CN101823073A

CN101823073A - Gasification-liquefaction disposal method, system and equipment for household garbage

Info

Publication number: CN101823073A
Application number: CN201010173404A
Authority: CN
Inventors: 周开根
Original assignee: Individual
Current assignee: QUZHOU CITY GUANGYUAN HOUSEHOLD GARBAGE TECHNOLOGY INSTITUTE
Priority date: 2010-03-13
Filing date: 2010-04-28
Publication date: 2010-09-08
Anticipated expiration: 2030-04-28
Also published as: CN101823073B

Abstract

The invention discloses a gasification-liquefaction disposal method, a system and equipment for household garbage, which relates to an organic waste disposal method and equipment for household garbage. The method of the invention comprises the following steps: pretreating household garbage, and delivering the pretreated household garbage into a plasma gasification furnace for gasification to generate hydrogen rich synthetic gas; then cooling, deacidifying and dedusting the hydrogen rich synthetic gas to separate CO2; then producing methanol in a methanol synthesis reactor; returning the separated CO2 to a gasification system to carry out carbonation reaction with calcium oxide to release heat for providing auxiliary heat energy for gasification, and simultaneously avoiding discharge of greenhouse gases to the environment; and returning tail gas to the plasma gasification furnace for remelting treatment, thus forming a closed-loop circulation production system. Disposal of the household garbage with zero discharge and no pollution is realized, the dioxin pollution problem is avoided, and the household garbage is converted to chemical raw materials and fuel needed by people. The invention is suitable for harmless and recycling disposal of the household garbage, industrial high polymer wastes, wastes produced by utilizing a composting method and waste in a garbage sorting site.

Description

The method of domestic garbage gasification-liquefaction disposal, system and equipment

Technical field

The present invention relates to the solid waste disposal technology, particularly relate to method and equipment that a kind of house refuse and debirs are disposed.

Background technology

House refuse and debirs are along with the continuous expansion of the development of Chinese national economy and city size and increase sharply, cause rubbish to overflow, current, the garbage-surrounded city phenomenon has all appearred in many cities of China, has had influence on the sustainable development of Chinese national economy and the development in restriction city.House refuse and debirs contain many harmful components, as handle badly, will pollute the environment, and threaten people health.At present, handle house refuse and mainly contain refuse classification comprehensive utilization, Sanitary Landfill Technology, compost (biochemistry) technology and incineration technology, wherein, refuse classification needs public participation and cooperation, China does not also carry out at present, if can reach separate waste collection, comprehensive utilization, still 40～50% amount needs burning disposal or landfill disposal in addition; China adopts sanitary landfill method to handle domestic waste in most of area, and this not only need take a large amount of land resource, and discharges a large amount of greenhouse gases, contaminated land and underground water, destroys existent environment of people; Adopt composting process only to utilize organic matter about 40%, remaining 60% also need make burning disposal or landfill disposal, has secondary pollution problem equally; Adopt burning method to handle house refuse, be to have accomplished minimizing, recycling treatment house refuse to the eye, but be actually the mode of ground solid contaminant with flue gas shifted in the atmosphere, these transfer to pollutant in the atmosphere along with cross-ventilation, terrestrial gravitation are got back on the ground, the life and health that influence is human, some pollutant is got back on the ground in the mode of making acid rain, and the carbon dioxide of discharging then plays the living environment that greenhouse effects destroy people.Burning method also generates the problem of carcinogenic violent in toxicity-bioxin contaminated environment, harm person health easily, though incineration plant has flue gas purification system, also lacks effective reliable terminal cleaning process technology at present and eliminate bioxin in the waste incineration field.

Bioxin is that a kind of chloride strong toxic organic is learned material, this class material is highly stable, water insoluble, it is the liposoluble substance of colorless and odorless, so be very easy to accumulation in vivo, the molecular structure influence of natural microorganism and hydrolysis Dui bioxin is less, and therefore, the De bioxin is difficult to the natural degradation elimination in the environment.Its toxicity is more than 1000 times of potassium cyanide, and the title of " poison in century " is arranged, and is classified as human one-level carcinogenic substance by IARC.House refuse, industrial debirs and medical waste all can produce bioxin in burning process, rubbish following approach: a. that is formed with of bioxin in burning process forms bioxin by chloride predecessors such as plastic containing chlorine, chloride pesticide/herbicide/timber preservative/bleaching agent/food, Polychlorinated biphenyls by molecular rearrangement, free radical condensation, dechlorination or other molecular reaction in combustion process; B. when burning when insufficient, chloride rubbish imperfect combustion produces the too much material that do not burn in the flue gas, meets heavy metal such as the material of strong catalytic such as copper chloride, iron chloride, nickel oxide, aluminium oxide and He Cheng bioxin; C. it is not destroyed in burning itself to contain the De bioxin in the fuel, is present in the gas fume after burning; D. carbon residue, oxygen, hydrogen, chlorine etc. are at flying dust surface catalysis synthetic mesophase product Huo bioxin in the solid flying dust, or the predecessor in the gas phase generates bioxin at the flying dust surface catalysis; E. flue gas from high temperature drop to low temperature between 250～500 ℃ the time decomposed bioxin can synthesize again; F. other unknown cause generates bioxin.Generally contain chlorine source, organic matter and heavy metal in the house refuse, therefore, in flue gas, flying dust and slag that incinerator produces, often contain bioxin.There are some researches show that the concentration of predecessor concentration, chlorine, temperature, oxygen content, sulfur content and heavy metal have material impact as the existence of unconscious catalyst to the generation and the discharging of De bioxin in the incineration process of domestic garbage.In the waste incineration process there be the measure of control bioxin: 1. before rubbish enters incinerator, take the refuse classification technology, sort out metals such as iron in the rubbish, copper, nickel, cut off the catalytic media in the waste incineration process, reduce the amount of chlorinated organics, reduce the source that waste incineration generates bioxin from the source; 2. at the control of burning condition, keep the rubbish combustion around more than 850 ℃, gas residence time was greater than 2 seconds, the peroxide amount is controlled at below 8%, realizes " 3T+E " the work principle, promptly, 1T-ignition temperature (Temperature), the 2T-time of staying (Time), 3T-turbulence level (Turbulence), E-peroxide control (Excess); 3. add to suppress bioxin and generate agent, in stove, add sulfur-containing compound and suppress the formation of bioxin; 4. quenching, the flue gas that will draw in the incinerator is plummeted to below 250 ℃ by 450 ℃ with interior at 3s, to reduce the time of staying of flue gas in regenerating 250 ℃ of-400 ℃ of peak district temperature ranges of bioxin; 5. deacidification fully uses absorbent to slough De bioxin predecessor in the flue gas; 6. avoid dust, dust is the carrier of catalyst, makes flue-gas temperature reach 450 ℃ of a large amount of before dust in flue gas content that reduce by rational boiler design; 7. avoid the outer low temperature of stove synthetic again, adopt the mode of half dry type aeration tower and sack cleaner collocation, the EGT of control appliance inlet is not less than 232 ℃ simultaneously.More than these measures, can only be the formation that relatively reduces bioxin, waste incineration still can produce the bioxin contaminated environment inevitably: one of reason is that its burning of burning method processing house refuse must just can make abundant burning above under 6% the condition in the peroxide amount, otherwise it will be more serious polluting, and peroxide is one of condition that forms bioxin, the concentration of peroxide environment Zhong bioxin increases greatly, and the concentration of anaerobic environment Zhong bioxin can descend, and does not have oxygen then not have bioxin synthetic; Former two is that the flue gas that burns must be to contact with metal heated of equipment such as superheater, boiler, heat exchanger, air preheater therefore, and these metal heated faces all can become the catalytic media that forms bioxin; Former three is be difficult to realize deacidification fully therefore, still has a certain amount of bioxin predecessor in the flue gas; Former four is that ubiquity has carbon residue, oxygen, hydrogen, chlorine and flying dust in the flue gas of waste incineration therefore, inevitably can close into bioxin again by low temperature outside stove; More than four cause descriptions in the flue gas of burning away the refuse, must have a certain amount of bioxin, it is unapproachable from flue gas bioxin being eliminated, it will be along with the discharging of flue gas contaminated environment.Because bioxin is difficult to degraded, its half-life can reach 273 years, substantially be considered as not degrading, its accumulation in people's living environment and in the human body can get more and more, serious bioxin pollution problem has all appearred in the big state of many burnings, it also is not very serious that the present De bioxin of China pollutes total amount, but the generation of China's solid waste and clinical waste and treating capacity are all in continuous increase in recent years, concentrated burning facility is set up or established in various places one after another, growth momentum is swift and violent, serious De bioxin pollution problem may be brought, enough attention should be caused.

In a word, it is not a good way that burning method is disposed house refuse, there is land occupation again in sanitary landfills, discharges greenhouse gases and pollution hidden trouble, refuse classification, composting process also will be in the face of not utilizing the problem of outlet of part, and headachy " garbage-surrounded city " problem must solve, therefore, the human urgent perfect technical scheme of disposing house refuse of wishing to have.

Summary of the invention

The objective of the invention is to overcome and solve destruction existent environment of people that landfill method, burning method bring with the bioxin pollution problem; a kind of technology that house refuse, debirs are disposed by gasification-liquefaction is proposed; the pollutant that effectively suppresses to be included forms; in whole disposal process, do not discharge pollutants and greenhouse gases; eliminate the bioxin pollution problem; preserve the ecological environment, simultaneously house refuse, debirs are converted into a kind of industrial chemicals or clean energy resource.

The method of a kind of domestic garbage gasification-liquefaction disposal of the present invention, comprise calcium oxide cooperation plasma gasification technology, it is characterized in that house refuse or debirs are dewatered and sorting through preliminary treatment, reduce moisture and inorganic content, to reduce the useless composition of feed stock for blast furnace, improve calorific value, thereby can reduce the quality of the power consumption and the raising synthesis gas of plasma gasification stove, pass through CO then ₂The sealing gland feed arrangement is sent into the plasma gasification stove, and the carbon dioxide sealing gland is air-isolation effectively, stops air synthesis gas in charging aperture enters gasification furnace and prevention stove to release outside the stove by charging aperture, and can obstruction not arranged to charging; Set gradually oven dry section, pyrolysis section and gasification section by upper, middle and lower in the plasma gasification stove, when being the liquid slag discharge to ash melting, the slag district also is set between gasification section and slag notch, the operating temperature of oven dry section is controlled between 120～300 ℃, the operating temperature of pyrolysis section is controlled between 300～1000 ℃, the operating temperature of gasification section is controlled between 1000～1300 ℃, the operating temperature in slag district is controlled between 1300～1600 ℃, the operating pressure in the gasification furnace is controlled at-30Pa～+ 5kPa between; Rubbish or debirs are dried in stove, after the pyrolysis, become the rubbish charcoal and enter gasification section, carry out gasification reaction with the water vapour analyte that sprays into gasification section from plasma torch, generate with CO and H ₂Hydrogen-rich synthetic gas for main component; In gasification section and slag district plasma torch is set, with the working gas of water vapour as gasifying agent and plasma torch, water vapour is heated to more than 4200 ℃ by plasma torch, and hydrone is all decomposed, and generates H ^*, H ₂ ^*, HO ^*, O ^*, O ₂ ^*And H ₂O ^*After, be sprayed directly on on the rubbish charcoal of gasification section, the rubbish charcoal as inhaling hydrogen and oxygen uptake element, is generated CO and H ₂, fusion is a liquid slag in the environment that lime-ash is 1300～1600 ℃ in the in-furnace slag district, enters slag bath by water seal; Adopt calcium oxide cooperation plasma gasification mode, at gasification system the carbonation reaction chamber is set, heat release when generating calcium carbonate with the calcium oxide absorbing carbon dioxide to provide auxiliary thermal source for gasification, to reduce the energy consumption of plasma torch, calcium oxide is double as dechlorination/desulfurizing agent also, the pyrolysis gas that pyrolysis section in the plasma gasification stove is produced is incorporated into the carbonation reaction chamber, in the environment that excessive calcium oxide exists, slough the bioxin predecessor, chloride and sulfide, again pyrolysis gas as carrier gas, take calcium oxide, calcium carbonate mixture and heat enter the oven dry section in the plasma gasification stove, for the oven dry and the preheating of newly going into the stove rubbish material provides heat energy, then pyrolysis gas is introduced gas-solid separator, calcium oxide and calcium carbonate are separated, again the pyrolysis pneumatic transmission is gone in the gasification section of plasma gasification stove, in 1000～1300 ℃ environment, make the methane in the pyrolysis gas, gaseous state tar, ethene, ethane, things such as water vapour carry out cracking and chemical reaction, thoroughly disintegrate simultaneously bioxin, pass through cycle gasification, make into stove rubbish and decomposed fully, generating high-quality is the hydrogen-rich synthetic gas of main component with hydrogen and carbon monoxide; Hydrogen-rich synthetic gas is drawn in the plasma gasification stove, after the waste heat boiler cooling, in the gas purifying equipment of forming by absorption reactor thermally, cyclone dust collectors and sack cleaner, carry out depickling and dedusting again, then at CO ₂The carbon dioxide that absorbs in the synthesis gas with solution of potassium carbonate in the absorption tower generates saleratus, the synthesis gas of sloughing carbon dioxide is sent into methanol synthesis reactor produce methyl alcohol, saleratus is sent into regeneration reactor, by heating saleratus is decomposed into solution of potassium carbonate and carbon dioxide, the solution of potassium carbonate that decomposites is sent back to CO ₂The absorption tower is carried out recycling, and the carbon dioxide that decomposites is sent into the carbonation reaction chamber of gasification system, carries out carbonation reaction with calcium oxide, for refuse gasification helps heat, avoids emission greenhouse gas simultaneously; Hydrogen-rich synthetic gas in methanol synthesis reactor by catalysis synthesizing methanol product, miscible with limewash in the blended absorbent device of cleaning equipment endways methanol product again, the remaining pollutant that comprises bioxin, carbon dioxide are absorbed by limewash, separate by destilling tower then, methyl alcohol is separated, unreacting gas is sent back to methanol synthesis reactor carry out circular response, limewash is sent back to the blended absorbent device by circulating pump after by scrubbing carry out recycling; Tail gas is returned the plasma gasification stove melt down processing, form a closed cycle production system.The draining that oozes that produces in the house refuse preprocessing process is sent into digester and is produced biogas by anaerobic fermentation, biogas is sent into the plasma gasification stove carry out resolution process, the natural pond slag as fertilizer.The inorganic matter that sub-elects in the preprocessing process is sorted again, reclaim old metal, after more nonmetal inorganic matter being passed through to pulverize, mix, be used for producing non-burning brick with the isolated calcium carbonate of gasification system, calcium oxide.The plasma gasification fire grate is gone into the slag of water seal slag bath, becomes the vitreum particle, can directly do the building materials utilization, the flying dust of collecting from sack cleaner, handles by melting furnace, and slag can directly be done the building materials utilization.

In the said method, the calcium oxide consumption that is input to the carbonation reaction chamber is determined by 1.2～1.5 times that react indoor carbon dioxide, chloride, sulfide and fluoride molal quantity total amount, wherein, detection level during the molal quantity of carbon dioxide is vented one's spleen by actual input quantity heating determines that the molal quantity of chloride, sulfide and fluoride is determined by the elementary analysis of sampling rubbish debirs.

In the said method, carry out house refuse with the water-vapor plasma gasification mode and dispose, to gasification furnace input oxygen or air, house refuse does not gasify in anaerobic environment, and it is synthetic effectively to suppress bioxin; Can effectively remove bioxin predecessor, chlorinated organics and desulfurization at the indoor direct thermotropism of the carbonation reaction mixed oxidization calcium powder of venting one's spleen, and be solidificated in the absorbent, reduce the probability that bioxin forms; In the plasma gasification stove, the circular flow of pyrolysis gas, even there is chlorinated organics, bioxin predecessor to exist, form bioxin by molecular rearrangement, free radical condensation, dechlorination or other molecular reaction at pyrolysis section, the ， bioxin can thoroughly be disintegrated when pyrolysis gas is recycled in 1000～1300 ℃ of environment of gasification section; In the plasma gasification stove, rubbish material earlier by pyrolysis, behind the effusion volatile matter, carry out gasification reaction with the water vapour active matter and the fixed carbon of plasma more than 4200 ℃ then, in 1000～1600 ℃ of environment of gasification section, fixed carbon will be gasified totally, and easily generate the situation of bioxin when not existing burning insufficient; The peroxide rate is zero in the synthesis gas of plasma gasification stove production, and synthesis gas is drawn the back from the gasification furnace of high temperature can effectively reduce the synthetic again probability of bioxin temperature-fall period; Adopt the production technology of closed circulation, even the You bioxin forms in the system, can not be discharged yet, by terminal purification run, absorb and tail gas is sent back to the plasma gasification stove with limewash and melt down to handle and eliminate bioxin and pollute, by cycling, progressively absorb remaining pollutant, not clear organic gas is further decomposed and is gasified in the tail gas, nitrogen in the tail gas consumes by producing synthetic ammonia, thereby realization zero-emission, pollution-free disposal house refuse and organic waste, the while is converted into house refuse and debirs human needs's methanol product.

The system of a kind of domestic garbage gasification-liquefaction disposal of the present invention comprises plasma gasification equipment, by pre-processing device, CO ₂Sealing gland feed arrangement (13), plasma gasification stove (23), plasma torch (24), gas-solid separator (17), circulating fan (18), heat exchanger (20), carbonation reaction chamber (2007), waste heat boiler (27), absorption reactor thermally (32), cyclone dust collectors (31), sack cleaner (38), CO ₂Absorption tower (42), regenerator (46), methanol synthesis reactor (52), blended absorbent device (55), destilling tower (62), dirt separator (58), circulating pump (60), methyl alcohol basin (65) and connecting pipe are formed, and wherein: pre-processing device comprises refuse pit (2) and separator (3); The interior space of plasma gasification stove (23) is divided into oven dry section, pyrolysis section and gasification section, on the oven dry section rubbish material import, the import of heat-carrying gas and pyrolysis gas outlet are arranged, heat-carrying gas output interface is arranged on the pyrolysis section, pyrolysis gas input interface is arranged on the gasification section, and the binding site of pyrolysis section and gasification section has the synthesis gas output interface; Plasma torch (24) is arranged on the gasification zone, bottom of plasma gasification stove (23); Heat exchanger (20) is made of sub-air chamber, heat-exchanging chamber and collection chamber, and pyrolysis gas input interface is arranged in the sub-air chamber, and heat-carrying gas output interface is arranged on the heat-exchanging chamber, and pyrolysis gas output interface is arranged on the collection chamber; Heat-exchanging chamber in carbonation reaction chamber (2007) and the heat exchanger (20) directly communicates, and heat-carrying gas input interface, calcium oxide input unit and carbon dioxide input interface are arranged on carbonation reaction chamber (2007); CO ₂Synthesis gas input interface, synthesis gas input interface, KHCO are arranged on the absorption tower (42) ₃Output interface and K ₂CO ₃The solution input interface, regenerator has KHCO on (46) ₃Input interface, CO ₂Output interface and K ₂CO ₃The solution output interface;

Weighing by loop wheel machine grab bucket (1) between refuse pit (2) and the separator (3) connects, and separator (3) is received the CO of plasma gasification equipment by band conveyor or feeding screw weighing apparatus ₂The charging aperture of sealing gland feed arrangement (13), CO ₂The discharging opening of sealing gland feed arrangement (13) is connected to the rubbish material import of plasma gasification stove (23), the heat-carrying gas output interface of plasma gasification stove (23) is connected to the heat-carrying gas input interface of carbonation reaction chamber (2007), and the heat-carrying gas output interface of heat exchanger (20) is connected to the heat-carrying gas import of plasma gasification stove (23); The pyrolysis gas outlet of plasma gasification stove (23) is connected to the mixture intake of gas-solid separator (17), the gaseous state thing of gas-solid separator (17) exports the pyrolysis gas input interface that is connected to heat exchanger (20) by circulating fan (18), and the pyrolysis gas output interface of heat exchanger (20) is connected to the pyrolysis gas input interface of plasma gasification stove (23); The synthesis gas output interface of plasma gasification stove (23) is connected to the synthesis gas input interface of waste heat boiler (27), the synthesis gas output interface of waste heat boiler (27) is connected to the synthesis gas input interface of absorption reactor thermally (32), the synthesis gas output interface of absorption reactor thermally (32) is connected to the mixture input interface of cyclone dust collectors (31), the solid of cyclone dust collectors (31) exports on the connecting pipe of the synthesis gas input interface that is connected to absorption reactor thermally (32), the gaseous state thing outlet of cyclone dust collectors (31) is connected to the synthesis gas input interface of sack cleaner (38), and the synthesis gas output interface of sack cleaner (38) is connected to CO ₂The synthesis gas input interface on absorption tower (42), CO ₂The KHCO on absorption tower (42) ₃Output interface is connected to the KHCO of regenerator (46) ₃Input interface, the CO of regenerator (46) ₂Output interface is connected to the carbon dioxide input interface of carbonation reaction chamber (2007), the K of regenerator (46) ₂CO ₃The solution output interface is connected to CO ₂The K on absorption tower (42) ₂CO ₃The solution input interface; CO ₂The synthesis gas output interface on absorption tower (42) is connected to the air entry of compressor (51), the exhaust outlet of compressor (51) is connected to the raw material gas inlet of methanol synthesis reactor (52), the methyl alcohol gas outlet of methanol synthesis reactor (52) is connected to the methyl alcohol gas import of blended absorbent device (55), the mixture outlet of blended absorbent device (55) is connected to the mixture input interface of destilling tower (62), the unreacting gas of destilling tower (62) exports the return-air interface that is connected to methanol synthesis reactor (52) by unreacting gas pipeline (61) and compressor b (56), and the methanol product outlet of destilling tower (62) is connected to methyl alcohol basin (65); The limewash outlet of destilling tower (62) is connected to the input interface of dirt separator (58), and the limewash outlet of dirt separator (58) is connected to the water sucking mouth of circulating pump (60), and the delivery port of circulating pump (60) is connected to the limewash import of blended absorbent device (55).

In the above-mentioned system, pre-processing device also comprises spiral water squeezing/feed appliance (10) and digester (9), and spiral water squeezing/feed appliance (10) is arranged on separator (3) and CO ₂Between the sealing gland feed arrangement (13), the outlet of the rubbish material of separator (3) is received the hopper of spiral water squeezing/feed appliance (10) by ribbon conveyer (8) weighing apparatus, and spiral water squeezing/feed appliance (10) discharging opening is connected to CO by carrier pipe (12) ₂The charging aperture of sealing gland feed arrangement (13), CO ₂The discharging opening of sealing gland feed arrangement (13) is connected to the charging aperture of plasma gasification stove (23) by carrier pipe (14); The draining interface that oozes of refuse pit (2), separator (3) and spiral water squeezing/feed appliance (10) is connected to the charging aperture of digester (9) by carrier pipe, and the methane outlet of digester (9) is connected to the gasification zone of plasma gasification stove (23) by carrier pipe.

In the above-mentioned system, at sack cleaner (38) and CO ₂Air-introduced machine (40) and carbon monodixe conversion reactor (41) also are set between the absorption tower (42), the synthesis gas output interface of sack cleaner (38) is connected to the inlet scoop of air-introduced machine (40), the air outlet of air-introduced machine (40) is connected to the synthesis gas input interface of carbon monodixe conversion reactor (41), and the synthesis gas output interface of carbon monodixe conversion reactor (41) is connected to CO ₂The synthesis gas input interface on absorption tower (42); At CO ₂Compressor a (44) and synthesis gas basin (48) also are set, CO between absorption tower (42) and the compressor (51) ₂The synthesis gas output interface on solution absorption tower (42) is connected to the air entry of compressor a (44), the exhaust outlet of compressor a (44) is connected to the input interface of synthesis gas basin (48), and the output interface of synthesis gas basin (48) is connected to the air entry of compressor (51).

In the above-mentioned system, in the unreacting gas pipeline (61) of system for methanol synthesis end, tail gas interface and synthetic ammonia installation are set, tail gas feedback pipe (30) is set between plasma gasification stove (23) and terminal cleaning equipment simultaneously, tail gas interface in the unreacting gas pipeline (61) is connected respectively to the tail gas feedback pipe (30) of plasma gasification stove (23) and the charging interface of synthetic ammonia installation by control valve, and the tail gas outlet of synthetic ammonia installation is connected to the tail gas feedback pipe (30) of plasma gasification stove (23).

The system of another kind of domestic garbage gasification-liquefaction disposal of the present invention comprises plasma gasification equipment, by pre-processing device, CO ₂Sealing gland feed arrangement (13), gas ions gasification furnace (23), plasma torch (24), circulating fan (18) and heat exchanger b (21), waste heat boiler (27), absorption reactor thermally (32), cyclone dust collectors (31), sack cleaner (38), hydrogenation blender (49), methanol synthesis reactor (52), blended absorbent device (55), destilling tower (62), dirt separator (58), circulating pump (60), methyl alcohol basin (65) and connecting pipe are formed, and wherein: pre-processing device comprises refuse pit (2) and separator (3); The interior space of plasma gasification stove (23) is divided into oven dry section, pyrolysis section and gasification section, on the oven dry section rubbish material import and pyrolysis gas outlet is arranged, and pyrolysis gas input interface is arranged on the gasification section, and the binding site of pyrolysis section and gasification section has the synthesis gas output interface; Plasma torch (24) is arranged on the gasification section of plasma gasification stove (23) bottom; Heat exchanger b (21) is made of sub-air chamber, heat-exchanging chamber and collection chamber, and pyrolysis gas input interface is arranged in the sub-air chamber, and synthesis gas input interface and synthesis gas output interface are arranged on the heat-exchanging chamber, and pyrolysis gas output interface is arranged on the collection chamber; Weighing by loop wheel machine grab bucket (1) between refuse pit (2) and the separator (3) connects, and separator (3) is received the CO of plasma gasification equipment by band conveyor or feeding screw weighing apparatus ₂The charging aperture of sealing gland feed arrangement (13), CO ₂The discharging opening of sealing gland feed arrangement (13) is connected to the charging aperture of plasma gasification stove (23), the pyrolysis gas outlet of plasma gasification stove (23) is connected to the pyrolysis gas input interface of heat exchanger b (21) by circulating fan (18), and the pyrolysis gas output interface of heat exchanger b (21) is connected to the pyrolysis gas input interface of plasma gasification stove (23) gasification section; The synthesis gas output interface of plasma gasification stove (23) is connected to the synthesis gas input interface of heat exchanger b (21), the synthesis gas output interface of heat exchanger b (21) is connected to the synthesis gas input interface of waste heat boiler (27), the synthesis gas output interface of waste heat boiler (27) is connected to the synthesis gas input interface of absorption reactor thermally (32), the synthesis gas output interface of absorption reactor thermally (32) is connected to the mixture input interface of cyclone dust collectors (31), and the solid of cyclone dust collectors (31) exports on the connecting pipe of the synthesis gas input interface that is connected to absorption reactor thermally (32); The gaseous state thing outlet of cyclone dust collectors (31) is connected to the synthesis gas input interface of sack cleaner (38), the synthesis gas output interface of sack cleaner (38) is connected to the air entry of compressor a (44), the exhaust outlet of compressor a (44) is connected to the input interface of synthesis gas basin (48), the output interface of synthesis gas basin (48) is connected to the synthesis gas input interface of hydrogenation blender (49), the synthesis gas output interface of hydrogenation blender (49) is connected to the air entry of compressor (51), the exhaust outlet of compressor (51) is connected to the raw material gas inlet of methanol synthesis reactor (52), the methyl alcohol gas outlet of methanol synthesis reactor (52) is connected to the methyl alcohol gas import of blended absorbent device (55), the mixture outlet of blended absorbent device (55) is connected to the mixture input interface of destilling tower (62), the unreacting gas of destilling tower (62) exports the return-air interface that is connected to methanol synthesis reactor (52) by unreacting gas pipeline (61) and compressor b (56), and the methanol product outlet of destilling tower (62) is connected to methyl alcohol basin (65); The limewash outlet of destilling tower (62) is connected to the input interface of dirt separator (58), and the limewash outlet of dirt separator (58) is connected to the water sucking mouth of circulating pump (60), and the delivery port of circulating pump (60) is connected to the limewash import of blended absorbent device (55).In the native system, pre-processing device also comprises spiral water squeezing/feed appliance (10) and digester (9), and spiral water squeezing/feed appliance (10) is arranged on separator (3) and CO ₂Between the sealing gland feed arrangement (13), the outlet of the rubbish material of separator (3) is received the hopper of spiral water squeezing/feed appliance (10) by ribbon conveyer (8) weighing apparatus, and spiral water squeezing/feed appliance (10) discharging opening is connected to CO by carrier pipe (12) ₂The charging aperture of sealing gland feed arrangement (13), CO ₂The discharging opening of sealing gland feed arrangement (13) is connected to the charging aperture of plasma gasification stove (23) by carrier pipe (14); The garbage percolation water interface of refuse pit (2), separator (3) and spiral water squeezing/feed appliance (10) is connected to the charging aperture of digester (9) by carrier pipe, and the methane outlet of digester (9) is connected to the gasification section of plasma gasification stove (23) by carrier pipe.Native system also has air-introduced machine (40) between waste heat boiler (27) and absorption reactor thermally (32), the syngas outlet of waste heat boiler (27) is connected to the air inlet of air-introduced machine (40), and the air outlet of air-introduced machine (40) is connected to the synthesis gas input interface of absorption reactor thermally (32); In the unreacting gas pipeline (61) of system for methanol synthesis end, tail gas interface and synthetic ammonia installation are set, tail gas feedback pipe (30) is set between the equipment of plasma gasification stove (23) and system for methanol synthesis end simultaneously, tail gas interface in the unreacting gas pipeline (61) is connected respectively to the tail gas feedback pipe (30) of plasma gasification stove (23) and the charging interface of synthetic ammonia installation by control valve, and the tail gas outlet of synthetic ammonia installation is connected to the tail gas feedback pipe (30) of plasma gasification stove (23).

Equipment in the said system, waste heat boiler (27), absorption reactor thermally (32), cyclone dust collectors (31), sack cleaner (38), CO ₂Absorption tower (42), regenerator (46), methyl alcohol basin (65), destilling tower (62) and dirt separator (58) adopt the routine techniques manufacturing, and methanol synthesis reactor (52) adopts the known technology manufacturing or adopts the electrocatalysis synthesis reactor technology of Chinese patent ZL 200710166618.5 to make.

Equipment in a kind of domestic garbage gasification of the present invention-liquefaction disposal system, it is characterized in that equipment for gasification is by plasma gasification stove (23), plasma torch (24), circulating fan (18), heat exchanger b (21) and connecting pipe are formed, wherein: oven dry section (23-I) is arranged in the plasma gasification stove (23) from top to bottom successively, pyrolysis section (23-II) and gasification section (23-III), oven dry section (23-I), directly communicate between pyrolysis section (23-II) and the gasification section (23-III), plasma torch (24) is arranged on the furnace wall of gasification section (23-III), there are rubbish material import (2302) access and pyrolysis gas outlet (2303) to pick out on the top of oven dry section (23-I), there is pyrolysis gas input interface (2309) to insert in gasification section (23-III), slag notch (2307) is arranged at the bottom of gasification section (23-III), has synthesis gas output interface (2304) to pick out at the binding site of pyrolysis section (23-II) and gasification section (23-III); Heat exchanger b (21) is by sub-air chamber (2102), heat-exchanging chamber (2104), heat-exchange tube bundle (2105) and collection chamber (2107) constitute, sub-air chamber (2102), heat-exchanging chamber (2104), collection chamber (2107) is presented, in, following layout, heat-exchanging chamber (2104) is in the centre, sub-air chamber (2102), heat-exchanging chamber (2104) and collection chamber (2107) are in box hat, the outer wall of box hat is installed insulation material, isolate by upper spacer between sub-air chamber (2102) and the heat-exchanging chamber (2104), isolate by lower clapboard between heat-exchanging chamber (2104) and the collection chamber (2107), heat-exchange tube bundle (2105) is arranged on heat-exchanging chamber (2104) and two ends are through to sub-air chamber (2102) and collection chamber (2107), sub-air chamber (2102), heat-exchange tube bundle (2105) and collection chamber (2107) constitute the return passage of pyrolysis gas, there is pyrolysis gas input interface (2101) to insert in sub-air chamber (2102), there are synthesis gas input interface (2108) access and synthesis gas output interface (2103) to pick out at heat-exchanging chamber (2104), have pyrolysis gas output interface (2109) to pick out at collection chamber (2107); The pyrolysis gas outlet (2303) of plasma gasification stove (23) oven dry section is connected to the air inlet of circulating fan (18), the air outlet of circulating fan (18) is connected to the pyrolysis gas input interface (2101) of heat exchanger b (21) sub-air chamber, and the pyrolysis gas output interface (2109) of heat exchanger b (21) collection chamber is connected to the pyrolysis gas input interface (2309) of plasma gasification stove (23) gasification section; The synthesis gas output interface (2304) of plasma gasification stove (23) is connected to the synthesis gas input interface (2108) of heat exchanger b (21) heat-exchanging chamber, and the synthesis gas output interface (2103) of heat exchanger b (21) heat-exchanging chamber is connected to follow-up equipment; The flying dust that the ash hole (2110) of heat exchanger b (21) is connected to plasma gasification stove (23) melts down interface (2306).In this equipment, the gasification section (23-III) in plasma gasification stove (23) also has flying dust to melt down interface (2306), biogas input interface (2308) and tail gas input interface (2305) access; Heat-exchanging chamber (2104) in heat exchanger b (21) blows ash mouthful (2106) access in addition and ash hole (2110) picks out, the flying dust that the ash hole (2110) of heat exchanger b (21) is connected to plasma gasification stove (23) melts down interface (2306), blowing on the ash mouthful (2106) of heat exchanger b (21) is connected with the soot-blowing wind machine, the air inlet of soot-blowing wind machine is connected on the synthesis gas conveyance conduit, and the air outlet of soot-blowing wind machine is connected to blowing of heat exchanger b (21) grey mouthful (2106).

The invention has the beneficial effects as follows: house refuse or debirs are disposed by gasification-liquefaction, realize zero-emission, can avoid the bioxin pollution problem, do not discharge pollutants in the whole disposal process, the methanol product of being produced can be made industrial chemicals or industrial fuel, and the economic benefit of obtaining is much higher than burning electricity generation.The present invention compares with burning facility: burning method has a large amount of carbon dioxides and other pollutant emission, and contaminated environment is made greenhouse effects and acid rain, and the present invention does not discharge flue gas, does not pollute the environment; Burning method can form the violent in toxicity bioxin inevitably, and is difficult to eliminate, and enters atmosphere with flue gas, the health of harm humans, and the present invention can suppress to form bioxin, even there is minute quantity De bioxin to occur, also removes in the cleaning equipment endways easily.The present invention compares with landfill method: the present invention does not have contamination-free and greenhouse gas emission; Landfill method to underground, discharges a large amount of greenhouse gases to pollution transportation, and contaminated soil and underground water jeopardize the healthy of the mankind, also has influence people's of future generation future trouble; The present invention is used as a kind of resource to junk and utilizes, and produces clean energy resource, alleviates energy pressure, produces economic benefit simultaneously, does not need government to bear disposal cost after the commercialization; And landfill method is not only wasted resource, and the expense of landfill yard then is bottomless pit, and is very big to the financial burden of government; Project land occupation of the present invention is few, and landfill method need be with a large amount of soils.The present invention is fit to the innoxious and disposal of resources of domestic waste, life in the countryside rubbish, medical waste, industrial high molecular waste material, agriculture and forestry organic waste material, composting process residue, garbage sorting field waste.

Description of drawings

Fig. 1 is the technological process block-diagram of a kind of domestic garbage gasification-liquefaction disposal of the present invention;

Fig. 2 is the general system diagram of the domestic garbage gasification-liquefaction disposal of a kind of calcium oxide cooperation of the present invention;

Fig. 3 is the general system diagram of the domestic garbage gasification-liquefaction disposal of a kind of hydrogenation method of the present invention;

Fig. 4 is the detail drawing in I district among the detail drawing in I district among Fig. 2 or Fig. 3;

Fig. 5 is the detail drawing in II-a district among Fig. 2;

Fig. 6 is the detail drawing in III-a district among Fig. 2;

Fig. 7 is the detail drawing in IV district among the detail drawing in IV district among Fig. 2 or Fig. 3.

Fig. 8 is the detail drawing in II-b district among Fig. 3, also is the equipment for gasification structure chart in a kind of house refuse disposal system of the present invention;

Fig. 9 is the detail drawing in III-b district among Fig. 3;

Among the figure: 1. loop wheel machine grab bucket, 2. refuse pit, 3. separator, 4. inorganic matter bunker, 5. ribbon conveyer, 6. magnetic separator, 7. old metal bunker, 8. ribbon conveyer, 9. digester, 10. spiral water squeezing/feed appliance, 11. biogas carrier pipes, 12. rubbish carrier pipes, 13.CO ₂The sealing gland feed arrangement, 14. rubbish carrier pipes, 15. air pumps, 16. blow the material blower fan, 17. gas-solid separators, 18. circulating fans, 19. calcium oxide replenishes interface, 20. heat exchangers, 21. heat exchanger b, 22. airduct, 23. plasma gasification stoves, 24. plasma torch, 25. the high temperature deodorizer, 25 '. deodorization of air/purifier, 26. heat exchanger c, 27. waste heat boiler, 28. synthesis gas carrier pipes, 29. flying dust carrier pipes, 30. tail gas feedback pipe, 31. cyclone dust collectors, 32. absorption reactor thermallies, 33. absorbent storehouse, 34. blow the material blower fan, 35. melting furnaces, 36. absorbent circulation pipes, 37. absorbent feedback pipe, 38. sack cleaner, 39. blow the material blower fan, 40. air-introduced machines, 41. the carbon monodixe conversion reactor, 42.CO ₂The absorption tower, 43. absorption liquids replenish pipe, 44. compressor a, 45. absorption liquid circulation pipes, 46. regeneration reactor, 47. absorption liquid circulating pumps, 48. synthesis gas basins, 49. the hydrogenation blender, 50. hydrogen make interfaces, 51. compressors, 52. methanol synthesis reactor, 53. sedimentation basins, 54. water pumps, 55. the blended absorbent device, 56. compressor b, 57. coolers, 58. the waterpower dirt separator, 59. solidify slag, 60. limewash circulating pumps, 61. the unreacting gas carrier pipe, 62. destilling towers, 63. reactors for synthesis of ammonia, 64. compressor c, 65. methanol product basins, 66. coolers, 67. ammonia separator, 68. anhydrous ammonia tanks, 69. air pumps, 70. rubbish ginseng draining pond, 71. water pumps, 72. air curtains, 73. discharging platform, 74. air exhausters, 75. control valves, 76. control valve, 77. control valves, 78. control valves; 301. hopper, the outlet of 302. inorganic matters, 303. garbage outlets; 901. slag notch, 902. methane outlets, 903. charging apertures; 1001. driving shaft, 1002. hoppers, 1003. helical axis, 1004. shaped spiral housings; 1301. charging aperture, 1302. carbon dioxide replenish interface, 1303. carbon dioxide sealing glands, 1304. feed bins, 1305. shaped spiral housings, 1306. helical axis, 1307. driving shafts; 1701. the solid outlet, 1702. mixture intakes, the outlet of 1703. gaseous state things; 2001. pyrolysis gas input interface, 2002. sub-air chamber, 2003. heat-carrying gas output interfaces, 2004. pyrolysis gas output interfaces, 2005. collection chamber, 2006. heat-exchanging chambers, carbonation reaction chambers 2007., 2008. the carbon dioxide input interface, 2009. calcium oxide spray guns, 2010. heat-carrying gas input interfaces; 2101. pyrolysis gas input interface, 2102. sub-air chamber, 2103. synthesis gas output interfaces, 2104. heat-exchanging chambers, 2105. heat-exchange tube bundles, 2106. blow ash mouth, 2107. collection chambers, 2108. synthesis gas input interfaces, 2109. pyrolysis gas output interfaces, 2110. ash holes; 2301. the import of heat-carrying gas, 2302. rubbish material imports, 2303. pyrolysis gas outlets, 2304. the synthesis gas output interface, 2305. tail gas input interfaces, 2306. flying dusts melt down interface, 2307. slag notch, 2308. the biogas input interface, 2309. pyrolysis gas input interfaces, 2310. heat-carrying gas output interfaces, 2311. furnace wall, 23-I. the oven dry section, 23-II. pyrolysis section, 23-III. gasification section; 2501. foul smell air input interface, 2502. syngas outlet, 2503. deodorization air outlet slits, 2504. synthetic input interfaces; 2601. air outlet slit, 2602. hot-air inlets; 2701. the synthesis gas import, 2702. syngas outlet; 3101. the outlet of gaseous state thing, 3102. mixture input interfaces, the outlet of 3103. solid; 3201. syngas outlet, 3202. absorbent input interfaces, 3203. synthesis gas input interfaces; 3801. the synthesis gas output interface, the outlet of 3802. flying dusts, 3803. synthesis gas input interfaces; 4101. the synthesis gas input interface, 4102. synthesis gas output interfaces; 4201. the synthesis gas output interface, 4202. synthesis gas input interfaces, 4203.K ₂CO ₃The solution input interface, 4204.KHCO ₃Output interface; 4601.KHCO ₃Input interface, 4602.K ₂CO ₃The solution output interface, 4603. carbon dioxide output interfaces; 4801. the synthesis gas input interface, 4802. synthesis gas output interfaces; 4901. the hydrogen input interface, 4902. synthesis gas output interfaces, 4903. synthesis gas input interfaces; 5201. raw material gas inlet, 5202. return-air interfaces, 5203. methyl alcohol gas output interfaces; 5301. the sewage import, 5302. suction hoses, 5203. slag tap; 5501. the import of methyl alcohol gas, 5502. limewash imports, 5503. mixture outlets; 5701. the limewash outlet, 5702. limewash imports; 5801. the limewash outlet, 5802. outlets of sewer, 5803. limewash input interfaces; 6201. the mixture input interface, the outlet of 6202. limewash, the outlet of 6203. methanol product, the outlet of 6204. unreacting gas; 6301. charging aperture, 6302. ammonia outlet; 6601. the ammonia input interface, 6602. ammonia mixture output interfaces; 6701. ammonia mixture input interface, 6702. liquefied ammonia output interfaces, the outlet of 6703. tail gas.

The specific embodiment

In embodiment 1 embodiment shown in Figure 1, house refuse or debirs are sloughed part moisture with fermentation mode in refuse pit, then by sorting, the organic solid waste material that sub-elects is sent into feeding screw, in the course of conveying of feeding screw, remove part moisture once more by extruding, then rubbish material is passed through CO ₂The sealing gland feed arrangement is sent into the plasma gasification stove; Rubbish material is dried, after the pyrolysis, is become the rubbish charcoal and enter gasification section by oven dry section, pyrolysis section successively in the plasma gasification stove, carries out gasification reaction with the water vapour analyte that sprays into gasification section from plasma torch, finishes gasification, generates with CO and H ₂Hydrogen-rich synthetic gas for main component; The operating temperature of control oven dry section is between 120～300 ℃, the operating temperature of pyrolysis section is between 300～1000 ℃, the operating temperature of gasification section is between 1000～1300 ℃, and the operating temperature in slag district is between 1300～1600 ℃, and the operating pressure in the gasification furnace is controlled between 0～5kPa; In gasification section plasma torch is set, the required heat of gasification mainly provides the exothermic reaction with plasma activity chemistry thing and rubbish charcoal to provide by plasma torch in the stove, with the working gas of water vapour as gasifying agent and plasma torch, water vapour is heated to more than 4200 ℃ by plasma torch, hydrone is all decomposed, generate H ^*, H ₂ ^*, HO ^*, O ^*, O ₂ ^*And H ₂O ^*After, be sprayed directly on on the rubbish charcoal of gasification section, the rubbish charcoal as inhaling hydrogen and oxygen uptake element, is generated CO and H ₂, fusion is a liquid slag in the environment that lime-ash is 1300～1600 ℃ in the in-furnace slag district, enters slag bath by water seal, becomes the vitreum particle; Heat release when generating calcium carbonate with the calcium oxide absorbing carbon dioxide to provide auxiliary thermal source for gasification, the coordinated with plasma gasification, at gasification system the carbonation reaction chamber is set, calcium oxide and carbon dioxide are input to the carbonation reaction chamber, carry out carbonation reaction, simultaneous oxidation calcium is double as dechlorination/desulfurizing agent also, the pyrolysis gas that pyrolysis section in the plasma gasification stove is produced is incorporated into the carbonation reaction chamber, in the environment that excessive 1.2 times of calcium oxide exist, slough the bioxin predecessor, chloride and sulfide, again pyrolysis gas as carrier gas, take calcium oxide, calcium carbonate mixture and heat enter the oven dry section in the plasma gasification stove, for the oven dry and the preheating of newly going into the stove rubbish material provides heat energy, then pyrolysis gas is drawn stove and send into gas-solid separator outward, calcium oxide and calcium carbonate are separated, again pyrolysis gas is sent into heat exchanger by circulating fan, after heat exchanger heats up by being heated indirectly, send in the gasification section of plasma gasification stove, in 1000～1300 ℃ environment, methane in the pyrolysis gas, gaseous state tar, ethene, ethane, things such as water vapour carry out cracking and chemical reaction, thoroughly disintegrate simultaneously bioxin, pass through cycle gasification, make into stove rubbish and decomposed fully, generating with hydrogen and carbon monoxide is the hydrogen-rich synthetic gas of main component; Hydrogen-rich synthetic gas is drawn in the plasma gasification stove, send into the waste heat boiler recovery waste heat and produce steam, synthesis gas is cooled to about 232 ℃, carry out the depickling processing sending into absorption reactor thermally by the synthesis gas after the waste heat boiler cooling, make absorbent with calcium oxide or calcium hydroxide, remove acid contaminants such as chloride in the synthesis gas, sulfide, fluoride, pass through cyclone dust collectors then, absorbent separated send absorption reactor thermally back to and carry out recyclingly, again synthesis gas is removed flying dust by sack cleaner; Sending into CO through the synthesis gas of depickling and dust removal process ₂The absorption tower, with the carbon dioxide in the solution of potassium carbonate absorption synthesis gas, the saleratus that the solution of potassium carbonate absorbing carbon dioxide generates is sent into regeneration reactor, saleratus is decomposed into solution of potassium carbonate and carbon dioxide, the solution of potassium carbonate that decomposites is sent back to CO by heating ₂The absorption tower is carried out recycling, and the carbon dioxide that decomposites is sent into the carbonation reaction chamber of gasification system, carries out carbonation reaction with calcium oxide; The synthesis gas of sloughing carbon dioxide is sent into the synthesis gas basin by compressor a; The synthesis gas that comes out from the synthesis gas basin is sent into methanol synthesis reactor by compressor produce methyl alcohol, hydrogen-rich synthetic gas in methanol synthesis reactor by catalysis synthesizing methanol product, go into the methyl alcohol pneumatic transmission in the blended absorbent device miscible again with limewash, the remaining pollutant that comprises bioxin, carbon dioxide are absorbed by limewash, pass through separated then, methyl alcohol is separated, unreacting gas is sent back to methanol synthesis reactor carry out circular response, limewash is sent back to the blended absorbent device by circulating pump after by scrubbing carry out recycling; Tail gas is sent back to the plasma gasification stove by control valve melt down processing or send into synthetic ammonia installation production liquefied ammonia,, form a closed cycle production system to eliminate nitrogen.In the present embodiment, the draining that oozes that produces in the house refuse preprocessing process is sent into digester and is produced biogas by anaerobic fermentation, biogas is sent into the plasma gasification stove carry out resolution process, the natural pond slag as fertilizer; The inorganic matter that sub-elects in the preprocessing process is sorted again, reclaim old metal, after more nonmetal inorganic matter being passed through to pulverize, mix, be used for producing non-burning brick with the isolated calcium carbonate of gasification system, calcium oxide; The plasma gasification fire grate is gone into the slag of water seal slag bath, becomes the vitreum particle, can directly do the building materials utilization; The flying dust of collecting from sack cleaner, to handle by melting furnace, slag can directly be done the building materials utilization; The vapour that shifts out from methanol synthesis reactor, aqueous mixtures are sent into waste heat boiler produce steam, steam is used for the work gas and the steam-electric power of plasma torch.In this enforcement, when the mark of hydrogen in the synthesis gas of plasma gasification stove production when not reaching the requiring of synthesizing methanol, take at CO ₂The prime on absorption tower increases carbon monodixe conversion and operates the hydrogen fraction scale that improves in the synthesis gas or take the hydrogenation measure to make synthesis gas reach requirement.Synthesis reactor that the synthetic employing of methyl alcohol is conventional or employing China Patent No. are 200710166618.5 electrocatalysis synthesis reactor, when adopting conventional synthesis reactor, use the Cu/Zn/Al catalyst, synthesizing methanol in the environment of 210～280 ℃ of operating pressure 3～15Mpa, operating temperature; When adopting electrocatalysis synthesis reactor, use the Cu/Zn/Al catalyst, synthesizing methanol in the environment of 120～400 ℃ of operating pressure 0～1Mpa, operating temperature.

Embodiment 2 present embodiments are shown in the general system diagram of Fig. 2 and shown in Fig. 4,5,6,7 detail drawing, the disposal system of domestic garbage gasification-liquefaction comprises: the synthetic and terminal part (the IV district of Fig. 2) that purifies of house refuse preprocessing part (the I district of Fig. 2), plasma gasification part (the II-a district of Fig. 2), purified synthesis gas part (the III-a district of Fig. 2) and methyl alcohol, system are mainly by discharging platform (73), refuse pit (2), loop wheel machine grab bucket (1), separator (3), spiral water squeezing/feed appliance (10), CO ₂Sealing gland feed arrangement (13), plasma gasification stove (23), plasma torch (24), gas-solid separator (17), circulating fan (18), carbonation reaction chamber (2007), heat exchanger (20), waste heat boiler (27), absorption reactor thermally (32), cyclone dust collectors (31), sack cleaner (38), air-introduced machine (40), carbon monodixe conversion reactor (41), CO ₂Absorption tower (42), regeneration reactor (46), compressor a (44), synthesis gas basin (48), compressor (51), methanol synthesis reactor (52), blended absorbent device (55), destilling tower (62), compressor b (56), methanol product basin (65), reactors for synthesis of ammonia (63) and connecting pipe are formed, wherein: discharging platform (73) comprises discharging track and vehicle command post, the discharging track, the vehicle command post, refuse pit (2) and loop wheel machine grab bucket (1) are in the building of steel and concrete structure, the garbage truck import department of building is provided with air curtain (72), there is air exhauster (74) on the roof, the air outlet of air exhauster (74) is connected to the foul smell air input interface (2501) of high temperature deodorizer (25) by airduct (22), and the deodorization air outlet slit (2503) of high temperature deodorizer (25) is connected to the hot-air inlets (2602) of heat exchanger c (26); Spiral water squeezing/feed appliance (10) is made up of hopper (1002), driving shaft (1001), helical axis (1003) and shaped spiral housing (1004), hopper (1002) is on shaped spiral housing (1004), helical axis (1003) is arranged in the shaped spiral housing (1004), helical axis (1003) is by driving shaft (1001) driven rotary, play water squeezing and push the material effect, the discharging opening of spiral water squeezing/feed appliance (10) is at the front end of shaped spiral housing (1004); CO ₂Sealing gland feed arrangement (13) is made up of feed bin (1304), carbon dioxide sealing gland (1303), shaped spiral housing (1305), helical axis (1306), driving shaft (1307), gearbox and motor, feed bin (1304) is on shaped spiral housing (1305), and feed bin has CO in (1304) ₂The sealing gland material, the feeding inlet of the discharging opening of feed bin (1304) and shaped spiral housing (1305) has helical axis (1306) in the shaped spiral housing (1305), and helical axis (1306) works to push material, CO ₂The discharging opening of sealing gland feed arrangement (13) is at the front end of shaped spiral housing (1305); The interior space of plasma gasification stove (23) is divided into oven dry section (23-I), pyrolysis section (23-II) and gasification section (23-III), on the oven dry section (23-I) rubbish material import (2302) is arranged, heat-carrying gas import (2301) and pyrolysis gas outlet (2303), heat-carrying gas output interface (2310) is arranged on the pyrolysis section (23-II), pyrolysis gas input interface (2309) is arranged on the gasification section (23-III), a side has slag notch (2307) in the bottom of gasification section (23-III), between gasification section (23-III) and slag notch (2307), the slag district is arranged, synthesis gas output interface (2304) is arranged at the binding site of pyrolysis section (23-II) and gasification section (23-III); Plasma torch (24) is installed in the gasification section (23-III) of plasma gasification stove (23) bottom; Heat exchanger (20) is made of sub-air chamber (2002), heat-exchanging chamber (2006) and collection chamber (2005), pyrolysis gas input interface (2001) is arranged in the sub-air chamber (2002), heat-carrying gas output interface (2003) is arranged on the heat-exchanging chamber (2006), pyrolysis gas output interface (2004) is arranged on the collection chamber (2005); Carbonation reaction chamber (2007) is installed on the heat exchanger (20), carbonation reaction chamber (2007) communicates with the heat-exchanging chamber (2006) of heat exchanger (20), and heat-carrying gas input interface (2010), calcium oxide spray gun (2009) and carbon dioxide input interface (2008) are arranged on carbonation reaction chamber (2007); Blended absorbent device (55) is by the blended absorbent chamber, the venturi water-filling nozzle, the methyl alcohol gas jets, methyl alcohol gas import (5501), limewash import (5502), mixture outlet (5503) and housing are formed, the blended absorbent chamber, venturi water filling port and methyl alcohol gas jets are in housing, the blended absorbent chamber is after the venturi water filling port, before the venturi water filling port is the methyl alcohol gas jets, the internal diameter of methyl alcohol gas jets is enlarged to import gradually by spout, the length of methyl alcohol gas jets is 2.5 times of average diameter, the external diameter of methyl alcohol gas jets spout is 0.7～0.8 times of venturi water filling port internal diameter, methyl alcohol gas jets and venturi water filling port coaxial design, the methyl alcohol gas jets extend into the venturi water filling port 1/3 in the housing, methyl alcohol gas import (5501) is connected the import of methyl alcohol gas jets, limewash import (5502) is arranged on the housing between venturi water filling port and the methyl alcohol gas input, and mixture outlet (5503) is arranged on the housing of blended absorbent chamber.Refuse pit (2) is received the hopper (301) of separator (3) by loop wheel machine grab bucket (1) weighing apparatus, the garbage outlet (303) of separator (3) is received the hopper (1002) of spiral water squeezing/feed appliance (10) by band conveyor (8) weighing apparatus, and the discharging opening of spiral water squeezing/feed appliance (10) is received CO by carrier pipe (12) weighing apparatus ₂The charging aperture (1301) of sealing gland feed arrangement (13), CO ₂The discharging opening of sealing gland feed arrangement (13) is connected to the rubbish material import (2302) of plasma gasification stove (23) by carrier pipe (14), the heat-carrying gas output interface (2310) of plasma gasification stove (23) is connected to the heat-carrying gas input interface (2010) of carbonation reaction chamber (2007), and the heat-carrying gas output interface (2003) of heat exchanger (20) is connected to the heat-carrying gas import (2301) of plasma gasification stove (23); The pyrolysis gas outlet (2303) of plasma gasification stove (23) is connected to the mixture intake (1702) of gas-solid separator (17), the gaseous state thing of gas-solid separator (17) outlet (1703) is connected to the pyrolysis gas input interface (2001) of heat exchanger (20) by circulating fan (18), and the pyrolysis gas output interface (2004) of heat exchanger (20) is connected to the pyrolysis gas input interface (2309) of plasma gasification stove (23); The solid outlet (1701) of gas-solid separator (17) is connected respectively to the slag storehouse and is connected to calcium oxide spray gun (2009) by pipeline, also is connected to calcium oxide and replenishes interface (19) and blow material blower fan (16) on connecting pipe; The synthesis gas output interface (2304) of plasma gasification stove (23) is connected to the synthesis gas import (2701) of waste heat boiler (27), the moisturizing interface of waste heat boiler (27) is connected to supply equipment, the steam output interface of waste heat boiler (27) is connected to on the steam pipe system, and the ash discharging hole of waste heat boiler (27) melts down interface (2306) by the flying dust that flying dust carrier pipe (29) is connected to plasma gasification stove (23); The syngas outlet (2702) of waste heat boiler (27) is connected to the synthesis gas input interface (3203) of absorption reactor thermally (32), the discharging opening in absorbent storehouse (33) connects the absorbent input interface (3202) of absorption reactor thermally (32), the conveying pipeline of absorbent input interface (3202) is also connected to the air outlet that blows material blower fan (34), and the air inlet that blows material blower fan (34) is connected on the synthesis gas carrier pipe (28); The synthesis gas output interface (3201) of absorption reactor thermally (32) is connected to the mixture input interface (3102) of cyclone dust collectors (31), the solid of cyclone dust collectors (31) outlet (3103) is connected on the tube connector of input interface (3203) of absorption reactor thermally (32), the gaseous state thing outlet (3101) of cyclone dust collectors (31) is connected to the synthesis gas input interface (3803) of sack cleaner (38), the flying dust outlet (3802) of sack cleaner (38) is connected to melting furnace (35), the synthesis gas output interface (3801) of sack cleaner (38) is connected to the air inlet of air-introduced machine (40), the air outlet of air-introduced machine (40) is connected to the synthesis gas input interface (4101) of carbon monodixe conversion reactor (41), and the synthesis gas output interface (4102) of carbon monodixe conversion reactor (41) is connected to CO ₂The synthesis gas input interface (4202) on absorption tower (42), CO ₂The KHCO on absorption tower (42) ₃Output interface (4204) is connected to the KHCO of regenerator (46) ₃Input interface (4601), the CO of regenerator (46) ₂Output interface (4603) is connected to the carbon dioxide input interface (2008) of carbonation reaction chamber (2007), the K of regenerator (46) ₂CO ₃Solution output interface (4602) is connected to CO ₂The K on absorption tower (42) ₂CO ₃Solution input interface (4203), CO ₂The synthesis gas output interface (4201) on absorption tower (42) is connected to the synthesis gas input interface (4801) of synthesis gas basin (48) by compressor a (44), the synthesis gas output interface (4802) of synthesis gas basin (48) is connected to the air entry of compressor (51), the exhaust outlet of compressor (51) is connected to the raw material gas inlet (5201) of methanol synthesis reactor (52), the methyl alcohol gas outlet (5203) of methanol synthesis reactor (52) is connected to the methyl alcohol gas import (5501) of blended absorbent device (55) by pressure reduction control valve, the mixture outlet (5503) of blended absorbent device (55) is connected to the mixture input interface (6201) of destilling tower (62), the unreacting gas outlet (6204) of destilling tower (62) is by control valve (76), unreacting gas pipeline (61) and compressor b (56) are connected to the return-air interface (5202) of methanol synthesis reactor (52), and the methanol product outlet (6203) of destilling tower (62) is connected to methyl alcohol basin (65); The limewash outlet (6202) of destilling tower (62) is connected to the input interface (5803) of dirt separator (58), the outlet of sewer (5802) of dirt separator (58) is connected to sedimentation basin (53), the limewash outlet (5801) of dirt separator (58) is connected to the water sucking mouth of circulating pump (60), and the delivery port of circulating pump (60) is connected to the limewash import (5502) of blended absorbent device (55); Filtered water one side of sedimentation basin (53) has suction hose (5302) to be connected to the water sucking mouth of water pump (54), and the delivery port of water pump (54) is connected on the connecting pipe of limewash import (5502) of blended absorbent device (55); The unreacting gas outlet (6204) of destilling tower (62) also is connected to the charging aperture (6301) of reactors for synthesis of ammonia (63) by control valve (75) and compressor c (64), the ammonia outlet (6302) of reactors for synthesis of ammonia (63) is connected to the ammonia input interface (6601) of cooler (66), the ammonia mixture output interface (6602) of cooler (66) is connected to the ammonia mixture input interface (6701) of ammonia separator (67), the liquefied ammonia output interface (6702) of ammonia separator (67) is connected to anhydrous ammonia tank (68), the tail gas outlet (6703) of ammonia separator (67) is connected on the unreacting gas pipeline (61) by control valve (78), and unreacting gas pipeline (61) is by control valve (77), air pump (69) and tail gas feedback pipe (30) are connected to the tail gas input interface (2305) of plasma gasification stove (23); The draining interface that oozes of refuse pit (2), separator (3) and spiral water squeezing/feed appliance (10) is connected to the charging aperture (903) of digester (9) by carrier pipe, and the methane outlet (902) of digester (9) is connected to the biogas input interface (2308) of plasma gasification stove (23) by biogas carrier pipe (11) and air pump (15).

Embodiment 3 present embodiments are shown in the general system diagram of Fig. 3 and shown in Fig. 4,7,8,9 detail drawing, the disposal system of domestic garbage gasification-liquefaction comprises: the synthetic and terminal part (the IV district of Fig. 3) that purifies of house refuse preprocessing part (the I district of Fig. 3), plasma gasification part (the II-b district of Fig. 3), purified synthesis gas part (the III-b district of Fig. 3) and methyl alcohol, system is mainly by discharging platform (73), loop wheel machine grab bucket (1), refuse pit (2), separator (3), digester (9), spiral water squeezing/feed appliance (10), CO ₂Sealing gland feed arrangement (13), plasma gasification stove (23), plasma torch (24), circulating fan (18), heat exchanger b (21), waste heat boiler (27), air-introduced machine (40), absorption reactor thermally (32), cyclone dust collectors (31), sack cleaner (38), compressor a (44), synthesis gas basin (48), hydrogenation blender (49), compressor (51), methanol synthesis reactor (52), blended absorbent device (55), compressor b (56), waterpower dirt separator (58), limewash circulating pump (60), destilling tower (62), reactors for synthesis of ammonia (63), compressor c (64), methanol product basin (65) and connecting pipe are formed, wherein: there is air exhauster (74) top of refuse pit (2) and separator (3), and the air outlet of air exhauster (74) is connected to deodorization of air/purifier (25 ') by airduct (22); The interior space of plasma gasification stove (23) is divided into oven dry section (23-I), pyrolysis section (23-II), gasification section (23-III), the oven dry section goes up (23-I) rubbish material import (2302) and pyrolysis gas outlet (2303), pyrolysis gas input interface (2309) is arranged on the gasification section (23-III), a side has slag notch (2307) in the bottom of gasification section (23-III), between gasification section (23-III) and slag notch (2307) the slag district is arranged, pyrolysis section (23-II) has synthesis gas output interface (2304) with the binding site of gasification section (23-III); Plasma torch (24) is installed in the gasification section (23-III) of plasma gasification stove (23) bottom; Heat exchanger b (21) is by sub-air chamber (2102), heat-exchanging chamber (2104) and collection chamber (2107) constitute, sub-air chamber (2102), heat-exchanging chamber (2104), collection chamber (2107) is isolated with dividing plate mutually, heat-exchange tube bundle (2105) is arranged in the heat-exchanging chamber (2104), place between sub-air chamber (2102) and the collection chamber (2107), sub-air chamber (2102) is communicated to collection chamber (2107) by heat-exchange tube bundle (2105), pyrolysis gas input interface (2101) is arranged in the sub-air chamber (2102), synthesis gas input interface (2108) is arranged on the heat-exchanging chamber (2104), synthesis gas output interface (2103), ash hole (2110) and blow ash mouthful (2106) has pyrolysis gas output interface (2109) on the collection chamber (2107).Refuse pit (2) is received the hopper (301) of separator (3) by loop wheel machine grab bucket (1) weighing apparatus, the garbage outlet (303) of separator (3) is received the hopper (1002) of spiral water squeezing/feed appliance (10) by band conveyor (8) weighing apparatus, and the discharging opening of spiral water squeezing/feed appliance (10) is received CO by carrier pipe (12) weighing apparatus ₂The charging aperture (1301) of sealing gland feed arrangement (13), CO ₂The discharging opening of sealing gland feed arrangement (13) is connected to the rubbish material import (2302) of plasma gasification stove (23) by carrier pipe (14); The pyrolysis gas outlet (2303) of plasma gasification stove (23) is connected to the pyrolysis gas input interface (2101) that is connected to heat exchanger b (21) by circulating fan (18), and the pyrolysis gas output interface (2109) of heat exchanger b (21) is connected to the pyrolysis gas input interface (2309) of plasma gasification stove (23) gasification section; The synthesis gas output interface (2304) of plasma gasification stove (23) is connected to the synthesis gas input interface (2108) of heat exchanger b (21), and the ash hole (2110) of heat exchanger b (21) melts down interface (2306) by the flying dust that ash-valve is connected to plasma gasification stove (23); The synthesis gas output interface (2103) of heat exchanger b (21) is connected to the synthesis gas import (2701) of waste heat boiler (27), and the ash discharging hole of waste heat boiler (27) melts down interface (2306) by the flying dust that flying dust carrier pipe (29) is connected to plasma gasification stove (23); The syngas outlet (2702) of waste heat boiler (27) is connected to the synthesis gas input interface (3203) of absorption reactor thermally (32) by air-introduced machine (40), the discharging opening in absorbent storehouse (33) connects the absorbent input interface (3202) of absorption reactor thermally (32), the conveying pipeline of absorbent input interface (3202) is also connected to the air outlet that blows material blower fan (34), and the air inlet that blows material blower fan (34) is connected on the synthesis gas carrier pipe (28); The synthesis gas output interface (3201) of absorption reactor thermally (32) is connected to the mixture input interface (3102) of cyclone dust collectors (31), the solid outlet (3103) of cyclone dust collectors (31) is connected to the input interface (3203) of absorption reactor thermally (32), the gaseous state thing outlet (3101) of cyclone dust collectors (31) is connected to the synthesis gas input interface (3803) of sack cleaner (38), the flying dust outlet (3802) of sack cleaner (38) is connected to melting furnace (35), the synthesis gas output interface (3801) of sack cleaner (38) is connected to the synthesis gas input interface (4801) of synthesis gas basin (48) by compressor a (44), the synthesis gas output interface (4802) of synthesis gas basin (48) is connected to the synthesis gas input interface (4903) of hydrogenation blender (49), the hydrogen input interface (4901) of hydrogenation blender (49) is connected to hydrogen supply equipment, the synthesis gas output interface (4902) of hydrogenation blender (49) is connected to the air entry of compressor (51), the exhaust outlet of compressor (51) is connected to the raw material gas inlet (5201) of methanol synthesis reactor (52), the methyl alcohol gas outlet (5203) of methanol synthesis reactor (52) is connected to the methyl alcohol gas import (5501) of blended absorbent device (55) by pressure reduction control valve, the mixture outlet (5503) of blended absorbent device (55) is connected to the mixture input interface (6201) of destilling tower (62), the unreacting gas outlet (6204) of destilling tower (62) is by control valve (76), unreacting gas pipeline (61) and compressor b (56) are connected to the return-air interface (5202) of methanol synthesis reactor (52), and the methanol product outlet (6203) of destilling tower (62) is connected to methyl alcohol basin (65); The limewash outlet (6202) of destilling tower (62) is connected to the input interface (5803) of dirt separator (58), the outlet of sewer (5802) of dirt separator (58) is connected to sedimentation basin (53), the limewash outlet (5801) of dirt separator (58) is connected to the water sucking mouth of circulating pump (60), and the delivery port of circulating pump (60) is connected to the limewash import (5502) of blended absorbent device (55); The unreacting gas outlet (6204) of destilling tower (62) also is connected to the charging aperture (6301) of reactors for synthesis of ammonia (63) by control valve (75) and compressor c (64), the ammonia outlet (6302) of reactors for synthesis of ammonia (63) is connected to the ammonia input interface (6601) of cooler (66), the ammonia mixture output interface (6602) of cooler (66) is connected to the ammonia mixture input interface (6701) of ammonia separator (67), the liquefied ammonia output interface (6702) of ammonia separator (67) is connected to anhydrous ammonia tank (68), the tail gas outlet (6703) of ammonia separator (67) is connected on the unreacting gas pipeline (61) by control valve (78), and unreacting gas pipeline (61) is by control valve (77), air pump (69) and tail gas feedback pipe (30) are connected to the tail gas input interface (2305) of plasma gasification stove (23); The draining interface that oozes of refuse pit (2), separator (3) and spiral water squeezing/feed appliance (10) is connected to the charging aperture (903) of digester (9) by carrier pipe, and the methane outlet (902) of digester (9) is connected to the biogas input interface (2308) of plasma gasification stove (23) by biogas carrier pipe (11) and air pump (15).

Among embodiment 4 embodiment shown in Figure 8, a kind of equipment for gasification in domestic garbage gasification-liquefaction disposal system, mainly by plasma gasification stove (23), plasma torch (24), circulating fan (18), heat exchanger b (21) and connecting pipe are formed, wherein: plasma gasification stove (23) is a blast furnace formula structure, furnace wall (2311) from-inner-to-outer of plasma gasification stove (23) is by flame retardant coating, thermal insulation layer, heat-insulation layer and steel sheel are formed, flame retardant coating is built by laying bricks or stones with alumina firebrick or alumina cement concreting, thermal insulation layer is selected diatomite material for use, and heat-insulation layer is selected the aluminosilicate refractory fiber material for use; Thermal insulation layer in gasification section is substituted by cooling layer, cooling layer constitutes water wall structure by the lower collecting box pipe of steel pipe, steel plate, upper header pipe, there is the cooling water interface to insert at the lower collecting box pipe, have the backwater interface to pick out at the upper header pipe, cooling layer is connected (not shown) with the backwater interface with recirculating cooling water system by the cooling water interface; Oven dry section (23-I) is arranged in the plasma gasification stove (23) from top to bottom successively, pyrolysis section (23-II) and gasification section (23-III), oven dry section (23-I), directly communicate between pyrolysis section (23-II) and the gasification section (23-III), there are rubbish material import (2302) access and pyrolysis gas outlet (2303) to pick out on the top of oven dry section (23-I), there is pyrolysis gas input interface (2309) to insert in gasification section (23-III), flying dust melts down interface (2306) and inserts, biogas input interface (2308) inserts and tail gas input interface (2305) inserts, the bottom side of gasification section (23-III) has slag notch (2307), between gasification section (23-III) and slag notch (2307), the slag district is arranged, binding site in pyrolysis section (23-II) and gasification section (23-III) has synthesis gas output interface (2304) to pick out, in oven dry section (23-I), pyrolysis section (23-II), on the furnace wall of gasification section (23-III) temperature sensor is installed respectively, flame-observing mirror also is installed on the furnace wall of gasification section (23-III), on the furnace wall of oven dry section (23-I), level sensor is installed also; Plasma torch (24) is arranged on the furnace wall in gasification section (23-III) and slag district, many plasma torch are the multilayer layout ringwise, work gas input interface, cooling agent input, cooling agent output interface and power interface are arranged on the plasma torch (24), work gas input interface is connected on the steam pipe system by control valve and tube connector, the feed flow that cooling agent input and output interface are connected respectively to coolant apparatus reaches back liquid interface, and power interface is connected on the power supply output of plasma controller; Heat exchanger b (21) is by sub-air chamber (2102), heat-exchanging chamber (2104), heat-exchange tube bundle (2105) and collection chamber (2107) constitute, sub-air chamber (2102), heat-exchanging chamber (2104), collection chamber (2107) is presented, in, following layout, sub-air chamber (2102), heat-exchanging chamber (2104) and collection chamber (2107) are in box hat, the outer wall of box hat is installed insulation material, isolate by upper spacer between sub-air chamber (2102) and the heat-exchanging chamber (2104), isolate by lower clapboard between heat-exchanging chamber (2104) and the collection chamber (2107), heat-exchange tube bundle (2105) is arranged on heat-exchanging chamber (2104) and two ends are through to sub-air chamber (2102) and collection chamber (2107), sub-air chamber (2102), heat-exchange tube bundle (2105) and collection chamber (2107) constitute the return passage of pyrolysis gas, there is pyrolysis gas input interface (2101) to insert in sub-air chamber (2102), there is synthesis gas input interface (2108) to insert at heat-exchanging chamber (2104), synthesis gas output interface (2103) picks out, blow ash mouthful (2106) access and ash hole (2110) and pick out, have pyrolysis gas output interface (2109) to pick out at collection chamber (2107); The pyrolysis gas outlet (2303) of plasma gasification stove (23) oven dry section is connected to the air inlet of circulating fan (18), the air outlet of circulating fan (18) is connected to the pyrolysis gas input interface (2101) of heat exchanger b (21) sub-air chamber, and the pyrolysis gas output interface (2109) of heat exchanger b (21) collection chamber is connected to the pyrolysis gas input interface (2309) of plasma gasification stove (23) gasification section; The synthesis gas output interface (2304) of plasma gasification stove (23) is connected to the synthesis gas input interface (2108) of heat exchanger b (21) heat-exchanging chamber, and the synthesis gas output interface (2103) of heat exchanger b (21) heat-exchanging chamber is connected to back level equipment; The flying dust that the ash hole (2110) of heat exchanger b (21) is connected to plasma gasification stove (23) melts down interface (2306), blowing on the ash mouthful (2106) of heat exchanger b (21) is connected with the soot-blowing wind machine, the air inlet of soot-blowing wind machine is connected on the synthesis gas conveyance conduit, and the air outlet of soot-blowing wind machine is connected to blowing of heat exchanger b (21) grey mouthful (2106).

Claims

1. the method for a domestic garbage gasification-liquefaction disposal comprises calcium oxide cooperation plasma gasification technology, it is characterized in that house refuse or debirs are dewatered and sorting through preliminary treatment, reduces moisture and inorganic content, passes through CO then ₂The sealing gland feed arrangement is sent into the plasma gasification stove; Sets gradually oven dry section, pyrolysis section, gasification section by upper, middle and lower in the plasma gasification stove, rubbish or debirs are dried in stove, pyrolysis and gasification, and generation is with CO and H ₂Hydrogen-rich synthetic gas for main component; In gasification section plasma torch is set, with the working gas of water vapour as gasifying agent and plasma torch, water vapour is heated to more than 4200 ℃ by plasma torch, and hydrone is all decomposed, and generates H ^*, H ₂ ^*, HO ^*, O ^*, O ₂ ^*And H ₂O ^*After, be sprayed directly on on the rubbish charcoal of gasification section, the rubbish charcoal as inhaling hydrogen and oxygen uptake element, is generated CO and H ₂Adopt calcium oxide cooperation plasma gasification mode, at gasification system the carbonation reaction chamber is set, heat release when generating calcium carbonate with the calcium oxide absorbing carbon dioxide to provide auxiliary thermal source for gasification, to reduce the energy consumption of plasma torch, calcium oxide is double as dechlorination/desulfurizing agent also, the pyrolysis gas that plasma gasification stove pyrolysis section is produced is incorporated into the carbonation reaction chamber, in the environment that excessive calcium oxide exists, slough the bioxin predecessor, chloride and sulfide, again pyrolysis gas as carrier gas, take calcium oxide, calcium carbonate mixture and heat enter the oven dry section in the plasma gasification stove, for the oven dry and the preheating of newly going into the stove rubbish material provides heat energy, then pyrolysis gas is introduced gas-solid separator, calcium oxide and calcium carbonate are separated, again the pyrolysis pneumatic transmission is gone in the gasification section of plasma gasification stove, make the methane in the pyrolysis gas, gaseous state tar, ethene, ethane, things such as water vapour carry out cracking and chemical reaction, generation is the hydrogen-rich synthetic gas of main component with hydrogen and carbon monoxide, thoroughly disintegrates bioxin simultaneously; Hydrogen-rich synthetic gas is drawn in the plasma gasification stove, after the waste heat boiler cooling, in the gas purifying equipment of forming by absorption reactor thermally, cyclone dust collectors and sack cleaner, carry out depickling and dedusting again, then at CO ₂The carbon dioxide that absorbs in the synthesis gas with solution of potassium carbonate in the absorption tower generates saleratus, the synthesis gas of sloughing carbon dioxide is sent into methanol synthesis reactor produce methyl alcohol, saleratus is sent into regeneration reactor, by heating saleratus is decomposed into solution of potassium carbonate and carbon dioxide, the solution of potassium carbonate that decomposites is sent back to CO ₂The absorption tower is carried out recycling, and the carbon dioxide that decomposites is sent into the carbonation reaction chamber of gasification system, carries out carbonation reaction with calcium oxide; Hydrogen-rich synthetic gas in methanol synthesis reactor by catalysis synthesizing methanol product, miscible with limewash in the blended absorbent device of cleaning equipment endways methanol product again, remaining pollutant, carbon dioxide are absorbed by limewash, pass through separated then, methyl alcohol is separated, unreacting gas is sent back to methanol synthesis reactor carry out circular response, limewash is sent back to the blended absorbent device after by scrubbing carry out recycling; Tail gas is returned the plasma gasification stove melt down processing, form a closed cycle production system.

2. the system of a domestic garbage gasification-liquefaction disposal comprises plasma gasification equipment, it is characterized in that system is by pre-processing device, CO ₂Sealing gland feed arrangement (13), plasma gasification stove (23), plasma torch (24), gas-solid separator (17), circulating fan (18), heat exchanger (20), carbonation reaction chamber (2007), waste heat boiler (27), absorption reactor thermally (32), cyclone dust collectors (31), sack cleaner (38), CO ₂Absorption tower (42), regenerator (46), methanol synthesis reactor (52), blended absorbent device (55), destilling tower (62), dirt separator (58), circulating pump (60), methyl alcohol basin (65) and connecting pipe are formed, and wherein: pre-processing device comprises refuse pit (2) and separator (3); The interior space of plasma gasification stove (23) is divided into oven dry section, pyrolysis section and gasification section, on the oven dry section rubbish material import, the import of heat-carrying gas and pyrolysis gas outlet are arranged, heat-carrying gas output interface is arranged on the pyrolysis section, pyrolysis gas input interface is arranged on the gasification section, and the binding site of pyrolysis section and gasification section has the synthesis gas output interface; Plasma torch (24) is arranged on the gasification zone, bottom of plasma gasification stove (23); Heat exchanger (20) is made of sub-air chamber, heat-exchanging chamber and collection chamber, and pyrolysis gas input interface is arranged in the sub-air chamber, and heat-carrying gas output interface is arranged on the heat-exchanging chamber, and pyrolysis gas output interface is arranged on the collection chamber; Heat-exchanging chamber in carbonation reaction chamber (2007) and the heat exchanger (20) directly communicates, and heat-carrying gas input interface, calcium oxide input unit and carbon dioxide input interface are arranged on carbonation reaction chamber (2007);

Weighing by loop wheel machine grab bucket (1) between refuse pit (2) and the separator (3) connects, and separator (3) is received the CO of plasma gasification equipment by band conveyor or feeding screw weighing apparatus ₂The charging aperture of sealing gland feed arrangement (13), CO ₂The discharging opening of sealing gland feed arrangement (13) is connected to the rubbish material import of plasma gasification stove (23); The heat-carrying gas output interface of plasma gasification stove (23) is connected to the heat-carrying gas input interface of carbonation reaction chamber (2007), and the heat-carrying gas output interface of heat exchanger (20) is connected to the heat-carrying gas import of plasma gasification stove (23); The pyrolysis gas outlet of plasma gasification stove (23) is connected to the mixture intake of gas-solid separator (17), the gaseous state thing of gas-solid separator (17) exports the pyrolysis gas input interface that is connected to heat exchanger (20) by circulating fan (18), and the pyrolysis gas output interface of heat exchanger (20) is connected to the pyrolysis gas input interface of plasma gasification stove (23); The synthesis gas output interface of plasma gasification stove (23) is connected to the synthesis gas input interface of waste heat boiler (27), the synthesis gas output interface of waste heat boiler (27) is connected to the synthesis gas input interface of absorption reactor thermally (32), the synthesis gas output interface of absorption reactor thermally (32) is connected to the mixture input interface of cyclone dust collectors (31), the solid of cyclone dust collectors (31) exports on the connecting pipe of the synthesis gas input interface that is connected to absorption reactor thermally (32), the gaseous state thing outlet of cyclone dust collectors (31) is connected to the synthesis gas input interface of sack cleaner (38), and the synthesis gas output interface of sack cleaner (38) is connected to CO ₂The synthesis gas input interface on absorption tower (42), CO ₂The KHCO on absorption tower (42) ₃Output interface is connected to the KHCO of regenerator (46) ₃Input interface, the CO of regenerator (46) ₂Output interface is connected to the carbon dioxide input interface of carbonation reaction chamber (2007), the K of regenerator (46) ₂CO ₃The solution output interface is connected to CO ₂The K on absorption tower (42) ₂CO ₃The solution input interface; CO ₂The synthesis gas output interface on absorption tower (42) is connected to the air entry of compressor (51), the exhaust outlet of compressor (51) is connected to the raw material gas inlet of methanol synthesis reactor (52), the methyl alcohol gas outlet of methanol synthesis reactor (52) is connected to the methyl alcohol gas import of blended absorbent device (55), the mixture outlet of blended absorbent device (55) is connected to the mixture input interface of destilling tower (62), the unreacting gas of destilling tower (62) exports the return-air interface that is connected to methanol synthesis reactor (52) by unreacting gas pipeline (61) and compressor b (56), and the methanol product outlet of destilling tower (62) is connected to methyl alcohol basin (65); The limewash outlet of destilling tower (62) is connected to the input interface of dirt separator (58), and the limewash outlet of dirt separator (58) is connected to the water sucking mouth of circulating pump (60), and the delivery port of circulating pump (60) is connected to the limewash import of blended absorbent device (55).

3. the system of a kind of domestic garbage gasification-liquefaction disposal according to claim 2 is characterized in that pre-processing device also comprises spiral water squeezing/feed appliance (10) and digester (9), and spiral water squeezing/feed appliance (10) is arranged on separator (3) and CO ₂Between the sealing gland feed arrangement (13), the outlet of the rubbish material of separator (3) is received the hopper of spiral water squeezing/feed appliance (10) by ribbon conveyer (8) weighing apparatus, and spiral water squeezing/feed appliance (10) discharging opening is connected to CO by carrier pipe (12) ₂The charging aperture of sealing gland feed arrangement (13), CO ₂The discharging opening of sealing gland feed arrangement (13) is connected to the charging aperture of plasma gasification stove (23) by carrier pipe (14); The draining interface that oozes of refuse pit (2), separator (3) and spiral water squeezing/feed appliance (10) is connected to the charging aperture of digester (9) by carrier pipe, and the methane outlet of digester (9) is connected to the gasification zone of plasma gasification stove (23) by carrier pipe.

4. the system of a kind of domestic garbage gasification-liquefaction disposal according to claim 2 is characterized in that at sack cleaner (38) and CO ₂Air-introduced machine (40) and carbon monodixe conversion reactor (41) also are set between the absorption tower (42), the synthesis gas output interface of sack cleaner (38) is connected to the inlet scoop of air-introduced machine (40), the air outlet of air-introduced machine (40) is connected to the synthesis gas input interface of carbon monodixe conversion reactor (41), and the synthesis gas output interface of carbon monodixe conversion reactor (41) is connected to CO ₂The synthesis gas input interface on absorption tower (42).

5. the system of a kind of domestic garbage gasification-liquefaction disposal according to claim 2 is characterized in that at CO ₂Compressor a (44) and synthesis gas basin (48) also are set, CO between absorption tower (42) and the compressor (51) ₂The synthesis gas output interface on solution absorption tower (42) is connected to the air entry of compressor a (44), the exhaust outlet of compressor a (44) is connected to the input interface of synthesis gas basin (48), and the output interface of synthesis gas basin (48) is connected to the air entry of compressor (51).

6. the system of a kind of domestic garbage gasification-liquefaction disposal according to claim 2, it is characterized in that in the unreacting gas pipeline (61) of system for methanol synthesis end, tail gas interface and synthetic ammonia installation being set, tail gas feedback pipe (30) is set between plasma gasification stove (23) and terminal cleaning equipment simultaneously, tail gas interface in the unreacting gas pipeline (61) is connected respectively to the tail gas feedback pipe (30) of plasma gasification stove (23) and the charging interface of synthetic ammonia installation by control valve, and the tail gas outlet of synthetic ammonia installation is connected to the tail gas feedback pipe (30) of plasma gasification stove (23).

7. the system of a domestic garbage gasification-liquefaction disposal comprises plasma gasification equipment, it is characterized in that system is by pre-processing device, CO ₂Sealing gland feed arrangement (13), plasma gasification stove (23), plasma torch (24), circulating fan (18), heat exchanger b (21), waste heat boiler (27), absorption reactor thermally (32), cyclone dust collectors (31), sack cleaner (38), hydrogenation blender (49), methanol synthesis reactor (52), blended absorbent device (55), destilling tower (62), dirt separator (58), circulating pump (60), methyl alcohol basin (65) and connecting pipe are formed, and wherein: pre-processing device comprises refuse pit (2) and separator (3); The interior space of plasma gasification stove (23) is divided into oven dry section, pyrolysis section and gasification section, on the oven dry section rubbish material import and pyrolysis gas outlet is arranged, and pyrolysis gas input interface is arranged on the gasification section, and the binding site of pyrolysis section and gasification section has the synthesis gas output interface; Plasma torch (24) is arranged on the gasification section of plasma gasification stove (23) bottom; Heat exchanger b (21) is made of sub-air chamber, heat-exchanging chamber and collection chamber, and pyrolysis gas input interface is arranged in the sub-air chamber, and synthesis gas input interface and synthesis gas output interface are arranged on the heat-exchanging chamber, and pyrolysis gas output interface is arranged on the collection chamber;

Weighing by loop wheel machine grab bucket (1) between refuse pit (2) and the separator (3) connects, and separator (3) is received the CO of plasma gasification equipment by band conveyor or feeding screw weighing apparatus ₂The charging aperture of sealing gland feed arrangement (13), CO ₂The discharging opening of sealing gland feed arrangement (13) is connected to the charging aperture of plasma gasification stove (23), the pyrolysis gas outlet of plasma gasification stove (23) is connected to the pyrolysis gas input interface of heat exchanger b (21) by circulating fan (18), and the pyrolysis gas output interface of heat exchanger b (21) is connected to the pyrolysis gas input interface of plasma gasification stove (23) gasification section; The synthesis gas output interface of plasma gasification stove (23) is connected to the synthesis gas input interface of heat exchanger b (21), the synthesis gas output interface of heat exchanger b (21) is connected to the synthesis gas input interface of waste heat boiler (27), the synthesis gas output interface of waste heat boiler (27) is connected to the synthesis gas input interface of absorption reactor thermally (32), the synthesis gas output interface of absorption reactor thermally (32) is connected to the mixture input interface of cyclone dust collectors (31), and the solid of cyclone dust collectors (31) exports on the connecting pipe of the synthesis gas input interface that is connected to absorption reactor thermally (32); The gaseous state thing outlet of cyclone dust collectors (31) is connected to the synthesis gas input interface of sack cleaner (38), the synthesis gas output interface of sack cleaner (38) is connected to the air entry of compressor a (44), the exhaust outlet of compressor a (44) is connected to the input interface of synthesis gas basin (48), the output interface of synthesis gas basin (48) is connected to the synthesis gas input interface of hydrogenation blender (49), and the synthesis gas output interface of hydrogenation blender (49) is connected to the air entry of compressor (51); The exhaust outlet of compressor (51) is connected to the raw material gas inlet of methanol synthesis reactor (52), the methyl alcohol gas outlet of methanol synthesis reactor (52) is connected to the methyl alcohol gas import of blended absorbent device (55), the mixture outlet of blended absorbent device (55) is connected to the mixture input interface of destilling tower (62), the unreacting gas of destilling tower (62) exports the return-air interface that is connected to methanol synthesis reactor (52) by unreacting gas pipeline (61) and compressor b (56), and the methanol product outlet of destilling tower (62) is connected to methyl alcohol basin (65); The limewash outlet of destilling tower (62) is connected to the input interface of dirt separator (58), and the limewash outlet of dirt separator (58) is connected to the water sucking mouth of circulating pump (60), and the delivery port of circulating pump (60) is connected to the limewash import of blended absorbent device (55).

8. the system of a kind of domestic garbage gasification-liquefaction disposal according to claim 7 is characterized in that pre-processing device also comprises spiral water squeezing/feed appliance (10) and digester (9), and spiral water squeezing/feed appliance (10) is arranged on separator (3) and CO ₂Between the sealing gland feed arrangement (13), the outlet of the rubbish material of separator (3) is received the hopper of spiral water squeezing/feed appliance (10) by ribbon conveyer (8) weighing apparatus, and spiral water squeezing/feed appliance (10) discharging opening is connected to CO by carrier pipe (12) ₂The charging aperture of sealing gland feed arrangement (13), CO ₂The discharging opening of sealing gland feed arrangement (13) is connected to the charging aperture of plasma gasification stove (23) by carrier pipe (14); The garbage percolation water interface of refuse pit (2), separator (3) and spiral water squeezing/feed appliance (10) is connected to the charging aperture of digester (9) by carrier pipe, and the methane outlet of digester (9) is connected to the gasification section of plasma gasification stove (23) by carrier pipe;

Between waste heat boiler (27) and absorption reactor thermally (32), also has air-introduced machine (40), the syngas outlet of waste heat boiler (27) is connected to the air inlet of air-introduced machine (40), and the air outlet of air-introduced machine (40) is connected to the synthesis gas input interface of absorption reactor thermally (32);

In the unreacting gas pipeline (61) of system for methanol synthesis end, tail gas interface and synthetic ammonia installation are set, tail gas feedback pipe (30) is set between the equipment of plasma gasification stove (23) and system for methanol synthesis end simultaneously, tail gas interface in the unreacting gas pipeline (61) is connected respectively to the tail gas feedback pipe (30) of plasma gasification stove (23) and the charging interface of synthetic ammonia installation by control valve, and the tail gas outlet of synthetic ammonia installation is connected to the tail gas feedback pipe (30) of plasma gasification stove (23).

9. the equipment in domestic garbage gasification-liquefaction disposal system, it is characterized in that equipment for gasification is by plasma gasification stove (23), plasma torch (24), circulating fan (18), heat exchanger b (21) and connecting pipe are formed, wherein: oven dry section (23-I) is arranged in the plasma gasification stove (23) from top to bottom successively, pyrolysis section (23-II) and gasification section (23-III), oven dry section (23-I), directly communicate between pyrolysis section (23-II) and the gasification section (23-III), plasma torch (24) is arranged on the furnace wall of gasification section (23-III), there are rubbish material import (2302) access and pyrolysis gas outlet (2303) to pick out on the top of oven dry section (23-I), there is pyrolysis gas input interface (2309) to insert in gasification section (23-III), slag notch (2307) is arranged at the bottom of gasification section (23-III), has synthesis gas output interface (2304) to pick out at the binding site of pyrolysis section (23-II) and gasification section (23-III); Heat exchanger b (21) is by sub-air chamber (2102), heat-exchanging chamber (2104), heat-exchange tube bundle (2105) and collection chamber (2107) constitute, sub-air chamber (2102), heat-exchanging chamber (2104), collection chamber (2107) is presented, in, following layout, isolate by upper spacer between sub-air chamber (2102) and the heat-exchanging chamber (2104), isolate by lower clapboard between heat-exchanging chamber (2104) and the collection chamber (2107), heat-exchange tube bundle (2105) is arranged on heat-exchanging chamber (2104) and two ends are through to sub-air chamber (2102) and collection chamber (2107), sub-air chamber (2102), heat-exchange tube bundle (2105) and collection chamber (2107) constitute the return passage of pyrolysis gas, there is pyrolysis gas input interface (2101) to insert in sub-air chamber (2102), there are synthesis gas input interface (2108) access and synthesis gas output interface (2103) to pick out at heat-exchanging chamber (2104), have pyrolysis gas output interface (2109) to pick out at collection chamber (2107);

The pyrolysis gas outlet (2303) of plasma gasification stove (23) oven dry section is connected to the air inlet of circulating fan (18), the air outlet of circulating fan (18) is connected to the pyrolysis gas input interface (2101) of heat exchanger b (21) sub-air chamber, and the synthesis gas output interface (2304) that the pyrolysis gas output interface (2109) of heat exchanger b (21) collection chamber is connected to pyrolysis gas input interface (2309) the plasma gasification stove (23) of plasma gasification stove (23) gasification section is connected to the synthesis gas input interface (2108) of heat exchanger b (21) heat-exchanging chamber.

10. the equipment in a kind of domestic garbage gasification according to claim 9-liquefaction disposal system is characterized in that the gasification section (23-III) in plasma gasification stove (23) also has flying dust to melt down interface (2306), biogas input interface (2308) and tail gas input interface (2305) access; Heat-exchanging chamber (2104) in heat exchanger b (21) blows ash mouthful (2106) access in addition and ash hole (2110) picks out, the flying dust that the ash hole (2110) of heat exchanger b (21) is connected to plasma gasification stove (23) melts down interface (2306), blowing on the ash mouthful (2106) of heat exchanger b (21) is connected with the soot-blowing wind machine, the air inlet of soot-blowing wind machine is connected on the synthesis gas conveyance conduit, and the air outlet of soot-blowing wind machine is connected to blowing of heat exchanger b (21) grey mouthful (2106).