CN106862242A - The system and method for processing house refuse - Google Patents

The system and method for processing house refuse Download PDF

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Publication number
CN106862242A
CN106862242A CN201710154376.1A CN201710154376A CN106862242A CN 106862242 A CN106862242 A CN 106862242A CN 201710154376 A CN201710154376 A CN 201710154376A CN 106862242 A CN106862242 A CN 106862242A
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CN
China
Prior art keywords
gas
pyrolysis
outlet
entrance
gasification
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Pending
Application number
CN201710154376.1A
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Chinese (zh)
Inventor
任浩华
张安强
刘璐
赵月晶
周方远
肖磊
吴道洪
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Beijing Shenwu Environmental and Energy Technology Co Ltd
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Beijing Shenwu Environmental and Energy Technology Co Ltd
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Priority to CN201710154376.1A priority Critical patent/CN106862242A/en
Publication of CN106862242A publication Critical patent/CN106862242A/en
Pending legal-status Critical Current

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Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
    • B09B—DISPOSAL OF SOLID WASTE
    • B09B3/00—Destroying solid waste or transforming solid waste into something useful or harmless
    • B09B3/40—Destroying solid waste or transforming solid waste into something useful or harmless involving thermal treatment, e.g. evaporation
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/58—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels combined with pre-distillation of the fuel
    • C10J3/60—Processes
    • C10J3/64—Processes with decomposition of the distillation products
    • C10J3/66—Processes with decomposition of the distillation products by introducing them into the gasification zone
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0913—Carbonaceous raw material
    • C10J2300/0946—Waste, e.g. MSW, tires, glass, tar sand, peat, paper, lignite, oil shale
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C10J2300/1603—Integration of gasification processes with another plant or parts within the plant with gas treatment
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C10J2300/164—Integration of gasification processes with another plant or parts within the plant with conversion of synthesis gas
    • C10J2300/1656—Conversion of synthesis gas to chemicals
    • C10J2300/1665—Conversion of synthesis gas to chemicals to alcohols, e.g. methanol or ethanol
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E50/00—Technologies for the production of fuel of non-fossil origin
    • Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
    • Y02W30/00—Technologies for solid waste management
    • Y02W30/20—Waste processing or separation

Abstract

The invention discloses a kind of system and method for processing house refuse, the system includes：Pretreatment unit, with house refuse entrance, organic waste outlet and inorganic refuse outlet；Pyrolysis installation, with organic waste entrance, high temperature pyrolysis oil gas vent, pyrolytic carbon outlet and pyrolysis offgas outlet；Collecting carbonic anhydride unit, with gas inlet and carbon dioxide gas outlet；First energy-conservation deacidifying device, with carbon dioxide gas outlet after being pyrolyzed oil gas vent and preheating after high temperature pyrolysis oil gas entrance, carbon dioxide entrance, cooling depickling；Methanol synthesis unit, with carbon dioxide entrance and methanol outlet after hydrogen inlet, preheating.The minimizing that can realize house refuse using the system is processed, while by the CO that will be pyrolyzed in tail gas2Utilized as the raw material for preparing methyl alcohol, so as to reduce greenhouse gases CO while realizing that domestic garbage resource is utilized2Discharge, is particularly well-suited to Technique Popularizing and large-scale production.

Description

The system and method for processing house refuse
Technical field
The invention belongs to solid waste resource recovery process field, specifically, the present invention relates to process house refuse System and method.
Background technology
China is faced with the dual-pressure of environment and the energy, and with the acceleration that economy and urbanization are in progress, the national energy disappears Consumption is huge, and 2/3 faces the predicament of garbage-surrounded city in big city.House refuse is changed into by available resources by technological means, The crisis of China's energy and environment can be alleviated to a certain extent.Domestic garbage pyrolysis technology is high with its resource utilization rate, ring Pollute small advantage and increasingly favored by people in border.The primary product of pyrolysis has following several：First, pyrolysis oil；A part Pyrolysis oil can be used by refined as fuel oil；Second, pyrolysis gas；Pyrolysis gas include some low-molecular-weight hydrocarbons, such as Hydrogen, methane, carbon monoxide etc., can use as fuel gas；3rd, pyrolytic carbon；Pyrolytic carbon is most of to be existed in carbon black form, But there is the poisonous and harmful substances such as heavy metal, calorific value is low, and market outlet is poor, if used as solid fuel, combustion efficiency It is poor, and substantial amounts of secondary pollution can be produced in combustion process, environmental benefit is poor, therefore most of pyrolytic carbons finally can only Landfill disposal is carried out as pyrolysis residue, a large amount of land resources is occupied and is caused the waste of the energy.
At present, with expanding economy, carbon emission reduction has turned into the problem of concern.As domestic garbage pyrolysis treatment technology, Substantial amounts of CO is generated while domestic garbage resource is realized2, CO2It is both to cause the greenhouse gases of global warming One of main component, the contribution to greenhouse effects reaches 55%, is again a kind of valuable resource.At present, CO2It is widely used in The fields such as food fresh keeping, oil recovery business, gas shielded arc welding and chemical industry synthesis, and achieve good economic benefit.But it is annual to use Discharged CO is only accounted in the amount of production consumption2One small part of total output, substantial amounts of CO2Cannot be fully used and discharge To in air, greenhouse effects are exacerbated, be the key factor for restricting Sustainable Development of Enterprises.
Therefore, the technology of existing treatment house refuse is further improved.
The content of the invention
It is contemplated that at least solving one of technical problem in correlation technique to a certain extent.Therefore, of the invention One purpose is to propose a kind of system and method for processing house refuse.The decrement of house refuse can be realized using the system Change is processed, while by the CO that will be pyrolyzed in tail gas2Utilized as the raw material for preparing methyl alcohol, so as to realize domestic garbage resources Changing reduces greenhouse gases CO while utilization2Discharge, is particularly well-suited to Technique Popularizing and large-scale production.
In one aspect of the invention, the present invention proposes a kind of system for processing house refuse, reality of the invention Example is applied, the system includes：
There is pretreatment unit, the pretreatment unit house refuse entrance, organic waste outlet and inorganic refuse to export；
Pyrolysis installation, the pyrolysis installation has organic waste entrance, high temperature pyrolysis oil gas vent, pyrolytic carbon outlet and heat Solution offgas outlet, the organic waste entrance is connected with organic waste outlet；
Collecting carbonic anhydride unit, the collecting carbonic anhydride unit has gas inlet and carbon dioxide gas outlet, The gas inlet is connected with the pyrolysis offgas outlet；
First energy-conservation deacidifying device, the first energy-conservation deacidifying device has high temperature pyrolysis oil gas entrance, carbon dioxide gas Body entrance, cooling depickling after be pyrolyzed oil gas vent and preheating after carbon dioxide gas outlet, the carbon dioxide entrance with The carbon dioxide gas outlet is connected, and the high temperature pyrolysis oil gas entrance is connected with the high temperature pyrolysis oil gas vent；
Methanol synthesis unit, the methanol synthesis unit has carbon dioxide entrance and first after hydrogen inlet, preheating Alcohol outlet, carbon dioxide entrance is connected with carbon dioxide gas outlet after the preheating after the preheating.
The system for the treatment of house refuse according to embodiments of the present invention by the way that house refuse is pre-processed after supply to pyrolysis Device carries out pyrolysis processing, to obtain high temperature pyrolysis oil gas, pyrolytic carbon and pyrolysis tail gas；Wherein, pyrolysis tail gas enters dioxy Changing carbon capture unit carries out collecting carbonic anhydride, and then will trap the carbon dioxide for obtaining and supply to the first energy-conservation depickling dress Heat exchange and depickling treatment are carried out in putting, so that carbon dioxide is preheated, the carbon dioxide after preheating is closed into methyl alcohol Into unit, for synthesizing methanol.Thus, the system of the application in the pyrolysis tail gas that is obtained from domestic garbage pyrolysis by extracting two Carbonoxide realizes the recycling of house refuse as the raw material of synthesizing methanol, while significantly reducing carbon dioxide Discharge, with significant economic benefit and environmental benefit, be particularly well-suited to Technique Popularizing and large-scale production.
In addition, the system for the treatment of house refuse according to the above embodiment of the present invention can also have following additional technology Feature：
In some embodiments of the invention, the system of above-mentioned treatment house refuse is further included：Pyrolysis oil gas purification Unit, the pyrolysis oil gas clean unit is pyrolyzed oil gas entrance, pyrolysis oil export and pyrolysis gas outlet, institute after having cooling depickling Pyrolysis oil gas entrance is connected with pyrolysis oil gas vent after the cooling depickling after stating cooling depickling；Hydrogen capture unit, the hydrogen Gas capture unit has the outlet of pyrolysis gas entrance, hydrogen outlet and combustible gas, the pyrolysis gas entrance and the pyrolysis gas outlet It is connected, the hydrogen outlet is connected with the hydrogen inlet；Generator unit, the generator unit has fuel inlet, water vapour Outlet and combustion tail gas outlet, the fuel inlet are connected with the pyrolysis oil export and combustible gas outlet respectively, described Combustion tail gas outlet is connected with the gas inlet.Thus, it is possible to using in the pyrolysis oil gas obtained from domestic garbage pyrolysis points Isolated combustible gas is generated electricity as fuel in the pyrolysis oil and pyrolysis gas for obtaining, so as to further improve life rubbish The resource utilization of rubbish.
In some embodiments of the invention, the system of above-mentioned treatment house refuse is further included：Breaker, it is described Breaker has pyrolytic carbon entrance and pyrolytic carbon particle outlet, and the pyrolytic carbon entrance is connected with pyrolytic carbon outlet；Gas Makeup is put, and the gasification installation has pyrolytic carbon particle entrance, steam entry, the outlet of gasification gas and gasification solid discharge, institute State pyrolytic carbon particle entrance to be connected with the pyrolytic carbon particle outlet, the steam entry is connected with the steam outlet； Second energy-conservation deacidifying device, the second energy-conservation deacidifying device has gasification gas outlet, institute after gasification gas entrance and cooling depickling Gasification gas entrance is stated to be connected with the gasification gas outlet；Gasification gas clean unit, the gasification gas clean unit has cooling de- Gasify after acid gas entrance and the outlet of purification gasification gas, gasify gas after gasify after the cooling depickling gas entrance and the cooling depickling Outlet is connected, and the purification gasification gas outlet is connected with the pyrolysis installation.Thus, it is possible to pass through breaker pyrolytic carbon be broken It is broken to obtain pyrolytic carbon particle, and then pyrolytic carbon particle is supplied to gasification installation, and using the vapor obtained in generator unit It is the gasification gas with carbon monoxide and hydrogen as main component by the gasification of pyrolytic carbon particle, gasification gas is filled into the second energy-conservation depickling Put with combustion-supporting gas after heat exchange and depickling are processed, combustion-supporting gas after gasify after the cooling depickling for obtaining gas and preheating, depickling of lowering the temperature Gasification gas enters in gasification gas clean unit afterwards carries out purified treatment, is purified gasification gas, subsequently can be used for pyrolysis installation In fuel use, thus achieve the recycling to low heat value pyrolytic carbon.
In another aspect of the invention, the present invention proposes a kind of system treatment life using above-mentioned treatment house refuse The method of rubbish living, embodiments in accordance with the present invention, the method includes：
(1) house refuse is supplied into the pretreatment unit and is pre-processed, to obtain organic waste and inorganic Rubbish；
(2) supplying the organic waste carries out pyrolysis processing into the pyrolysis installation, to obtain high temperature pyrolysis oil Air and heat solution charcoal and pyrolysis tail gas；
(3) the pyrolysis tail gas is supplied into the collecting carbonic anhydride unit, to obtain carbon dioxide；
(4) carbon dioxide and the high temperature pyrolysis oil gas are supplied into the first energy-conservation deacidifying device Row heat exchange and depickling treatment, to be pyrolyzed oil gas after carbon dioxide after being preheated and cooling depickling；
(5) carbon dioxide after the preheating and hydrogen are supplied into the methanol synthesis unit, to obtain first Alcohol.
It is according to the above embodiment of the present invention treatment house refuse method by the way that house refuse is pre-processed after supply to Pyrolysis installation carries out pyrolysis processing, to obtain high temperature pyrolysis oil gas, pyrolytic carbon and pyrolysis tail gas；Wherein, pyrolysis tail gas enters Collecting carbonic anhydride unit carries out collecting carbonic anhydride, and then will trap the carbon dioxide for obtaining and supply to the first energy-conservation and take off Heat exchange and depickling treatment are carried out in sour device, so that carbon dioxide is preheated, the carbon dioxide after preheating enters first Alcohol synthesis unit, for synthesizing methanol.Thus, the present processes in the pyrolysis tail gas that is obtained from domestic garbage pyrolysis by carrying Raw material of the carbon dioxide as synthesizing methanol is taken, the recycling of house refuse is realized, while significantly reducing carbon dioxide The discharge of gas, with significant economic benefit and environmental benefit, is particularly well-suited to Technique Popularizing and large-scale production.
In addition, the method for the treatment of house refuse according to the above embodiment of the present invention can also have following additional technology Feature：
In some embodiments of the invention, the method for the treatment house refuse is further included：(6) by step (4) Pyrolysis oil gas is supplied after the cooling depickling for obtaining carries out purified treatment into the pyrolysis oil gas clean unit, to obtain Pyrolysis oil and pyrolysis gas；(7) pyrolysis gas are supplied into the hydrogen capture unit, to obtain hydrogen and combustible gas, And the hydrogen is supplied into the methanol synthesis unit into step (5)；(8) pyrolysis oil for obtaining step (6) and The combustible gas that step (7) is obtained supplies the combustion power generation into the generator unit, to obtain water vapour and combustion tail gas, And the combustion tail gas are supplied the collecting carbonic anhydride unit into step (3).Thus, it is possible to using from house refuse Combustible gas isolated in isolated pyrolysis oil and pyrolysis gas is sent out as fuel in the pyrolysis oil gas that obtains of pyrolysis Electricity, so as to further improve the resource utilization of house refuse.
In some embodiments of the invention, the method for the treatment house refuse is further included：(9) by the pyrolysis Charcoal is supplied carries out break process into the breaker, to obtain pyrolytic carbon particle；(10) by the pyrolytic carbon particle and The water vapour that step (8) is obtained supplies and gasification process is carried out into the gasification installation, to obtain gasify gas and gasification Residue；(11) supplying into the second energy-conservation deacidifying device the gasification gas carries out heat exchange and depickling treatment, to obtain Gasify gas after cooling depickling；(12) gas that will gasify after the cooling depickling is supplied into the gasification gas clean unit and purified Treatment, to be purified gasification gas, and is back to the pyrolysis installation in step (2) by the purification gasification gas.Thus, Pyrolytic carbon can be crushed by breaker and obtain pyrolytic carbon particle, and then pyrolytic carbon particle is supplied to gasification installation, and By the gasification of pyrolytic carbon particle it is gasification with carbon monoxide and hydrogen as main component using the vapor obtained in generator unit Gas, gasification gas enters the second energy-conservation deacidifying device and combustion-supporting gas after heat exchange and depickling are processed, gas after the cooling depickling for obtaining Change combustion-supporting gas after gas and preheating, the gas that gasifies after cooling depickling enters in gasification gas clean unit carries out purified treatment, is purified Gasification gas, the fuel that subsequently can be used in pyrolysis installation is used, and thus achieves the recycling to low heat value pyrolytic carbon.
Additional aspect of the invention and advantage will be set forth in part in the description, and will partly become from the following description Obtain substantially, or recognized by practice of the invention.
Brief description of the drawings
Of the invention above-mentioned and/or additional aspect and advantage will become from description of the accompanying drawings below to embodiment is combined Substantially and be readily appreciated that, wherein：
Fig. 1 is the system structure diagram for the treatment of house refuse according to an embodiment of the invention；
Fig. 2 is the system structure diagram of the treatment house refuse according to further embodiment of the present invention；
Fig. 3 is the system structure diagram of the treatment house refuse according to another embodiment of the invention；
Fig. 4 is the method flow schematic diagram for the treatment of house refuse according to an embodiment of the invention；
Fig. 5 is the method flow schematic diagram of the treatment house refuse according to further embodiment of the present invention；
Fig. 6 is the method flow schematic diagram of the treatment house refuse according to another embodiment of the invention；
Fig. 7 is the system structure diagram of the treatment house refuse according to another embodiment of the invention.
Specific embodiment
Embodiments of the invention are described below in detail, the example of the embodiment is shown in the drawings, wherein from start to finish Same or similar label represents same or similar element or the element with same or like function.Below with reference to attached It is exemplary to scheme the embodiment of description, it is intended to for explaining the present invention, and be not considered as limiting the invention.
In the description of the invention, it is to be understood that term " first ", " second " are only used for describing purpose, and can not It is interpreted as indicating or implying relative importance or the implicit quantity for indicating indicated technical characteristic.Thus, define " the One ", at least one this feature can be expressed or be implicitly included to the feature of " second ".In the description of the invention, " multiple " It is meant that at least two, such as two, three etc., unless otherwise expressly limited specifically.
In the present invention, unless otherwise clearly defined and limited, term " installation ", " connected ", " connection ", " fixation " etc. Term should be interpreted broadly, for example, it may be fixedly connected, or be detachably connected, or integrally；Can be that machinery connects Connect, or electrically connect；Can be joined directly together, it is also possible to be indirectly connected to by intermediary, can be in two elements The connection in portion or two interaction relationships of element, unless otherwise clearly restriction.For one of ordinary skill in the art For, can as the case may be understand above-mentioned term concrete meaning in the present invention.
In one aspect of the invention, the present invention proposes a kind of system for processing house refuse, reality of the invention Example is applied, with reference to Fig. 1, the system includes：Pretreatment unit 100, pyrolysis installation 200, collecting carbonic anhydride unit 300, first segment Can deacidifying device 400 and methanol synthesis unit 500.
There is embodiments in accordance with the present invention, pretreatment unit 100 house refuse entrance 101, organic waste to export 102 and Inorganic refuse outlet 103, and be suitable to be pre-processed house refuse, to obtain organic waste and inorganic refuse.Specifically, Pre-processed by by house refuse, the inorganic refuses such as the bulk inorganic matter and metal in house refuse can be removed, obtained Organic waste to needed for next step pyrolysis.It should be noted that pretreatment unit is not particularly restricted, people in the art Member can be selected according to actual needs, for example, can include the bag-breaking machine being sequentially connected, cylinder round sifter, separator and break Broken machine.Specifically, the metal, the glass that remove in house refuse can be processed by broken bag mechanism, roller screen mechanism and sorting mechanism The inorganic matters such as glass, fragment of brick, and then crushed house refuse by crushing mechanism.A specific implementation of the invention Example, after being processed through above-mentioned pretreatment unit, the particle diameter that can obtain meeting revolving bed pyrolysis oven pan feeding requirement is organic less than 20mm Rubbish, and the moisture content of organic waste is 20wt%-60wt%.
Embodiments in accordance with the present invention, pyrolysis installation 200 has organic waste entrance 201, high temperature pyrolysis oil gas vent 202nd, pyrolytic carbon outlet 203 and pyrolysis offgas outlet 204, organic waste entrance 201 are connected with organic waste outlet 102, and suitable In organic waste is carried out into pyrolysis processing, to obtain high temperature pyrolysis oil gas, pyrolytic carbon and pyrolysis tail gas.It should be noted that hot Solution device is not particularly restricted, and those skilled in the art can be selected according to actual needs, for example, can be to be carried without heat Body heat accumulating type rotating bed pyrolysis oven.Specifically, it should be noted that pyrolysis installation is not particularly restricted, those skilled in the art Can according to actual needs be selected, for example, can be without heat carrier heat accumulating type rotating bed pyrolysis oven.Specifically, by above-mentioned institute The organic waste for obtaining uniformly delivers to revolving bed pyrolysis oven, and layer thickness 50-250mm heats up in stove by the stage, completes dry Dry, pyrolysis and the reaction of activation, the time that revolving bed pyrolysis oven rotates a circle is 1h.Wherein, revolving bed pyrolysis oven is to realize being somebody's turn to do The main equipment of process, it includes revolving bed pyrolysis chamber, ring-shaped furnace bottom and is located at the upper and lower heat accumulating type combustion of ring-shaped furnace bottom respectively The mechanism such as gas radiant tube burner and cloth, discharging, heat storage type gas radiation pipe burner is arranged in annular furnace wall, with hot spoke The mode penetrated refuse pyrolysis are provided needed for heat.Revolving bed pyrolysis oven is disposed with dry section, pyrolysis along the direction for rotating An area, the area of pyrolytic reaction two and the area of pyrolytic reaction three are reacted, pending organic waste enters revolving bed pyrolysis oven from dry section, The furnace roof of revolving bed pyrolysis oven regional is provided with high temperature pyrolysis oil gas vent, for collecting high temperature pyrolysis oil gas, in heat The end pyrolytic carbon exit in 3rd area of solution reaction is provided with drawing mechanism, for collecting pyrolytic carbon, in addition, in order that pending have Machine rubbish is heated evenly, and furnace bottom flitch can select perforated plate.
There is embodiments in accordance with the present invention, collecting carbonic anhydride unit 300 gas inlet 301 and carbon dioxide to go out Mouth 302, gas inlet 301 is connected with pyrolysis offgas outlet 204, and is suitable to be processed in pyrolysis tail gas, to obtain dioxy Change carbon gas.It should be noted that collecting carbonic anhydride unit is not particularly restricted, those skilled in the art can be according to reality Border need selected, for example can include be sequentially connected absorption tower, rich solution pump, desorber, reboiler, gas-liquid separator, Lean pump and lean solution cooler.Specifically, the pyrolysis tail gas from pyrolysis installation feeds absorption tower through blower fan pressurization, on absorption tower Interior and absorbent counter current contacting, the CO in pyrolysis tail gas2Absorbed by absorbent, be changed into rich solution, rich solution feeds desorption through rich solution pump Tower, desorption generation CO2The mixed gas and lean solution of gas, steam and mist, the CO after desorption2Cooled down through cooler, Steam and mist become water and foam, and the mixed gas after cooling enter gas-liquid separator, remove the Shui Hepao in mixed gas Foam, obtains CO2Gas.Wherein, the particular type of absorbent is not particularly restricted, and those skilled in the art can be according to reality Border needs to be selected, for example, can be alkanolamine solution.
Embodiments in accordance with the present invention, the first energy-conservation deacidifying device 400 has high temperature pyrolysis oil gas entrance 401, titanium dioxide Carbon dioxide gas outlet 404, carbon dioxide gas after oil gas vent 403 and preheating are pyrolyzed after carbon gas access 402, cooling depickling Body entrance 402 is connected with carbon dioxide gas outlet 302, high temperature pyrolysis oil gas entrance 401 and the phase of high temperature pyrolysis oil gas vent 202 Connect, and be suitable to for carbon dioxide and high temperature pyrolysis oil gas to carry out heat exchange and depickling treatment, so as to titanium dioxide after being preheated Oil gas is pyrolyzed after carbon gas and cooling depickling.It should be noted that the first energy-conservation deacidifying device is not particularly restricted, this area Technical staff can be selected according to actual needs, for example, can include inert gas duct, pyrolysis feed channel, two four-ways Depickling mode in reversal valve, depickling-accumulation of heat complex, and the step can be that can remove high temperature pyrolysis in the prior art Any method of oil gas middle acid substance, those skilled in the art can be selected according to actual needs.Specifically, carrying out self-heating The high temperature pyrolysis oil gas for solving device enters the first energy-conservation deacidifying device completion waste heat recovery and depickling, high temperature pyrolysis oil gas through pipeline Temperature be down to 200 degrees Celsius, acidic gas concentration is down to 0.02%.First energy-conservation deacidifying device can be to the high-purity that traps CO2Gas is preheated, the CO after preheating2The temperature of gas is up to 100-500 degrees Celsius.
Embodiments in accordance with the present invention, methanol synthesis unit 500 has carbon dioxide after hydrogen inlet 501, preheating Entrance 502 and methanol outlet 503, after preheating carbon dioxide entrance 502 with preheating after the phase of carbon dioxide gas outlet 404 Connect, and be suitable to be processed carbon dioxide after preheating and hydrogen, to obtain methyl alcohol.It should be noted that methanol-fueled CLC Unit is not particularly restricted, and those skilled in the art can be selected according to actual needs, for example, can be closed including methyl alcohol Into device and methanol rectifying system.Wherein methanol synthesizer and methanol rectifying system is not particularly restricted, art technology Personnel can be selected according to actual needs, for example, methanol synthesizer can include gasification gas reburner and methanol-fueled CLC Tower, methanol rectifying system can use double-column process, be made up of pre-tower and king-tower.Specifically, the CO after preheating2Gas and hydrogen 5-7MPa is compressed to through synthesic gas compressor, methanol synthesizer is then entered together, methanol-fueled CLC uses the oxygen of copper, zinc and aluminium Used as catalyst, reaction pressure is 6-9MPa to one or more in compound, and reaction temperature is 200-300 degrees Celsius, after synthesis Crude carbinol by methanol rectifying tower rectifying be obtained methyl alcohol.
It is according to the above embodiment of the present invention treatment house refuse system by the way that house refuse is pre-processed after supply to Pyrolysis installation carries out pyrolysis processing, to obtain high temperature pyrolysis oil gas, pyrolytic carbon and pyrolysis tail gas；Wherein, pyrolysis tail gas enters Collecting carbonic anhydride unit carries out collecting carbonic anhydride, and then will trap the carbon dioxide for obtaining and supply to the first energy-conservation and take off Heat exchange and depickling treatment are carried out in sour device, so that carbon dioxide is preheated, the carbon dioxide after preheating enters first Alcohol synthesis unit, for synthesizing methanol.Thus, the system of the application in the pyrolysis tail gas that is obtained from domestic garbage pyrolysis by carrying Raw material of the carbon dioxide as synthesizing methanol is taken, the recycling of house refuse is realized, while significantly reducing carbon dioxide The discharge of gas, with significant economic benefit and environmental benefit, is particularly well-suited to Technique Popularizing and large-scale production.
Embodiments in accordance with the present invention, with reference to Fig. 2, the system of above-mentioned treatment house refuse is further included：Pyrolysis oil gas Clean unit 600, hydrogen capture unit 700 and generator unit 800.
Embodiments in accordance with the present invention, pyrolysis oil gas clean unit 600 have after cooling depickling be pyrolyzed oil gas entrance 601, Pyrolysis oil export 602 and pyrolysis gas outlet 603, pyrolysis oil gas goes out after oil gas entrance 601 and cooling depickling are pyrolyzed after cooling depickling Mouthfuls 403 are connected, and are suitable to be pyrolyzed oil gas after the cooling depickling that obtains the first energy-conservation deacidifying device and carry out purified treatment, so as to To pyrolysis oil and pyrolysis gas.It should be noted that pyrolysis oil gas clean unit is not particularly restricted, those skilled in the art can To be selected according to actual needs, for example, can include that the gas wash tower, primary cooler, electrical tar precipitator and the dry type that are sequentially connected take off Sulphur tower.A specific embodiment of the invention, oil gas is pyrolyzed after the cooling depickling from the first energy-conservation deacidifying device, is entered Pyrolysis oil gas clean unit can be realized to being pyrolyzed dedusting, desulfurization and denitration of oil gas etc. after cooling depickling so that H2The content of S is not More than 0.01g/Nm3, the content of dust is not more than 50mg/Nm3, the content of benzene is not more than 20mg/Nm3, the content of HCl is not more than 10mg/Nm3.Specifically, being pyrolyzed oil gas after cooling depickling first using the sprinkling cooling of Quench recirculated water, heat to be clean is separated into Profit is vented one's spleen and is pyrolyzed, pyrolysis profit is separated into pyrolysis oil and waste water by Pipeline transport to oil-water separation tank；Heat to be clean Vent one's spleen and complete dedusting by wet dedusting tower, transverse pipe initial cooler is entered after dust therein is removed, primary cooler is with 32 degrees Celsius Recirculated water and two sections of cooling waters of 16 degrees Celsius of chilled water the pyrolysis gas after dedusting are cooled to 21 degrees centigrades, by first The pyrolysis gas of cooler bottom discharge enter the electrical tar precipitator that two parallel connections are operated simultaneously, remove the tar carried secretly in pyrolysis gas, The pyrolysis gas of tar and denitration to be desulfurization are obtained, pyrolysis gas are finally delivered into desulphurization denitration tower by Roots blower again, complete de- Sulphur denitration, obtains pure pyrolysis gas.
Embodiments in accordance with the present invention, hydrogen capture unit 700 has pyrolysis gas entrance 701, hydrogen outlet 702 and flammable Gas outlet 703, pyrolysis gas entrance 701 is connected with pyrolysis gas outlet 603, and hydrogen outlet 702 is connected with hydrogen inlet 501, and suitable Processed in by pyrolysis gas, to obtain hydrogen and combustible gas, and supplied hydrogen to methanol synthesis unit.Need explanation It is that hydrogen capture unit is not particularly restricted, those skilled in the art can be selected according to actual needs, for example can be with It is hydrogen adsorption tower.Specifically, hydrogen pressure-swing absorber has different absorption under different partial pressures using adsorbent to adsorbate Capacity, and under certain adsorptive pressure, each component of the admixture of gas to separate has the characteristic that selection is adsorbed to carry Pure hydrogen.Composed in parallel by 4 adsorbent beds in pressure-swing absorber, adsorptive pressure scope is 1~3MPa, and adsorbent is using activity Charcoal, more than 92%, the hydrogen for being trapped can deliver to the carbon dioxide gas after methanol synthesis unit and preheating to hydrogen recovery rate Thus precursor reactant, can significantly reduce the cost of material of whole system to prepare methyl alcohol, improve the economic benefit of whole system.
Embodiments in accordance with the present invention, generator unit 800 has fuel inlet 801, steam outlet 802 and combustion tail gas Outlet 803, fuel inlet 801 is connected with pyrolysis oil export 602 and combustible gas outlet 703 respectively, and combustion tail gas export 803 and tail Gas entrance 301 is connected, and is suitable to the combustible gas that pyrolysis oil and hydrogen capture unit are obtained for obtaining pyrolysis oil gas clean unit Combustion power generation, to obtain water vapour and combustion tail gas, and combustion tail gas is supplied to collecting carbonic anhydride unit.Specifically, Pyrolysis oil and combustible gas can be supplied to the waste heat boiler of generator unit, exchange heat or produced by burning with water in waste heat boiler Raw superheated steam, superheated steam is generated electricity into Steam Turbine Driven generator, and the electric energy of generation is connected to the grid, and generator unit The combustion tail gas of generation can carry out collecting carbonic anhydride utilization into collecting carbonic anhydride unit.
Embodiments in accordance with the present invention, with reference to Fig. 3, the system of above-mentioned treatment house refuse is further included：Breaker 900th, gasification installation 1000, the second energy-conservation deacidifying device 1100 and gasification gas clean unit 1200.
Embodiments in accordance with the present invention, breaker 900 has pyrolytic carbon entrance 901 and pyrolytic carbon particle outlet 902, heat Solution charcoal entrance 901 is connected with pyrolytic carbon outlet 203, and is suitable to for pyrolytic carbon to carry out break process, to obtain pyrolytic carbon particle. Specifically, after the rubbish charcoal obtained by pyrolysis installation is crushed through breaker, obtaining the rubbish charcoal particle of particle diameter no more than 10mm.Hair A person of good sense has found, by before pyrolytic carbon is carried out into gasification process, pyrolytic carbon being crushed into the particle diameter in advance, can significantly improve The efficiency of gasification process simultaneously reduces the energy consumption of gasification process.
Embodiments in accordance with the present invention, gasification installation 1000 have pyrolytic carbon particle entrance 1001, steam entry 1002, Gasification gas outlet 1003 and gasification solid discharge 1004, pyrolytic carbon particle entrance 1001 are connected with pyrolytic carbon particle outlet 902, water Steam inlet 1002 is connected with steam outlet 802, and the water vapour for being suitable to obtain pyrolytic carbon particle and generator unit is carried out Gasification process, to obtain gasify gas and residue after gasifying.It should be noted that gasification installation is not particularly restricted, this area Technical staff can be selected according to actual needs, for example, can be circle fluidized-bed gasification furnace.Specifically, grain will be crushed to The pyrolytic carbon particle that footpath is not more than 10mm passes through press device and pipeline to circle fluidized-bed gasification furnace as gasified raw material, Vapor enters circle fluidized-bed gasification furnace with pyrolytic carbon particle and gasifies jointly, and gasification temperature is 1000 degrees centigrades, is obtained Gasification gas, residue after gasifying is relatively low due to value, can do construction material or landfill disposal.
Embodiments in accordance with the present invention, after the second energy-conservation deacidifying device 1100 has gasification gas entrance 1101 and cooling depickling Gasification gas outlet 1102, gasification gas entrance 1101 is connected with gasification gas outlet 1003, and is suitable to gasification gas is exchanged heat and taken off Acid treatment, to gasify gas after obtaining cooling depickling.It should be noted that the second energy-conservation deacidifying device can be same as foregoing description The first energy-conservation deacidifying device structure.Specifically, the gasification gas for carrying out self-gasifying device enters the second energy-conservation deacidifying device through pipeline Waste heat recovery and depickling are completed, is gasified gas after obtaining cooling depickling, it is Celsius that the temperature of the gas that gasifies after cooling depickling is down to 200-350 Degree, acidic gas concentration is down to 0.02%-0.05%.
Embodiments in accordance with the present invention, the gas clean unit 1200 that gasifies is with gasification gas entrance 1201 after cooling depickling and only Change gasification gas outlet 1202, the gas entrance 1201 that gasifies after cooling depickling is connected with gas outlet 1102 of gasifying after cooling depickling, purifies Gasification gas outlet 1202 is connected with pyrolysis installation 200, and is suitable to for the gas that gasifies after cooling depickling to carry out purified treatment, to obtain Purification gasification gas, and purification gasification gas is back to pyrolysis installation.It should be noted that gasification gas clean unit is not by special Limitation, those skilled in the art can be selected according to actual needs, such as the gas wash tower that can include being sequentially connected, first cold Device and dry-type desulfurizing tower.Gasify gas after cooling depickling from the second energy-conservation deacidifying device, can be real into gasification gas clean unit Now to dedusting, desulfurization and the denitration etc. of the gas that gasifies after cooling depickling so that wherein H2The content of S is not more than 0.01g/Nm3, dust Content be not more than 50mg/Nm3, the content of benzene is not more than 20mg/Nm3, the content of HCl is not more than 10mg/Nm3.After cooling depickling Gasification gas using the sprinkling of Quench recirculated water, is separated into gasification gas and tar to be clean first, and tar is by Pipeline transport to oil Water separating tank, is separated into tar and waste water；Gasification gas to be clean completes dedusting by wet dedusting tower, and dust therein is removed Enter transverse pipe initial cooler after falling, primary cooler will be removed with two sections of cooling waters of 32 degrees Celsius of recirculated water and 16 degrees Celsius of chilled water To 21 degrees centigrades, the gasification gas discharged by primary cooler bottom enters what two parallel connections were operated simultaneously to gasification air cooling after dirt Electrical tar precipitator, removes the tar carried secretly in gasification gas, obtains the gasification gas of tar and denitration to be desulfurization, is finally roused by Roots again The pneumatic transmission to desulphurization denitration tower that gasifies is completed desulphurization denitration by blower fan, obtains pure gasification gas.
As described above, the system for the treatment of house refuse proposed by the invention has at least one of following advantages：
The system for the treatment of house refuse according to embodiments of the present invention is used as organic waste by using revolving bed pyrolysis oven The equipment of pyrolysis oil preparation, gas and charcoal, completes drying in same stove, and the process of pyrolysis, flow is short, and energy utilization rate is high, It is easy to amplify simultaneously, realizes scale；
The system for the treatment of house refuse according to embodiments of the present invention, high temperature pyrolysis oil gas and the not independent warp of gasification qi leel Cross energy-conservation deacidifying device and realize waste heat recovery and the removing of sour gas, improve energy utilization efficiency, and acid can be mitigated Corrosion of the property gas to equipment；
The system for the treatment of house refuse according to embodiments of the present invention, is gasified raw material by using pyrolytic carbon, generates electricity single The water vapour that unit produces, using recirculating fluidized bed gasification and pyrolysis charcoal, solves that pyrolytic carbon calorific value is low, market outlet as gasifying agent The problem of not smooth and deficiency in economic performance；
The system for the treatment of house refuse according to embodiments of the present invention, by using the high-purity H trapped in pyrolysis gas2With catch High-purity CO of collection2Methyl alcohol is prepared as raw material, carbon emission amount is high during solving the problems, such as garbage treating process；
The system for the treatment of house refuse according to embodiments of the present invention, CO2The rate of recovery up to more than 90%, purity is reachable More than 98%, by by CO2It is preheated to 100-600 degrees Celsius and delivers to methanol synthesis unit again, it is possible to decrease the energy consumption of methanol-fueled CLC, Energy-conservation 10%-20% is realized, and solves CO in the prior art2Discharge capacity is big, and pyrolytic carbon calorific value is low, and market outlet is not smooth, warp The low problem of of poor benefits, resource utilization of helping.
In another aspect of the invention, the present invention proposes a kind of system treatment life using above-mentioned treatment house refuse The method of rubbish living, embodiments in accordance with the present invention, with reference to Fig. 4, the method includes：
S100：House refuse is supplied and is pre-processed into pretreatment unit
In the step, house refuse is supplied and is pre-processed into pretreatment unit, to obtain organic waste and nothing Machine rubbish.Specifically, pre-processed by by house refuse, can be by nothings such as the bulk inorganic matters and metal in house refuse Machine rubbish is removed, the organic waste needed for obtaining next step pyrolysis.It should be noted that pretreatment unit is not particularly restricted, Those skilled in the art can be selected according to actual needs, for example, can include the bag-breaking machine, the roller screening that are sequentially connected Machine, separator and disintegrating machine.Specifically, can be processed by broken bag mechanism, roller screen mechanism and sorting mechanism and remove life rubbish The inorganic matters such as metal, glass, fragment of brick in rubbish, and then crushed house refuse by crushing mechanism.It is of the invention One specific embodiment, after being processed through above-mentioned pretreatment unit, the particle diameter that can obtain meeting revolving bed pyrolysis oven pan feeding requirement is small In the organic waste of 20mm, and the moisture content of organic waste is 20wt%-60wt%.
S200：Organic waste is supplied into pyrolysis installation carries out pyrolysis processing
In the step, organic waste is supplied into pyrolysis installation carries out pyrolysis processing, so as to obtain high temperature pyrolysis oil gas, Pyrolytic carbon and pyrolysis tail gas.It should be noted that pyrolysis installation is not particularly restricted, those skilled in the art can be according to reality Border needs to be selected, for example, can be without heat carrier heat accumulating type rotating bed pyrolysis oven.Specifically, it should be noted that pyrolysis dress Put and be not particularly restricted, those skilled in the art can be selected according to actual needs, for example, can be to be stored without heat carrier Hot type revolving bed pyrolysis oven.Specifically, the organic waste of above-mentioned gained is uniformly delivered into revolving bed pyrolysis oven, layer thickness 50- 250mm, heats up in stove by the stage, completes the reaction for drying, being pyrolyzed and activating, the time that revolving bed pyrolysis oven rotates a circle It is 1h.Wherein, revolving bed pyrolysis oven is the main equipment for realizing the process, it include revolving bed pyrolysis chamber, ring-shaped furnace bottom and The mechanisms, regenerative gas spoke such as the upper and lower heat storage type gas radiation pipe burner of ring-shaped furnace bottom and cloth, discharging are located at respectively Pipe burner arrangement is penetrated in annular furnace wall, the heat needed for refuse pyrolysis are provided in the way of heat radiation.Revolving bed pyrolysis oven edge The direction of rotation is disposed with dry section, the area of pyrolytic reaction one, the area of pyrolytic reaction two and the area of pyrolytic reaction three, pending organic Rubbish enters revolving bed pyrolysis oven from dry section, and high temperature pyrolysis oil gas is provided with the furnace roof of revolving bed pyrolysis oven regional Outlet, for collecting high temperature pyrolysis oil gas, drawing mechanism is provided with the end pyrolytic carbon exit in the area of pyrolytic reaction three, is used for Pyrolytic carbon is collected, in addition, in order that pending organic waste is heated evenly, furnace bottom flitch can select perforated plate.
S300：Pyrolysis tail gas is supplied into collecting carbonic anhydride unit
In the step, pyrolysis tail gas is supplied into collecting carbonic anhydride unit, to obtain carbon dioxide.Need What is illustrated is that collecting carbonic anhydride unit is not particularly restricted, and those skilled in the art can be selected according to actual needs Select, for example, can include the absorption tower, rich solution pump, desorber, reboiler, gas-liquid separator, lean pump and the lean solution that are sequentially connected Cooler.Specifically, the pyrolysis tail gas from pyrolysis installation feeds absorption tower through blower fan pressurization, it is inverse with absorbent in absorption tower Stream contact, the CO in pyrolysis tail gas2Absorbed by absorbent, be changed into rich solution, rich solution feeds desorber, desorption generation CO through rich solution pump2 The mixed gas and lean solution of gas, steam and mist, the CO after desorption2Cooled down through cooler, steam and mist become Cheng Shui and foam, the mixed gas after cooling enter gas-liquid separator, remove water and foam in mixed gas, obtain CO2Gas Body.Wherein, the particular type of absorbent is not particularly restricted, and those skilled in the art can be selected according to actual needs Select, for example, can be alkanolamine solution.
S400：Carbon dioxide and high temperature pyrolysis oil gas are supplied and is exchanged heat and is taken off into the first energy-conservation deacidifying device Acid treatment
In the step, carbon dioxide and high temperature pyrolysis oil gas are supplied into the first energy-conservation deacidifying device and is exchanged heat Processed with depickling, to be pyrolyzed oil gas after carbon dioxide after being preheated and cooling depickling.It should be noted that first segment Energy deacidifying device is not particularly restricted, and those skilled in the art can be selected according to actual needs, for example, can include Depickling mode in inert gas duct, pyrolysis feed channel, two four-way reversing valves, depickling-accumulation of heat complexs, and the step Can be any method that can remove high temperature pyrolysis oil gas middle acid substance in the prior art, those skilled in the art can be with root Selected according to being actually needed.Specifically, the high temperature pyrolysis oil gas from pyrolysis installation is filled through pipeline into the first energy-conservation depickling Completion waste heat recovery and depickling are put, the temperature of high temperature pyrolysis oil gas is down to 200 degrees Celsius, and acidic gas concentration is down to 0.02%. First energy-conservation deacidifying device can be to the high-purity CO that traps2Gas is preheated, the CO after preheating2The temperature of gas is reachable 100-500 degrees Celsius.
S500：Carbon dioxide after preheating and hydrogen are supplied into methanol synthesis unit
In the step, carbon dioxide after preheating and hydrogen are supplied into methanol synthesis unit, to obtain methyl alcohol. It should be noted that methanol synthesis unit is not particularly restricted, those skilled in the art can be selected according to actual needs Select, for example, can include methanol synthesizer and methanol rectifying system.Wherein methanol synthesizer and methanol rectifying system be not It is particularly limited, those skilled in the art can be selected according to actual needs, for example, methanol synthesizer can include gas Change gas reburner and methyl alcohol synthetic reactor, methanol rectifying system can use double-column process, is made up of pre-tower and king-tower.Specifically, CO after preheating2Gas is compressed to 5-7MPa with hydrogen through synthesic gas compressor, and methanol synthesizer, methyl alcohol are then entered together Using one or more in the oxide of copper, zinc and aluminium as catalyst, reaction pressure is 6-9MPa, and reaction temperature is for synthesis 200-300 degrees Celsius, the crude carbinol after synthesis is obtained methyl alcohol by methanol rectifying tower rectifying.
It is according to the above embodiment of the present invention treatment house refuse method by the way that house refuse is pre-processed after supply to Pyrolysis installation carries out pyrolysis processing, to obtain high temperature pyrolysis oil gas, pyrolytic carbon and pyrolysis tail gas；Wherein, pyrolysis tail gas enters Collecting carbonic anhydride unit carries out collecting carbonic anhydride, and then will trap the carbon dioxide for obtaining and supply to the first energy-conservation and take off Heat exchange and depickling treatment are carried out in sour device, so that carbon dioxide is preheated, the carbon dioxide after preheating enters first Alcohol synthesis unit, for synthesizing methanol.Thus, the present processes in the pyrolysis tail gas that is obtained from domestic garbage pyrolysis by carrying Raw material of the carbon dioxide as synthesizing methanol is taken, the recycling of house refuse is realized, while significantly reducing carbon dioxide The discharge of gas, with significant economic benefit and environmental benefit, is particularly well-suited to Technique Popularizing and large-scale production.
Embodiments in accordance with the present invention, with reference to Fig. 5, the method for above-mentioned treatment house refuse is further included：
S600：Pyrolysis oil gas is supplied into pyrolysis oil gas clean unit and carried out at purification after the cooling depickling that S400 is obtained Reason
In the step, pyrolysis oil gas is supplied into pyrolysis oil gas clean unit and carried out only after the cooling depickling that S400 is obtained Change is processed, to obtain pyrolysis oil and pyrolysis gas.It should be noted that pyrolysis oil gas clean unit is not particularly restricted, ability Field technique personnel can be selected according to actual needs, for example, can include the gas wash tower, primary cooler, the electric tar that are sequentially connected Oily device and dry-type desulfurizing tower.A specific embodiment of the invention, after the cooling depickling from the first energy-conservation deacidifying device Pyrolysis oil gas, can realize, to being pyrolyzed dedusting, desulfurization and denitration of oil gas etc. after cooling depickling, making into pyrolysis oil gas clean unit Obtain H2The content of S is not more than 0.01g/Nm3, the content of dust is not more than 50mg/Nm3, the content of benzene is not more than 20mg/Nm3, HCl Content be not more than 10mg/Nm3.Specifically, being pyrolyzed oil gas after cooling depickling first using the sprinkling cooling of Quench recirculated water, separate Into pyrolysis gas to be clean and pyrolysis profit, pyrolysis profit is separated into pyrolysis oil and gives up by Pipeline transport to oil-water separation tank Water；Pyrolysis gas to be clean complete dedusting by wet dedusting tower, and transverse pipe initial cooler is entered after dust therein is removed, just cold Pyrolysis gas after dedusting are cooled to 21 and taken the photograph by device with two sections of cooling waters of 32 degrees Celsius of recirculated water and 16 degrees Celsius of chilled water Family name's degree or so, the pyrolysis gas discharged by primary cooler bottom enter the electrical tar precipitator that two parallel connections are operated simultaneously, remove pyrolysis gas The tar of middle entrainment, obtains the pyrolysis gas of tar and denitration to be desulfurization, and pyrolysis gas finally are delivered into desulfurization by Roots blower again Denitrating tower, completes desulphurization denitration, obtains pure pyrolysis gas.
S700：Pyrolysis gas are supplied into hydrogen capture unit
In the step, pyrolysis gas are supplied into hydrogen capture unit, to obtain hydrogen and combustible gas, and hydrogen is supplied To the methanol synthesis unit in S500.It should be noted that hydrogen capture unit is not particularly restricted, people in the art Member can be selected according to actual needs, for example, can be hydrogen adsorption tower.Specifically, hydrogen pressure-swing absorber is using absorption Agent has different adsorption capacities under different partial pressures to adsorbate, and under certain adsorptive pressure, to separate gas The each component of mixture has the characteristic that selection is adsorbed to carry out purifying hydrogen of hydrogen.Composed in parallel by 4 adsorbent beds in pressure-swing absorber, adsorbed Pressure limit is 1~3MPa, and adsorbent uses activated carbon, and more than 92%, the hydrogen for being trapped can be delivered to hydrogen recovery rate Thus carbon dioxide gas precursor reactant after methanol synthesis unit and preheating, can significantly reduce the original of whole system to prepare methyl alcohol Material cost, improves the economic benefit of whole system.
S800：The combustible gas that the pyrolysis oil and S700 that S600 is obtained are obtained supplies into generator unit combustion power generation
In the step, the combustible gas that the pyrolysis oil and S700 that S600 is obtained are obtained supplies into generator unit burning hair Electricity, to obtain water vapour and combustion tail gas, and combustion tail gas is supplied the collecting carbonic anhydride unit into S300.Specifically Ground, can supply pyrolysis oil and combustible gas to the waste heat boiler of generator unit, be exchanged heat or by combustion with water in waste heat boiler Burn and produce superheated steam, superheated steam to be generated electricity into Steam Turbine Driven generator, the electric energy of generation is connected to the grid, and generates electricity The combustion tail gas that unit is produced can carry out collecting carbonic anhydride utilization into collecting carbonic anhydride unit.
Embodiments in accordance with the present invention, with reference to Fig. 6, the method for above-mentioned treatment house refuse is further included：
S900：Pyrolytic carbon is supplied into breaker carries out break process
In the step, pyrolytic carbon is supplied into breaker carries out break process, to obtain pyrolytic carbon particle.Specifically , after the rubbish charcoal obtained by pyrolysis installation is crushed through breaker, obtain the rubbish charcoal particle of particle diameter no more than 10mm.Inventor It was found that, by before pyrolytic carbon is carried out into gasification process, pyrolytic carbon being crushed into the particle diameter in advance, gasification can be significantly improved The efficiency for the treatment of simultaneously reduces the energy consumption of gasification process.
S1000：The water vapour that pyrolytic carbon particle and S800 are obtained is supplied into gasification installation carries out gasification process
In the step, the water vapour that pyrolytic carbon particle and S800 are obtained is supplied into gasification installation carries out gasification process, To obtain gasify gas and residue after gasifying.It should be noted that gasification installation is not particularly restricted, those skilled in the art can To be selected according to actual needs, for example, it can be circle fluidized-bed gasification furnace.Specifically, particle diameter will be crushed to being not more than The pyrolytic carbon particle of 10mm as gasified raw material by press device and pipeline to circle fluidized-bed gasification furnace, vapor with Pyrolytic carbon particle enters circle fluidized-bed gasification furnace and gasifies jointly, and gasification temperature is 1000 degrees centigrades, obtains gasify gas, gas Change residue because value is relatively low, construction material or landfill disposal can be done.
S1100：Gasification gas is supplied into the second energy-conservation deacidifying device carries out heat exchange and depickling treatment
In the step, gasification gas is supplied into the second energy-conservation deacidifying device carries out heat exchange and depickling treatment, to obtain Gasify gas after cooling depickling.It should be noted that the second energy-conservation deacidifying device can be same as the first energy-conservation depickling of foregoing description Apparatus structure.Specifically, come the gasification gas of self-gasifying device through pipeline enter the second energy-conservation deacidifying device complete waste heat recovery and Depickling, gasifies gas after obtaining cooling depickling, and the temperature of the gas that gasifies after cooling depickling is down to 200-350 degrees Celsius, and sour gas is dense Degree is down to 0.02%-0.05%.
S1200：The gas that will gasify after cooling depickling is supplied and carries out purified treatment into gasification gas clean unit
In the step, the gas that will gasify after cooling depickling is supplied and carries out purified treatment into gasification gas clean unit, so as to To purification gasification gas, and purification gasification gas is back to the pyrolysis installation in S200.It should be noted that gasification gas clean unit It is not particularly restricted, those skilled in the art can be selected according to actual needs, for example, can includes what is be sequentially connected Gas wash tower, primary cooler and dry-type desulfurizing tower.Gasify gas after cooling depickling from the second energy-conservation deacidifying device, net into gasification gas Changing unit can realize to dedusting, desulfurization and denitration of gasification gas etc. after cooling depickling so that wherein H2The content of S is not more than 0.01g/Nm3, the content of dust is not more than 50mg/Nm3, the content of benzene is not more than 20mg/Nm3, the content of HCl is not more than 10mg/ Nm3.Gas gasify after cooling depickling first using the sprinkling of Quench recirculated water, gasification gas and tar to be clean, tar warp is separated into Pipeline transport to oil-water separation tank is crossed, tar and waste water is separated into；Gasification gas to be clean completes dedusting by wet dedusting tower, Enter transverse pipe initial cooler, primary cooler 32 degrees Celsius of recirculated water and 16 degrees Celsius of chilled water after dust therein is removed Gasification air cooling after dedusting to 21 degrees centigrades, the gasification gas discharged by primary cooler bottom are entered two by two sections of cooling waters The electrical tar precipitator of operation simultaneously in parallel, removes the tar carried secretly in gasification gas, obtains the gasification gas of tar and denitration to be desulfurization, It is last to complete desulphurization denitration again by Roots blower by the pneumatic transmission to desulphurization denitration tower that gasifies, obtain pure gasification gas.
Below with reference to specific embodiment, present invention is described, it is necessary to explanation, these embodiments are only description Property, and the present invention is limited never in any form.
Embodiment
It is raw material to use certain city's house refuse, and it is as shown in table 1 into being grouped into.
The house refuse of table 1 is into being grouped into (wt%)
With reference to Fig. 7, then above-mentioned house refuse is crushed by simple sorting removal bulk inorganic matter and metal, is broken The broken particle diameter for being met revolving bed pyrolysis oven pan feeding requirement is the organic waste of 20wt%-60wt% less than 20mm, moisture content； Organic waste is uniformly fed revolving bed pyrolysis oven, fabric thickness about 100mm, and rubbish is dry with rotating through for furnace bottom in stove Dry, pyrolysis, activation complete reaction, and wherein dry section temperature is 350 degrees Celsius, and pyrolysis zone temperature is 800 degrees Celsius, region of activation temperature It is 900 degrees Celsius to spend, reaction time 1h, obtains high temperature pyrolysis oil gas, pyrolytic carbon and pyrolysis tail gas.It is pyrolyzed the composition such as table of tail gas Shown in 2.
The exhaust gas component of table 2 is constituted
Pyrolysis tail gas from pyrolysis installation feeds absorption tower through blower fan pressurization, with absorbent alkanolamine solution in absorption tower Counter current contacting, the CO in pyrolysis tail gas2Absorbed by absorbent, be changed into rich solution, rich solution feeds desorber, desorption generation through rich solution pump CO2The mixed gas and lean solution of gas, steam and mist, the CO after desorption2Cooled down through cooler, steam and mist Become water and foam, the mixed gas after cooling enter gas-liquid separator, remove water and foam in mixed gas, obtain CO2 Gas.High temperature pyrolysis oil gas from pyrolysis installation enters the first energy-conservation deacidifying device and completes waste heat recovery and depickling through pipeline, The temperature of high temperature pyrolysis oil gas is down to 200 degrees Celsius, and acidic gas concentration is down to 0.02%.First energy-conservation deacidifying device can be to catching The high-purity CO for collecting2Gas is preheated, the CO after preheating2The temperature of gas is up to 100-500 degrees Celsius.CO after preheating2 Gas and hydrogen are compressed to 5-7MPa through synthesic gas compressor, then enter methanol synthesizer together, methanol-fueled CLC using copper, Used as catalyst, reaction pressure is 8.1MPa to one or more in the oxide of zinc and aluminium, and reaction temperature is 280 degrees Celsius, Crude carbinol after synthesis is obtained methyl alcohol by methanol rectifying tower rectifying, and yield is 3t/h, methyl alcohol after rectifying purity up to 97%. CO2The rate of recovery up to more than 90%, purity is up to more than 98%, while the energy consumption of methanol-fueled CLC can be reduced, realizes energy-conservation 10%- 20%, solve CO in the prior art2Discharge capacity is big, deficiency in economic performance and the low problem of resource utilization.
Oil gas is pyrolyzed after cooling depickling from the first energy-conservation deacidifying device, it is right to be realized into pyrolysis oil gas clean unit Dedusting, desulfurization and denitration of oil gas etc. are pyrolyzed after cooling depickling so that H2The content of S is not more than 0.01g/Nm3, the content of dust No more than 50mg/Nm3, the content of benzene is not more than 20mg/Nm3, the content of HCl is not more than 10mg/Nm3.Specifically, cooling depickling Pyrolysis oil gas is separated into pyrolysis gas and tar to be clean first using the sprinkling cooling of Quench recirculated water afterwards, and tar is by pipeline Oil-water separation tank is delivered to, tar and waste water is separated into；Then pyrolysis gas to be clean complete dedusting in wet dedusting tower, will Dust therein enters transverse pipe initial cooler after removing, primary cooler is with the two of 32 degrees Celsius of recirculated water and 16 degrees Celsius of chilled water Section cooling water will lower the temperature depickling after pyrolysis gas be cooled to 21 degrees centigrades, after the cooling depickling discharged by primary cooler bottom being pyrolyzed Gas enters the electrical tar precipitator that two parallel connections are operated simultaneously, and the tar carried secretly in pyrolysis gas after removing cooling depickling is pyrolyzed Pyrolysis gas are finally delivered to desulphurization denitration tower by the pyrolysis gas of oily and to be desulfurization denitration by Roots blower again, complete desulphurization denitration, Obtain cleaning pyrolysis gas.The constituent and calorific value of pyrolysis gas are as shown in table 3.
The pyrolysis gas of table 3 are constituted and calorific value
, again through pressure-swing absorber absorption to trap hydrogen, hydrogen pressure-swing absorber is using adsorbent in different partial pressures for pyrolysis gas Under have different adsorption capacities to adsorbate, and under certain adsorptive pressure, each group of the admixture of gas to separate Part has the characteristic that selection is adsorbed to carry out purifying hydrogen of hydrogen.Composed in parallel by 4 adsorbent beds in pressure-swing absorber, adsorptive pressure scope is 1 ~3MPa, adsorbent uses activated carbon, and more than 92%, purity is up to more than 94%, the hydrogen for being trapped for hydrogen recovery rate Carbon dioxide gas precursor reactant after methanol synthesis unit being delivered to and being preheated is to prepare methyl alcohol.
Above-mentioned pyrolysis oil and combustible gas are used to generate electricity, the economic benefit of system, the combustion tail gas of gained is remarkably improved Can be supplied to collecting carbonic anhydride unit be used to trap carbon dioxide again, so that as the raw material of production methyl alcohol.
After rubbish charcoal obtained by pyrolysis installation is crushed through breaker, the rubbish charcoal particle of particle diameter no more than 10mm is obtained. The pyrolytic carbon particle that particle diameter no more than 10mm will be crushed to passes through press device and pipeline to recycle stream as gasified raw material Change bed gasification furnace, vapor enters circle fluidized-bed gasification furnace with pyrolytic carbon particle and gasifies jointly, and gasification temperature is 1000 Celsius Degree left and right, obtains the gas that gasifies, and residue after gasifying is relatively low due to value, can do construction material or landfill disposal.Pyrolytic carbon is converted Up to more than 97%, gasification gas calorific value reaches 2670Kcal/Nm to rate3, gasify gas constituent and calorific value it is as shown in table 4.
The gasification gas composition of table 4 and calorific value
The gasification gas for carrying out self-gasifying device enters the second energy-conservation deacidifying device completion waste heat recovery and depickling through pipeline, obtains Gasify gas after cooling depickling, and the temperature of the gas that gasifies after cooling depickling is down to 200-350 degrees Celsius, and acidic gas concentration is down to 0.02%-0.05%.Gasify gas after cooling depickling from the second energy-conservation deacidifying device, can be realized into gasification gas clean unit Dedusting, desulfurization and denitration to the gas that gasifies after cooling depickling etc. so that wherein H2The content of S is not more than 0.01g/Nm3, dust Content is not more than 50mg/Nm3, the content of benzene is not more than 20mg/Nm3, the content of HCl is not more than 10mg/Nm3.Gas after cooling depickling Change gas first using the sprinkling cooling of Quench recirculated water, be separated into gasification gas and tar to be clean, tar by Pipeline transport extremely Oil-water separation tank, is separated into tar and waste water；Then gasification gas to be clean complete dedusting in wet dedusting tower, will be therein Dust enters transverse pipe initial cooler after removing, primary cooler is cooled down with two sections of 32 degrees Celsius of recirculated water and 16 degrees Celsius of chilled water Water will lower the temperature and gasify air cooling to 21 degrees centigrades after depickling, and gasify gas after the cooling depickling finally discharged by primary cooler bottom The pneumatic transmission to desulphurization denitration tower that gasifies after cooling depickling is completed into desulphurization denitration by Roots blower again, obtains cleaning the gas that gasifies, only Change gasification gas and may return to fuel of the pyrolysis installation as pyrolysis.
In the description of this specification, reference term " one embodiment ", " some embodiments ", " example ", " specifically show The description of example " or " some examples " etc. means to combine specific features, structure, material or spy that the embodiment or example are described Point is contained at least one embodiment of the invention or example.In this manual, to the schematic representation of above-mentioned term not Identical embodiment or example must be directed to.And, the specific features of description, structure, material or feature can be with office Combined in an appropriate manner in one or more embodiments or example.Additionally, in the case of not conflicting, the skill of this area Art personnel can be tied the feature of the different embodiments or example described in this specification and different embodiments or example Close and combine.
Although embodiments of the invention have been shown and described above, it is to be understood that above-described embodiment is example Property, it is impossible to limitation of the present invention is interpreted as, one of ordinary skill in the art within the scope of the invention can be to above-mentioned Embodiment is changed, changes, replacing and modification.

Claims (6)

1. it is a kind of process house refuse system, it is characterised in that including：
There is pretreatment unit, the pretreatment unit house refuse entrance, organic waste outlet and inorganic refuse to export；
Pyrolysis installation, the pyrolysis installation has organic waste entrance, high temperature pyrolysis oil gas vent, pyrolytic carbon outlet and pyrolysis tail Gas is exported, and the organic waste entrance is connected with organic waste outlet；
Collecting carbonic anhydride unit, the collecting carbonic anhydride unit has gas inlet and carbon dioxide gas outlet, described Gas inlet is connected with the pyrolysis offgas outlet；
There is first energy-conservation deacidifying device, the first energy-conservation deacidifying device high temperature pyrolysis oil gas entrance, carbon dioxide to enter Mouthful, cooling depickling after be pyrolyzed oil gas vent and preheating after carbon dioxide gas outlet, the carbon dioxide entrance with it is described Carbon dioxide gas outlet is connected, and the high temperature pyrolysis oil gas entrance is connected with the high temperature pyrolysis oil gas vent；
Methanol synthesis unit, carbon dioxide entrance and methyl alcohol go out after the methanol synthesis unit has hydrogen inlet, preheating Mouthful, carbon dioxide entrance is connected with carbon dioxide gas outlet after the preheating after the preheating.
2. system according to claim 1, it is characterised in that further include：
Pyrolysis oil gas clean unit, the pyrolysis oil gas clean unit goes out with pyrolysis oil gas entrance, pyrolysis oil after cooling depickling Mouth and pyrolysis gas outlet, are pyrolyzed oil gas entrance and are connected with pyrolysis oil gas vent after the cooling depickling after the cooling depickling；
There is hydrogen capture unit, the hydrogen capture unit pyrolysis gas entrance, hydrogen outlet and combustible gas to export, the pyrolysis Gas entrance is connected with the pyrolysis gas outlet, and the hydrogen outlet is connected with the hydrogen inlet；
There are generator unit, the generator unit fuel inlet, steam outlet and combustion tail gas to export, the fuel inlet point It is not connected with the pyrolysis oil export and combustible gas outlet, the combustion tail gas outlet is connected with the gas inlet.
3. system according to claim 1 and 2, it is characterised in that further include：
Breaker, the breaker has pyrolytic carbon entrance and a pyrolytic carbon particle outlet, the pyrolytic carbon entrance with it is described Pyrolytic carbon outlet is connected；
There is gasification installation, the gasification installation pyrolytic carbon particle entrance, steam entry, the outlet of gasification gas and residue after gasifying to go out Mouthful, the pyrolytic carbon particle entrance is connected with the pyrolytic carbon particle outlet, the steam entry and the steam outlet It is connected；
Second energy-conservation deacidifying device, gasification gas goes out after the second energy-conservation deacidifying device has gasification gas entrance and cooling depickling Mouthful, the gasification gas entrance is connected with the gasification gas outlet；
Gasification gas clean unit, the gasification gas clean unit goes out with gasification gas entrance after cooling depickling and purification gasification gas Mouthful, the gas entrance that gasifies after the cooling depickling is connected with gas outlet of gasifying after the cooling depickling, the purification gasification gas outlet It is connected with the pyrolysis installation.
4. the method that the system any one of a kind of use claim 1-3 processes house refuse, it is characterised in that bag Include：
(1) house refuse is supplied into the pretreatment unit and is pre-processed, to obtain organic waste and inorganic refuse；
(2) supplying the organic waste carries out pyrolysis processing into the pyrolysis installation, to obtain high temperature pyrolysis oil air and heat Solution charcoal and pyrolysis tail gas；
(3) the pyrolysis tail gas is supplied into the collecting carbonic anhydride unit, to obtain carbon dioxide；
(4) carbon dioxide and the high temperature pyrolysis oil gas are supplied into the first energy-conservation deacidifying device and is changed Heat and depickling treatment, to be pyrolyzed oil gas after carbon dioxide after being preheated and cooling depickling；
(5) carbon dioxide after the preheating and hydrogen are supplied into the methanol synthesis unit, to obtain methyl alcohol.
5. method according to claim 4, it is characterised in that further include：
(6) after the cooling depickling for obtaining step (4) be pyrolyzed oil gas supply to it is described pyrolysis oil gas clean unit in carry out Purified treatment, to obtain pyrolysis oil and pyrolysis gas；
(7) pyrolysis gas are supplied into the hydrogen capture unit, to obtain hydrogen and combustible gas, and by the hydrogen Supply to the methanol synthesis unit in step (5)；
(8) combustible gas that the pyrolysis oil and step (7) for obtaining step (6) are obtained is supplied into the generator unit The combustion tail gas to obtain water vapour and combustion tail gas, and are supplied the titanium dioxide into step (3) by combustion power generation Carbon capture unit.
6. method according to claim 5, it is characterised in that further include：
(9) supplying the pyrolytic carbon carries out break process into the breaker, to obtain pyrolytic carbon particle；
(10) water vapour that the pyrolytic carbon particle and step (8) are obtained is supplied into the gasification installation and is gasified Treatment, to obtain gasify gas and residue after gasifying；
(11) supplying into the second energy-conservation deacidifying device the gasification gas carries out heat exchange and depickling treatment, to be dropped Gasify gas after warm depickling；
(12) gas that will gasify after the cooling depickling is supplied and carries out purified treatment into the gasification gas clean unit, to obtain Purification gasification gas, and the purification gasification gas is back to the pyrolysis installation in step (2).
CN201710154376.1A 2017-03-15 2017-03-15 The system and method for processing house refuse Pending CN106862242A (en)

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Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN109679672A (en) * 2019-01-31 2019-04-26 华南理工大学 A kind of reaction system and its method of catalytic pyrolysis organic solid castoff preparing gas fuel
WO2023029151A1 (en) * 2021-09-03 2023-03-09 山东大学 Method and system for realizing cyclic utilization of carbon‐hydrogen by using organic wastes
CN116066831A (en) * 2022-12-27 2023-05-05 博耐特瑞(北京)环保科技有限公司 Garbage disposal system and method

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN109679672A (en) * 2019-01-31 2019-04-26 华南理工大学 A kind of reaction system and its method of catalytic pyrolysis organic solid castoff preparing gas fuel
WO2023029151A1 (en) * 2021-09-03 2023-03-09 山东大学 Method and system for realizing cyclic utilization of carbon‐hydrogen by using organic wastes
CN116066831A (en) * 2022-12-27 2023-05-05 博耐特瑞(北京)环保科技有限公司 Garbage disposal system and method

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