-ash falls into slag bath; By circulation, make the flue gas, water vapor and the charcoal gasification that generate in the stove generate carbon monoxide and hydrogen, make the methane, the C that generate in the stove simultaneously
nH
m, tar with water vapor coexistence under reform, generate carbon monoxide and hydrogen.The product that produces in plasma gasification Reaktionsofen (10) is to be the hydrogen-rich synthetic gas of main component with carbon monoxide, hydrogen, hydrogen-rich synthetic gas is drawn in the position, middle and lower part of Reaktionsofen (10), after the cooling of waste heat boiler (15) exchange heat energy, enter into absorption reactor thermally (18), carrying out hydrogen-rich synthetic gas after dechlorination/desulfurization is handled with absorption agent enters fly-ash separator (20) and removes remaining dust, the solid absorbent that dedusting is got off carries out recycle by revert pipe (19) Returning reactor (18), and the absorption agent of loss replenishes by absorption agent feed bin (17); Hydrogen-rich synthetic gas after the dedusting enters in the synthesis reactor (23) by compressor (22) as unstripped gas, unstripped gas is the katalysis by dual-function catalyst (catalst for synthesis of methanol and methanol dehydration catalyst) under the temperature of the pressure of 2～5Mpa and 230～270 ℃, finish synthetic and two reaction process of methanol dehydration of methyl alcohol simultaneously, a dimethyl ether synthesis; From the product of synthesis reactor (23) outlet output is methyl alcohol, dme, water, the mixture of synthetic gas, mixture separates through knockout tower (28), product dimethyl ether, unreacted methanol, unreacted synthetic gas, water is drawn from corresponding outlet respectively, wherein unreacted methanol is returned synthesis reactor (23) and is carried out circulating reaction by returning liquid compressor (27) and liquid returning tube (25), unreacted synthetic gas returns synthesis reactor (23) by same air compressor (26) and muffler (24) and carries out circulating reaction, the compressed machine of product dimethyl ether (29) compress and water cooler (30) cooling after send into basin (31) and store; The temperature of the hydrogen-rich synthetic gas of extracting out from plasma gasification Reaktionsofen (10) up to 1000 ℃ about, produce superheated vapour by waste heat boiler (15), a large amount of reaction heat in the synthesis reactor (23) shift out production steam by heat exchanger, the steam that produces in superheated vapour that waste heat boiler (15) produces and the synthesis reactor (23) is transported to turbine driven set (16) by steam distributor (14) and generates electricity, generate electricity and can offer the miscellaneous equipment electricity consumption that plasma burner (44) used and provided native system.
In the above-mentioned technological process of production: use the plasma body combustion technology, under not having the situation of oxygen supply, realizes air-isolation the combustion reactions in the gasification reacting furnace (10), the temperature of combustion zone is more than 1000 ℃, the pyrolysis zone temperature is 500～800 ℃, by flue gas recirculation, carcinogenic violent in toxicity Dioxins is thoroughly disintegrated; The hydrogen-rich synthetic gas of drawing in the plasma gasification Reaktionsofen (10) is reduced to the temperature of hydrogen-rich synthetic gas below 200 ℃ fast by waste heat boiler (15) heat-shift, regenerates Dioxins with the chloride thing that prevents synthetic gas; Carrying out dechlorination/desulfurization at absorption reactor thermally (18), to handle employed lime (CaO) absorption agent be the powder of 100～500um; Send into that the volume ratio of carbon monoxide and hydrogen is 1: 2 (CO/2H in the unstripped gas that carries out building-up reactions in the synthesis reactor (23)
2), can regulate by the hydrogenation measure, the chemical formula that carries out building-up reactions in synthesis reactor (23) is 4H
2+ 2CO=(CH
3)
2O+H
2O+200.2kj/mol produces reaction heat simultaneously; The working gas of plasma burner (44) derives from the hydrogen of device for producing hydrogen, or introduce the working gas of unreacted return-air as plasma burner (44) from the outlet of return-air compressor (26), this measure can also make the carbonic acid gas of the Dioxins of slipping through the net and system's end return in the plasma gasification Reaktionsofen (10) to carry out circular treatment, make system not have pollutent to discharge; The whole service system is isolated from the outside, and the opening for feed of gasification reacting furnace (10) is isolated by raw material in the feeding screw (9) and outside air, and slag-drip opening is isolated from the outside with water seal; Fly-ash separator (20) is sack cleaner or electrostatic precipitator.
When the biomass with agricultural wastes, forestry waste, wood working waste, waterplant and so on are raw material production dme liquefied gas, the technological process of production of device systems is: send into hopper (8) after biomass are shredded by stock cutter (65), enter in the plasma gasification Reaktionsofen (10) by feeding screw (9); Solid-state raw material is reverse and descend with hot gas flow in gasification reacting furnace (10), through oven dry, pyrolysis, and generation gas (vapour) attitude thing and solid-state charcoal, the composition of gas (vapour) attitude thing has flue gas, water vapor, carbon monoxide, hydrogen, C
nH
mWith steam state tar, gas (vapour) attitude thing up moves, top outlet by stove is forced to send into the air compartment of plasma gasification Reaktionsofen (10) bottom by flue gas recirculation pipe (11) by flue gas recirculation blower fan (43), enters combustion zone and red-hot coke again and carries out gasification reaction; Solid-state charcoal in the stove down moves, and enters into the combustion zone, with plasma burner solid-state charcoal is carried out just generating carbon monoxide or methane after red-hot, red-hot charcoal touches vaporized chemical, finishes burning until the carbon residue reaction, and lime-ash falls into slag bath; By circulation, make the flue gas, water vapor and the charcoal gasification that generate in the stove generate carbon monoxide and hydrogen, make the methane, the C that generate in the stove simultaneously
nH
m, tar with water vapor coexistence under reform, generate carbon monoxide and hydrogen.The product that produces in plasma gasification Reaktionsofen (10) is to be the hydrogen-rich synthetic gas of main component with carbon monoxide, hydrogen, hydrogen-rich synthetic gas is drawn in the position, middle and lower part of Reaktionsofen (10), after the cooling of waste heat boiler (15) exchange heat energy, enter into fly-ash separator (20) and remove remaining dust; Enter synthesis reactor (23) as unstripped gas by compressor (22) then, hydrogen-rich synthetic gas under the temperature of the pressure of 2～5Mpa and 230～270 ℃ by the katalysis of dual-function catalyst (catalst for synthesis of methanol and methanol dehydration catalyst) finish simultaneously methyl alcohol synthetic with two reaction process of methanol dehydration, a dimethyl ether synthesis; From the product of synthesis reactor (23) outlet output is methyl alcohol, dme, water, the mixture of synthetic gas, mixture separates through knockout tower (28), product dimethyl ether, unreacted methanol, unreacted synthetic gas, water is drawn from corresponding outlet respectively, the wherein last methyl alcohol that reacts returns synthesis reactor (23) by time liquid compressor (27) and liquid returning tube (25) and carries out circulating reaction, unreacted synthetic gas returns synthesis reactor (23) by return-air compressor (26) and same tracheae (24) and carries out circulating reaction, the compressed machine of product dimethyl ether (29) compress and water cooler (30) cooling after send into basin (31) and store.
Equipment in the said system, the nucleus equipment that rubbish is converted into hydrogen-rich synthetic gas is plasma gasification Reaktionsofen (10), can adopt me to make in 200720174504.0 " a kind of is rubbish, Wood Adhesives from Biomass the equipment for gasification of high heating value synthetic gas " utility model technical project of application on August 24th, 2007; The nucleus equipment of producing dme is synthesis reactor (23), can adopt me to make in 200710085393.0 " electrocatalysis synthesis reactor " invention technical project of application on March 2nd, 2007, also can select for use known mature technology to manufacture and design; Miscellaneous equipment all adopts known mature technology manufacturing.
The technological process of production of the present utility model can realize automatic red-tape operati by collective and distributive type control system, collective and distributive type control system is that core is carried out system's centralized supervisory control management by principal computer, and rubbish is weighed by special purpose computer, the discharging vehicle scheduling, the operation of crane grapple, broken charging, the operation control of gasification reacting furnace, absorb dedusting, building-up reactions, separate cooling, the operation of subsidiary engine device control, the generating electricity consumption, decentralised control is carried out in ganging of products can etc., automatic control system is by monitoring the operation of each equipment, with each operation centralization, automatization, optimization.
The beneficial effects of the utility model are: with rubbish, biomass is the secondary clean energy of raw material production high heating value, turns waste into wealth, and has not only eliminated the pollution of rubbish, reduces discharging CO
2, environmental protection and ecological effect are outstanding, and can alleviate the energy-intensive situation.The utility model is compared with waste incineration and generating electricity, has following advantage: do not have carcinogenic violent in toxicity Dioxins discharging, and also lack the reliable NO of technology at present in the waste incineration and generating electricity field
xTerminal cleaning process technology with Dioxins etc.; Rubbish is converted into secondary clean energy is major objective, real innoxious, minimizing, the resource utilization that realizes refuse treatment, and waste incineration and generating electricity has only reclaimed waste gas of incineration, and the resource utilization level of application is lower, moreover waste incineration and generating electricity easily causes secondary pollution; The device systems scale is changeable, production line all can be built in small towns, county, city, cities and towns and city above the provincial level, and there is not the market problem in product, thereby be easy to popularize, and waste incineration and generating electricity can only be in economically developed big city, and the waste resources amount of small and medium-sized cities is not suitable for building refuse-burning plant.
Description of drawings
The utility model provides following accompanying drawing to be further described, but each accompanying drawing and following embodiment all do not constitute restriction of the present utility model:
Fig. 1 is to be the device systems synoptic diagram of raw material production dme liquefied gas with rubbish, biomass.
Fig. 2 is to be the device systems synoptic diagram of raw material production dme liquefied gas with biomass.
Fig. 3 is to be the skeleton diagram of the collective and distributive type control system of raw material production dme liquefied gas with rubbish, biomass.
Among the figure: 1. grab bucket, 2. loop wheel machine driving, 3. vacuum fan/or air purifier, 4. overhead crane control chamber form, 5. powerful blower fan, 6. crusher, 7. winnowing machine, 8. hopper, 9. feeding screw, 10. plasma gasification Reaktionsofen, 11. flue gas recirculation pipes, 12. catalysis deodorization devices, 12b. heat exchanger, 13. plasma body working powers, 14. steam distributors, 15. waste heat boiler, 16. turbine driven set, 17. absorption agent feed bins, 18. absorption reactor thermally, 19. absorption agent revert pipes, 20. fly-ash separators, 21. muffler, 22. feed gas compressors, 23. synthesis reactor, 24. muffler, 25. liquid returning tubes, 26. return-air compressors, 27. return the liquid compressor, 28. knockout towers, 29. compressors, 30. water cooler, 31. dme basins, 32. groove tank cars, 33. water coolant, 34. materials warehouses, 35. maintenance of the equipment centers, 36. the fire fighting monitoring center, 37. red-tape operati centers, high voltage power distribution chambers 38., 39. the low-voltage distribution chamber, 40. induced draft fans, 41. storage pits, 42. conveying belt, 43. flue gas recirculation blower fans, 44. plasma burners, 45. clinker pusher, 46. hydrogen manufacturing workshops, 47. hydrogen containers, 48. hydrogen feeding pipe, 49. device for producing hydrogen, 50. inorganicss storage hole, 51. scrap metal storage hole, 52. garbage percolation water, 53. water pump, 54. water absorption tubes, 55. refuse pits, 56. garbage percolation is water pipe under water, 57. the band transfer roller, 58. magnetic separators, 59. dumpers, 60. air curtain, 61. the rubbish discharging platform, 62. dumper watch-keeping cubicle forms, 63. vacuum fans/or air purifier, 64. scraper conveyor, 65. stock cutter, 66. pallet conveyers, 67. stock yards.
Embodiment
Among the embodiment shown in Figure 1, use rubbish, biomass be the raw material production dme device systems mainly by the grab bucket (1), loop wheel machine driving (2), crusher (6), winnowing machine (7), magnetic separator (58), hopper (8), feeding screw (9), plasma gasification Reaktionsofen (10), plasma burner (44), catalysis deodorization device (12), flue gas recirculation blower fan (43), water pump (53), waste heat boiler (15), induced draft fan (40), absorption agent feed bin (17), absorption reactor thermally (18), fly-ash separator (20), compressor (22), synthesis reactor (23), knockout tower (28), return liquid compressor (27), return-air compressor (26), compressor (29), water cooler (30), dme basin (31), hydrogen manufacturing workshop (46), steam distributor (14), turbine driven set (16), plasma body working power (13) is formed, wherein: the discharge port of crusher (6) is connected winnowing machine (7), and powerful blower fan (5) is installed on the winnowing machine (7); Hopper (8) is arranged on the feeding screw (9), and the organic matter rubbish outlet of winnowing machine (7) is over against hopper (8), and the discharge port of feeding screw (9) puts in the abdomen of plasma gasification Reaktionsofen (10); The exhanst gas outlet on plasma gasification Reaktionsofen (10) top is connected to the air suction inlet of flue gas recirculation blower fan (43) by flue gas recirculation pipe (11), catalysis deodorization device (12) is serially connected on the flue gas recirculation pipe (11), and the air outlet of flue gas recirculation blower fan (43) is connected to the air compartment of plasma gasification Reaktionsofen (10) bottom; Plasma burner (44) is installed in the side, combustion chamber of gasification reacting furnace (10) bottom, and the power output end of plasma body working power (13) is connected to the power input interface of plasma burner (44) by supply lead; The synthetic gas output interface of plasma gasification Reaktionsofen (10) is connected to waste heat boiler (15), and waste heat boiler (15) is by the air suction inlet of pipe connection to induced draft fan (40); The air outlet of induced draft fan (40) arrives absorption reactor thermally (18) by pipe connection, absorption agent feed bin (17) is connected on the inlet duct of absorption reactor thermally (18), the outlet of absorption reactor thermally (18) is connected to the import of fly-ash separator (20), and the outlet of fly-ash separator (20) is connected to the suction port of feed gas compressor (22); The outlet of feed gas compressor (22) is connected to the unstripped gas inlet of synthesis reactor (23), the product outlet of synthesis reactor (23) is connected to the product inlet of knockout tower (28), the methyl alcohol of knockout tower (28) returns the suction port that the liquid outlet is connected to go back to liquid compressor (27), and the outlet of returning liquid compressor (27) is connected to time liquid input interface of synthesis reactor (23) by liquid returning tube (25); The return-air outlet of knockout tower (28) is connected to return-air compressor (26), and return-air compressor (26) is connected to the return-air input aperture of synthesis reactor (23) by muffler (24); The product outlet of knockout tower (28) is connected to the suction port of compressor (29), and the outlet of compressor (29) is connected to the product inlet of water cooler (30), and the product outlet of water cooler (30) is connected to dme basin (31); The branching of pipes interface is connected to the work gas interface of plasma burner (44) by muffler (21) between return-air compressor (26) and synthesis reactor (23).In the present embodiment, gasification reacting furnace (10) is designed to the bed furnace of blast furnace formula, is the empty stomach cylindrical structure, and it is dolioform that the bottom is; Plasma burner (44) is many combinations, is installed in the side of gasification reacting furnace (10) combustion zone, bottom, and burner noz(zle) points to the axle center; The suction port of water pump (53) extend in the garbage percolation water (52) by water absorption tube (54), the water outlet of water pump (53) is by the water jet of pipe connection to plasma gasification Reaktionsofen (10) internal upper part, garbage percolation water is sprayed in the gasification reacting furnace (10), make the garbage percolation water vapor with the high temperature in the stove, the water vapor of vaporization uses as vaporized chemical, promptly handled garbage percolation water, made again and obtained vaporized chemical in the stove; Device for producing hydrogen (49), hydrogen container (47) are arranged in the hydrogen manufacturing workshop (46), and hydrogen container (47) is connected to the work gas interface of plasma burner (44) by hydrogen feeding pipe (48), or is connected to the hydrogenation mixing tank of fly-ash separator (20) back level; The vapour outlet of the vapour outlet of waste heat boiler (15) and synthesis reactor (23) is connected to steam distributor (14) by steam-pipe respectively, be connected to turbine driven set (16) by steam distributor (14) again, utilize the waste heat of gasification reacting furnace and the heat energy power-generating that synthesis reactor shifts out, plenum system and plasma burner use, to reduce production costs; Magnetic separator (58) is installed in the top of conveying belt (57), and magnetic separator sorts out the ferromagnetic metal in the raw material, recycles.In this enforcement: the rubbish that dumper (59) is transported is discharged in the refuse pit (55) by discharging platform (61), (1) grasps rubbish from refuse pit (55), biomass are knocked down crusher (6) with grabbing bucket, rubbish after fragmentation, biomass enter winnowing machine (7), inorganics is separated, the organic solid waste that selection by winnowing is come out, biomass enter into hopper (8) as raw material, enter in the plasma gasification Reaktionsofen (10) by feeding screw (9); Use the plasma body combustion technology, do not make in plasma gasification Reaktionsofen (10) stove under air-isolation has the situation of oxygen supply and realize combustion reactions, the temperature of combustion zone is more than 1000 ℃, the pyrolysis zone temperature is 500～800 ℃, utilize in the stove high temperature raw material dry, pyrolysis, produce gas (vapour) attitude thing and solid-state charcoal, the composition of gas (vapour) attitude thing has flue gas, water vapor, carbon monoxide, hydrogen, C
nH
mWith steam state tar, gas (vapour) attitude thing up moves, forced to send into the air compartment of plasma gasification Reaktionsofen (10) bottom by flue gas recirculation blower fan (43) by flue gas recirculation pipe (11) by the top outlet of stove, enter combustion zone and red-hot coke again and carry out gasification reaction, by flue gas recirculation, carcinogenic violent in toxicity Dioxins is thoroughly disintegrated more than 1000 ℃ in the hot environment in the combustion zone simultaneously; Solid-state charcoal in the stove down moves, and enters into the combustion zone, with plasma burner (44) solid-state charcoal is carried out just generating carbon monoxide or methane after red-hot, red-hot charcoal touches vaporized chemical, finishes burning until the carbon residue reaction, and lime-ash falls into slag bath; By circulation, make the flue gas, water vapor and the charcoal gasification that generate in the stove generate carbon monoxide and hydrogen, make the methane, the C that generate in the stove simultaneously
nH
m, tar with water vapor coexistence under reform, generate carbon monoxide and hydrogen.The product that produces in plasma gasification Reaktionsofen (10) is to be the hydrogen-rich synthetic gas of main component with carbon monoxide, hydrogen, and hydrogen-rich synthetic gas is drawn from the position, middle and lower part of Reaktionsofen (10); The hydrogen-rich synthetic gas of drawing is reduced to the temperature of hydrogen-rich synthetic gas below 200 ℃ fast by waste heat boiler (15) heat-shift, regenerates Dioxins with the chloride thing that prevents synthetic gas; Hydrogen-rich synthetic gas enters into absorption reactor thermally (18) after lowering the temperature through waste heat boiler (15), carries out dechlorination/desulfurization with absorption agent and handles, and employed lime (CaO) absorption agent is the powder of 100～500um; Enter fly-ash separator (20) through the hydrogen-rich synthetic gas after dechlorination/desulfurization processing and remove dust, the absorption agent that dedusting is got off carries out recycle by revert pipe (19) Returning reactor (18), and the absorption agent of loss replenishes by absorption agent feed bin (17); Hydrogen-rich synthetic gas after the dedusting enters synthesis reactor (23) as unstripped gas by compressor (22), sends into that the volume ratio of carbon monoxide and hydrogen is 1: 2 (CO/2H in the unstripped gas that carries out building-up reactions in the synthesis reactor (23)
2), can regulate by the hydrogenation measure; Send into the katalysis under the temperature of the pressure of 2～5Mpa and 230～270 ℃ of hydrogen-rich synthetic gas in the synthesis reactor (23) by dual-function catalyst (catalst for synthesis of methanol and methanol dehydration catalyst), finish synthetic and two reaction process of methanol dehydration of methyl alcohol simultaneously, a dimethyl ether synthesis, catalyzer is selected CuO/ZnO/Al for use
2O
3And modified ZSM-5 catalyst; From the product of synthesis reactor (23) outlet output is methyl alcohol, dme, water, the mixture of synthetic gas, mixture separates through knockout tower (28), product dimethyl ether, unreacted methanol, unreacted synthetic gas, water is drawn from corresponding outlet respectively, wherein unreacted methanol is returned synthesis reactor (23) and is carried out circulating reaction by returning liquid compressor (27) and liquid returning tube (25), the synthetic gas of end reaction returns synthesis reactor (23) by return-air compressor (26) and muffler (24) and carries out circulating reaction, and the compressed machine of product dimethyl ether (29) compresses and water cooler (30) is sent into basin (31) storage after cooling off.In the present embodiment, the working gas of part plasma burner (44) derives from the hydrogen of device for producing hydrogen, the working gas of another part plasma burner (44) derives from the unreacted synthetic gas of introducing from the outlet of return-air compressor (26), this measure can also make the carbonic acid gas of the Dioxins of slipping through the net and system's end return in the plasma gasification Reaktionsofen (10) to carry out circular treatment, make system not have pollutent to discharge.In the present embodiment, with air curtain (60) air and the external world of rubbish discharging platform (61) are isolated, the overhead mephitic air of the space mephitic air of rubbish discharging platform (61) and refuse pit (55) is sent into catalysis deodorization device (12) by vacuum fan (3), (63), the heat energy that utilizes high-temperature flue gas enters atmosphere again after destroying foul odors under the effect of catalyzer; Fly-ash separator (20) is a sack cleaner.
Among the embodiment shown in Figure 2, be with agricultural wastes, forestry waste, the wood working waste, the biomass of waterplant and so on are the device systems of raw material production dme, mainly by pallet conveyer (66), stock cutter (65), scraper conveyor (64), hopper (8), feeding screw (9), plasma gasification Reaktionsofen (10), plasma burner (44), heat exchanger (12b), flue gas recirculation blower fan (43), clinker pusher (45), waste heat boiler (15), induced draft fan (40), fly-ash separator (20), feed gas compressor (22), synthesis reactor (23), knockout tower (28), return liquid compressor (27), return-air compressor (26), compressor (29), water cooler (30), dme basin (31), hydrogen manufacturing workshop (46), steam distributor (14), turbine driven set (16), plasma body working power (13) is formed, wherein: hopper (8) is arranged on the feeding screw (9), and the discharge port of feeding screw (9) puts in the abdomen of plasma gasification Reaktionsofen (10); The exhanst gas outlet on plasma gasification Reaktionsofen (10) top is connected to the air suction inlet of flue gas recirculation blower fan (43) by flue gas recirculation pipe (11), heat exchanger (12b) is serially connected in flue gas recirculation pipe (11), and the air outlet of flue gas recirculation blower fan (43) is connected to the air compartment of plasma gasification Reaktionsofen (10) bottom; Plasma burner (44) is installed in the side, combustion chamber of gasification reacting furnace (10) bottom, and the power output end of plasma body working power (13) is connected to the power input interface of plasma burner (44) by supply lead; The synthetic gas output interface of plasma gasification Reaktionsofen (10) is connected to waste heat boiler (15), and waste heat boiler (15) is by the air suction inlet of pipe connection to induced draft fan (40); The air outlet of induced draft fan (40) is by the import of pipe connection to fly-ash separator (20), and the outlet of fly-ash separator (20) is connected to the suction port of feed gas compressor (22); The outlet of feed gas compressor (22) is connected to the unstripped gas inlet of synthesis reactor (23), the product outlet of synthesis reactor (23) is connected to the product inlet of knockout tower (28), the methyl alcohol of knockout tower (28) returns the suction port that the liquid outlet is connected to go back to liquid compressor (27), and the outlet of returning liquid compressor (27) is connected to time liquid input interface of synthesis reactor (23) by liquid returning tube (25); The return-air outlet of knockout tower (28) is connected to the suction port of return-air compressor (26), and the outlet of return-air compressor (26) is connected to the return-air input aperture of synthesis reactor (23) by muffler (24); The product outlet of knockout tower (28) is connected to the suction port of compressor (29), and the outlet of compressor (29) is connected to the product inlet of water cooler (30), and the product outlet of water cooler (30) is connected to dme basin (31); The branching of pipes interface is connected to the work gas interface of plasma burner (44) by muffler (21) between return-air compressor (26) and synthesis reactor (23).In the present embodiment, gasification reacting furnace (10) is designed to the bed furnace of blast furnace formula, and for to the abdomen cylindrical structure, it is dolioform that the bottom is; Plasma burner (44) is many combinations, is installed in the side of gasification reacting furnace (10) combustion zone, bottom, and burner noz(zle) points to the axle center; Device for producing hydrogen (49), hydrogen container (47) are arranged in the hydrogen manufacturing workshop (46), and hydrogen container (47) is connected to the work gas interface of plasma burner (44) by hydrogen feeding pipe (48), or is connected to the hydrogenation mixing tank of fly-ash separator (20) back level; The vapour outlet of the vapour outlet of waste heat boiler (15) and synthesis reactor (23) is connected to steam distributor (14) by steam-pipe respectively, be connected to turbine driven set (16) by steam distributor (14) again, utilize the waste heat of gasification reacting furnace and the heat energy power-generating that synthesis reactor shifts out, plenum system and plasma burner use, to reduce production costs.In this enforcement: served pallet conveyer (66) from the biomass that stock yard (67) comes, enter stock cutter (65) by spout, the biomass material that is cut into particle enters into hopper (8) by scraper conveyor (64), enters in the plasma gasification Reaktionsofen (10) by feeding screw (9); Use the plasma body combustion technology, do not make in plasma gasification Reaktionsofen (10) stove under air-isolation has the situation of oxygen supply and realize combustion reactions, the temperature of combustion zone is more than 1000 ℃, the pyrolysis zone temperature is 500～800 ℃, utilize in the stove high temperature raw material dry, pyrolysis, produce gas (vapour) attitude thing and solid-state charcoal, the composition of gas (vapour) attitude thing has flue gas, water vapor, carbon monoxide, hydrogen, C
nH
mWith steam state tar, gas (vapour) attitude thing up moves, top outlet by stove is forced to send into the air compartment of plasma gasification Reaktionsofen (10) bottom by flue gas recirculation pipe (11) by flue gas recirculation blower fan (43), enters combustion zone and red-hot coke again and carries out gasification reaction; Solid-state charcoal in the stove down moves, and enters into the combustion zone, with plasma burner (44) solid-state charcoal is carried out just generating carbon monoxide or methane after red-hot, red-hot charcoal touches vaporized chemical, finishes burning until the carbon residue reaction, and lime-ash falls into slag bath; By circulation, make the flue gas, water vapor and the charcoal gasification that generate in the stove generate carbon monoxide and hydrogen, make the methane, the C that generate in the stove simultaneously
nH
m, tar with water vapor coexistence under reform, generate carbon monoxide and hydrogen.The product that produces in plasma gasification Reaktionsofen (10) is to be the hydrogen-rich synthetic gas of main component with carbon monoxide, hydrogen, and hydrogen-rich synthetic gas is drawn from the position, middle and lower part of Reaktionsofen (10); The hydrogen-rich synthetic gas of drawing is by waste heat boiler (15) heat-shift; Enter into fly-ash separator (20) after hydrogen-rich synthetic gas is lowered the temperature through waste heat boiler (15) and remove remaining dust; Hydrogen-rich synthetic gas after the dedusting enters synthesis reactor (23) as unstripped gas by compressor (22), sends into that the volume ratio of carbon monoxide and hydrogen is 1: 2 (CO/2H in the unstripped gas in the synthesis reactor (23)
2), can regulate by the hydrogenation measure; Unstripped gas in the synthesis reactor (23) is the katalysis by dual-function catalyst (catalst for synthesis of methanol and methanol dehydration catalyst) under the temperature of the pressure of 2～5Mpa and 230～270 ℃, finish synthetic and two reaction process of methanol dehydration of methyl alcohol simultaneously, a dimethyl ether synthesis, catalyzer is selected CuO/ZnO/Al for use
2O
3And modified ZSM-5 catalyst; From the product of synthesis reactor (23) outlet output is methyl alcohol, dme, water, the mixture of synthetic gas, mixture separates through knockout tower (28), product dimethyl ether, unreacted methanol, unreacted synthetic gas, water is drawn from corresponding outlet respectively, wherein unreacted methanol is returned synthesis reactor (23) and is carried out circulating reaction by returning liquid compressor (27) and liquid returning tube (25), unreacted synthetic gas returns synthesis reactor (23) by return-air compressor (26) and muffler (24) and carries out circulating reaction, the compressed machine of product dimethyl ether (29) compress and water cooler (30) cooling after send into basin (31) and store.In the present embodiment, the working gas of wherein a part of plasma burner (44) derives from the hydrogen of device for producing hydrogen, the working gas of another part plasma burner (44) derives from from the outlet of return-air compressor (26) and introduces unreacted synthetic gas, this measure can also make the residual carbon dioxide of system's end return in the plasma gasification Reaktionsofen (10) to carry out circular treatment, makes system not have pollutent to discharge; Fly-ash separator (20) is a sack cleaner.
In the above-mentioned two routine embodiments, after means of detection, sensing device, monitoring device, executive device are installed on the relevant device, all can realize full-automatic red-tape operati, with each operation centralization, automatization, optimization.
Claims (10)
1. use rubbish for one kind, biomass material is produced the device systems of dme, comprise rubbish, the pyrolytic gasification equipment of biomass, it is characterized in that device systems is mainly by feeding screw (9), plasma gasification Reaktionsofen (10), plasma burner (44), plasma body working power (13), waste heat boiler (15), induced draft fan (40), fly-ash separator (20), feed gas compressor (22), synthesis reactor (23), knockout tower (28), return liquid compressor (27), compressor (29), water cooler (30) and dme basin (31) are formed, wherein: hopper (8) is arranged on the feeding screw (9), and the discharge port of feeding screw (9) puts in the abdomen of plasma gasification Reaktionsofen (10); Plasma burner (44) is installed in the lower combustion chamber side of gasification reacting furnace (10), and the power output end of plasma body working power (13) is connected to the power input interface of plasma burner (44) by supply lead; The synthetic gas output interface of plasma gasification Reaktionsofen (10) is connected to waste heat boiler (15), and waste heat boiler (15) is by the air suction inlet of pipe connection to induced draft fan (40); The air outlet of induced draft fan (40) is by the import of pipe connection to fly-ash separator (20), and the outlet of fly-ash separator (20) is connected to the suction port of feed gas compressor (22); The outlet of feed gas compressor (22) is connected to the unstripped gas inlet of synthesis reactor (23), the product outlet of synthesis reactor (23) is connected to the product inlet of knockout tower (28), the methyl alcohol of knockout tower (28) returns the suction port that the liquid outlet is connected to go back to liquid compressor (27), and the outlet of returning liquid compressor (27) is connected to time liquid input interface of synthesis reactor (23) by liquid returning tube (25); The product outlet of knockout tower (28) is connected to the suction port of compressor (29), and the outlet of compressor (29) is connected to the product input aperture of water cooler (30), and the product outlet of water cooler (30) is connected to dme basin (31).
2. a kind of device systems with rubbish, biomass material production dme according to claim 1 is characterized in that described plasma burner (44) is more than one, at least one.
3. a kind of device systems with rubbish, biomass material production dme according to claim 1 is characterized in that the exhanst gas outlet on plasma gasification Reaktionsofen (10) top is connected to the air compartment of plasma gasification Reaktionsofen (10) bottom by flue gas recirculation pipe (11).
4. a kind of device systems of producing dme with rubbish, biomass material according to claim 1, the exhanst gas outlet that it is characterized in that plasma gasification Reaktionsofen (10) top is connected to the air suction inlet of flue gas recirculation blower fan (43) by flue gas recirculation pipe (11), and the air outlet of flue gas recirculation blower fan (43) is connected to the air compartment of plasma gasification Reaktionsofen (10) bottom.
5. a kind of device systems of producing dme with rubbish, biomass material according to claim 1, it is characterized in that the exhanst gas outlet on plasma gasification Reaktionsofen (10) top is connected to the air suction inlet of flue gas recirculation blower fan (43) by flue gas recirculation pipe (11), the air outlet of flue gas recirculation blower fan (43) is connected to the air compartment of plasma gasification Reaktionsofen (10) bottom, and catalysis deodorization device (12) or heat exchanger (12b) also are installed on the pipeline of flue gas recirculation pipe (11).
6. a kind of device systems of producing dme with rubbish, biomass material according to claim 1, return-air exports to it is characterized in that going up in addition by knockout tower (28), the return-air outlet of knockout tower (28) is connected to return-air compressor (26), and return-air compressor (26) is connected to the return-air input aperture of synthesis reactor (23) by muffler (24).
7. a kind of device systems with rubbish, biomass material production dme according to claim 1 is characterized in that also being connected to the combustion zone of plasma gasification Reaktionsofen (10) bottom or the work gas interface of plasma burner (44) by muffler (21) on the top of synthesis reactor (23).
8. a kind of device systems of producing dme with rubbish, biomass material according to claim 1, it is characterized in that also having water pump (53) in the system, the suction port of water pump (53) extend in the garbage percolation water (52) by water absorption tube (54), and the water outlet of water pump (53) is by the water jet of pipe connection to plasma gasification Reaktionsofen (10) internal upper part.
9. a kind of device systems of producing dme with rubbish, biomass material according to claim 1, it is characterized in that also having hydrogen manufacturing workshop (46) in the system, device for producing hydrogen (49), hydrogen container (47) are arranged in the hydrogen manufacturing workshop (46), hydrogen container (47) is connected to the work gas interface of plasma burner (44) by hydrogen feeding pipe (48), or is connected to the hydrogenation mixing tank of fly-ash separator (20) back level.
10. use rubbish for one kind, biomass material is produced the device systems of dme, it is characterized in that device systems is mainly by crusher (6), winnowing machine (7), feeding screw (9), plasma gasification Reaktionsofen (10), plasma burner (44), plasma body working power (13), waste heat boiler (15), induced draft fan (40), absorption reactor thermally (18), fly-ash separator (20), feed gas compressor (22), synthesis reactor (23), knockout tower (28), return liquid compressor (27), compressor (29), water cooler (30) and dme basin (31) are formed, wherein: the discharge port of crusher (6) is connected winnowing machine (7), the organic matter rubbish outlet of winnowing machine (7) faces the hopper (8) on the feeding screw (9), and the discharge port of feeding screw (9) puts in the abdomen of plasma gasification Reaktionsofen (10); Plasma burner (44) is installed in the side, combustion chamber of gasification reacting furnace (10) bottom, and the power output end of plasma body working power (13) is connected to the power input interface of plasma burner (44) by supply lead; The synthetic gas output interface of plasma gasification Reaktionsofen (10) is connected to waste heat boiler (15), and waste heat boiler (15) is by the air suction inlet of pipe connection to induced draft fan (40); The air outlet of induced draft fan (40) is by the inlet of pipe connection to absorption reactor thermally (18), and the outlet of absorption reactor thermally (18) is connected to the import of fly-ash separator (20), and the outlet of fly-ash separator (20) is connected to the suction port of feed gas compressor (22); The outlet of feed gas compressor (22) is connected to the unstripped gas inlet of synthesis reactor (23), the product outlet of synthesis reactor (23) is connected to the product inlet of knockout tower (28), the methyl alcohol of knockout tower (28) returns the suction port that the liquid outlet is connected to go back to liquid compressor (27), and the outlet of returning liquid compressor (27) is connected to time liquid input interface of synthesis reactor (23) by liquid returning tube (25); The product outlet of knockout tower (28) is connected to the suction port of compressor (29), and the outlet of compressor (29) is connected to the product inlet of water cooler (30), and the product outlet of water cooler (30) is connected to dme basin (31).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNU2007201833234U CN201109766Y (en) | 2007-09-22 | 2007-09-22 | Equipment system for producing dimethyl ether by garbage and biomass raw material |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNU2007201833234U CN201109766Y (en) | 2007-09-22 | 2007-09-22 | Equipment system for producing dimethyl ether by garbage and biomass raw material |
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| CN201109766Y true CN201109766Y (en) | 2008-09-03 |
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| CNU2007201833234U Expired - Fee Related CN201109766Y (en) | 2007-09-22 | 2007-09-22 | Equipment system for producing dimethyl ether by garbage and biomass raw material |
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101823073A (en) * | 2010-03-13 | 2010-09-08 | 周开根 | Gasification-liquefaction disposal method, system and equipment for household garbage |
| CN103402643A (en) * | 2011-03-01 | 2013-11-20 | 克莱索佩亚有限责任公司 | Mill for grinding rubbish |
| CN104456576A (en) * | 2014-12-08 | 2015-03-25 | 王威平 | Melting incineration system and incineration process thereof |
| CN106269815A (en) * | 2016-10-27 | 2017-01-04 | 威德环境科技股份有限公司 | Changing food waste pretreatment system |
| CN112441890A (en) * | 2020-11-25 | 2021-03-05 | 武汉理工大学 | Method and system for preparing dimethyl ether by garbage gasification |
| CN117563509A (en) * | 2023-11-20 | 2024-02-20 | 广州汇锦能效科技有限公司 | System for preparing dimethyl ether by coupling oxygen-enriched incineration power generation with carbon dioxide hydrogenation |
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2007
- 2007-09-22 CN CNU2007201833234U patent/CN201109766Y/en not_active Expired - Fee Related
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101823073A (en) * | 2010-03-13 | 2010-09-08 | 周开根 | Gasification-liquefaction disposal method, system and equipment for household garbage |
| CN101823073B (en) * | 2010-03-13 | 2012-01-04 | 周开根 | Gasification-liquefaction disposal method, system and equipment for household garbage |
| CN103402643A (en) * | 2011-03-01 | 2013-11-20 | 克莱索佩亚有限责任公司 | Mill for grinding rubbish |
| US9327286B2 (en) | 2011-03-01 | 2016-05-03 | Chrysopoeia Srl | Mill for grinding rubbish |
| CN103402643B (en) * | 2011-03-01 | 2016-06-29 | 克莱索佩亚有限责任公司 | For grinding the grinding machine of rubbish |
| CN104456576A (en) * | 2014-12-08 | 2015-03-25 | 王威平 | Melting incineration system and incineration process thereof |
| CN106269815A (en) * | 2016-10-27 | 2017-01-04 | 威德环境科技股份有限公司 | Changing food waste pretreatment system |
| CN112441890A (en) * | 2020-11-25 | 2021-03-05 | 武汉理工大学 | Method and system for preparing dimethyl ether by garbage gasification |
| CN117563509A (en) * | 2023-11-20 | 2024-02-20 | 广州汇锦能效科技有限公司 | System for preparing dimethyl ether by coupling oxygen-enriched incineration power generation with carbon dioxide hydrogenation |
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