CN108409530A - Organic waste produces the device and method of low carbon mixed alcohol - Google Patents

Organic waste produces the device and method of low carbon mixed alcohol Download PDF

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CN108409530A
CN108409530A CN201810193052.3A CN201810193052A CN108409530A CN 108409530 A CN108409530 A CN 108409530A CN 201810193052 A CN201810193052 A CN 201810193052A CN 108409530 A CN108409530 A CN 108409530A
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gas
synthesis
section
synthesis gas
organic waste
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CN108409530B (en
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吴辉胜
钱丰
刘安平
蒋红光
覃文斌
钟土生
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    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
    • C07C29/15—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively
    • C07C29/151—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases
    • C07C29/1516—Multisteps
    • C07C29/1518—Multisteps one step being the formation of initial mixture of carbon oxides and hydrogen for synthesis
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/06—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B32/00—Carbon; Compounds thereof
    • C01B32/05—Preparation or purification of carbon not covered by groups C01B32/15, C01B32/20, C01B32/25, C01B32/30
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
    • C07C29/15—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively
    • C07C29/151—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases
    • C07C29/152—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases characterised by the reactor used
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
    • C07C29/15—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively
    • C07C29/151—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases
    • C07C29/153—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases characterised by the catalyst used
    • C07C29/154—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases characterised by the catalyst used containing copper, silver, gold, or compounds thereof
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
    • C07C29/15—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively
    • C07C29/151—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases
    • C07C29/153—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases characterised by the catalyst used
    • C07C29/156—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases characterised by the catalyst used containing iron group metals, platinum group metals or compounds thereof
    • 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
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
    • Y02E60/30—Hydrogen technology
    • Y02E60/36—Hydrogen production from non-carbon containing sources, e.g. by water electrolysis
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/141—Feedstock
    • Y02P20/145—Feedstock the feedstock being materials of biological origin

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Inorganic Chemistry (AREA)
  • Health & Medical Sciences (AREA)
  • General Health & Medical Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Processing Of Solid Wastes (AREA)

Abstract

The invention discloses the device and method that organic waste produces low carbon mixed alcohol, which includes organic castoff heat cracking charing section, synthesis gas preparation section, catalyzes and synthesizes section.Production method is that organic waste is first carried out thermal cracking carbonization reaction to generate charcoal；Charcoal milling is sized mixing again, carrying out pressurized gasification in gasifier with compressed air, high steam reacts, and generates CO, H2、CO2And other synthesis gas, it is adjusted using gas, controls H2It is 1 with CO molar ratios:1.2~2.5；It is transported to after purified synthesis gas and catalyzes and synthesizes workshop section；Synthesis gas carries out catalyzing and synthesizing effect under the action of catalyst, generates first, ethyl alcohol and the thick mixed alcohol of other alcohol, using decompression, flash distillation impurity elimination, isolated mixed alcohol product.The present invention not only solves the problems, such as garbage loading embeading minimizing, innoxious, realization recycling organic waste is turned waste into wealth, while reducing the production cost of the low carbon mixed alcohols such as methanol, ethyl alcohol using discarded organic matter as the raw materials for production of low-carbon alcohols.

Description

Organic waste produces the device and method of low carbon mixed alcohol
Technical field
The present invention is to belong to organic waste treatment and mixed alcohol production technical field, is particularly related to using organic The method that waste makees raw material production mixed alcohol.
Background technology
For a long time, to the processing of house refuse, mainly dissolved with finding solution space, most cities still with Simple landfill is main processing ways (accounting for about 80% or so), followed by During High-Temperature Composting (accounting for about 5%-10%), burns mode (about Account for 10%-15%).China year generates about 2.3 hundred million tons of quantity of refuse at present, and with the speed increase in year 8%~10%, 70% city County is absorbed in the predicament of garbage-surrounded city.And the quantity of refuse for having filled stockpiling has more than 8,000,000,000 tons, for a long time by stockpiling rubbish appropriation of land face Product is up to more than 700,000,000 square metre.Also, also to produce the incremental stockpiling of speed landfill of 1.8 hundred million tons of quantity of refuse, the state of flood tide preciousness per year Soil resource is occupied pollution for a long time.
The city of the fast development of current national economy, each city in the whole nation is all being expanded rapidly, is located in remote location originally Refuse landfill, it is now to have become prime location or close to city more, some be also in factory, residential quarter encirclement among.These Harmful substance and gas caused by rubbish cause fire, surface water pollution, groundwater resources pollution, air pollution, give the people Bring the security risk of life, property.
Three kinds of processing modes that garbage disposal at present generally uses：
1, it fills：Contain heavy metal and poisonous and hazardous organic chemical pollutant, Escherichia coli in the percolate of rubbish Deng viral germ, after the water that permeates the ground, easily causes water resource and seriously pollute.
2, it burns：A large amount of solid suspension and the smaller dust particles of diameter are formed, gray haze is caused, it is even more serious It is to generate " dioxin " carcinogenic gas.In the world, garbage burning factory is acknowledged as most dangerous pollution sources.
3, compost：Existing composting technology by microorganism species ferment in the way of degrade and sort after organic matter and first compost. Metal class and battery battery plate through a long time fermentation corruption harmful toxins seriously immerse in rubbish, lead to a fertilizer product oxious component huge sum of money Belong to and severely exceeding.
Landfill burns, and all there is serious shortcomings for compost.Therefore, how to realize organic waste minimizing, it is innoxious, The processing of recycling just by there is an urgent need to.
Methanol is particularly important basic organic chemical raw material, the industries such as chemical industry, medicine, light industry, weaving and transport all It is widely used, derivative product development prospect is wide.In Chemical Manufacture, methanol can be used for manufacturing formaldehyde, acetic acid, chlorine Methane, methylamine, methyl tertiary butyl ether(MTBE) (fuel additive mtbe), polyvinyl alcohol (pva), dimethyl suflfate, terephthalic acid (TPA) two Methyl esters (dmt), dimethyl ether, methyl acrylate, methacrylic acid methanol etc..The raw material of production methanol generally uses coal or day now Right gas, production cost is high, pollutes environment.
Ethyl alcohol has many uses too, and acetic acid, beverage, essence, dyestuff, fuel etc. can be manufactured with ethyl alcohol.Medically also commonly use The ethyl alcohol that volume fraction is 70%~75% makees disinfectant etc., in national defence chemical industry, health care, food industry, industrial and agricultural production In all have been widely used.Ethyl alcohol is produced generally with amyloid agricultural product, such as cereal, potato or wild plant fruit, The blackstrap of sugar refinery can be used, or use cellulose-containing sawdust, plant haulm etc. as raw material, after certain pretreatment, Fermentation, distillation can be prepared by ethyl alcohol.Or using coal based synthetic gas as raw material, through methanol, Dimethyl ether carbonylation, hydrogenation synthesis second Alcohol.The problems such as equally existing production cost height, polluting environment.
Garbage waste material how to be efficiently used to produce the mixed alcohols such as methanol, ethyl alcohol, rubbish conversion processing will be provided New approaches turn waste into wealth, and reduce environmental pollution hidden danger, are also of great significance to the people's livelihood.
Invention content
The object of the present invention is to provide a kind of methods producing mixed alcohol as raw material using organic waste, solve garbage loading embeading Minimizing, innoxious problem, recycling organic waste are turned waste into wealth, while reducing the production cost of methanol, ethyl alcohol, But also as energy fuel.
The purpose of the present invention is achieved through the following technical solutions.
Organic waste produces the device of low carbon mixed alcohol comprising organic waste thermal cracking carbonizes section, synthesis gas system Standby section catalyzes and synthesizes section.Below construction explanation is carried out according to technological process:
1, thermal cracking carbonizes section：Including reaction system, heating system and piece-rate system.Specific configuration is as follows：
(1) reaction system includes feeder, cracking reactor, vacuum pump, discharging conveyer.The feeder passes through pipeline It is connected with the feed inlet of cracking reactor, the discharge nozzle of cracking reactor is connected with discharging conveyer, discharging conveyer and synthesis The flour mill that gas prepares section is connected by pipeline.Automatic grate is provided in cracking reactor, velocity of rotation control raw material exists Reaction time in pyrolysis reactor.Cracking reactor is connected with vacuum pump, is kept in pyrolysis reactor by vacuum pump Negative pressure, vacuum pump outlet connect with piece-rate system.
(2) heating system includes fused salt heating furnace, cracking reactor and molten salt circulating pump.Fused salt heating furnace to go out heat pipe straight It connects and is connect with cracking reactor, the fused salt outlet of cracking reactor is connect by molten salt circulating pump with fused salt heating furnace, and heat is formed Cycle.
(3) piece-rate system includes heavy oil condenser, light-water condenser, technique water pump, petroleum pump, fixed gas pump.Vacuum pump Outlet after be connected successively with heavy oil condenser and light-water condenser, the condensate pipe of light-water condenser is defeated by technique water pump It is sent to the flour mill that synthesis gas prepares workshop section；The fixed gas pipe of light-water condenser is pumped by fixed gas and is connect with fused salt heating furnace. The condenser pipe of heavy oil condenser is connect by petroleum pump with fused salt heating furnace.
As the further preferred of technical solution, dry materials device is added before the feeder of reaction system.Drier with Feeder, the gas outlet of fused salt heating furnace are connected.
2, synthesis gas prepares section：Including gasification system, purification system.Specific configuration is as follows：
(1) gasification system includes flour mill, charcoal slurry tank, charcoal stock pump, gasifier and grey pulp separator.Flour mill starches tank with charcoal It is connected；Charcoal slurry tank is connected by charcoal stock pump with gasifier, and gasifier is equipped with compressed air inlet and high pressure steam inlet, gasification The escape pipe of device is connected with grey pulp separator, and the slag notch of gasifier is connected with fixed-end forces system.The gas phase of grey pulp separator Outlet adjusts pipe with adjuster and gas phase by three-way connection and connect, residue outlet and the fixed-end forces system phase of grey pulp separator Even.Gas phase adjustment pipe with catalyze and synthesize section and be connected.
(2) purification system：Including adjuster, synthesic gas compressor, purifying, preheating device, synthesis gas gas-liquid separator, purification Filter and CO2Absorption tower.Adjuster is connect by synthesic gas compressor with purifying, preheating device；The escape pipe of purifying, preheating device according to Secondary and synthesis gas gas-liquid separator, polishing filter and CO2Absorption tower connects；CO2The top gas phase outlet on absorption tower passes through purification Preheater connect after being exchanged heat with gas phase adjustment pipe, and gas phase adjustment manages and catalyzes and synthesizes section and connect.
It further includes absorbent transport system that the synthesis gas, which prepares section, comprising high pressure flash fills, atmospheric flashing fills, absorbs Agent circulating pump, absorbent force (forcing) pump, high pressure liquid heater, absorbent heat exchanger；Fresh absorbent delivery pipe is filled with atmospheric flashing It is connected with absorbent circulating pump, absorbent circulating-pump outlet is connect with absorbent heat exchanger, and absorbent heat exchanger passes through absorbent Force (forcing) pump is connected to CO2Absorption tower top；CO2The absorbent sewer pipe of absorb the bottom of the tower is filled with high pressure flash successively, absorbent changes Hot device, high pressure liquid heater, atmospheric flashing fill connection, and atmospheric flashing filling is connect with absorbent circulating pump by pipeline.
3, section is catalyzed and synthesized：Including synthesis air preheater, reaction gas heat exchanger, reaction start heater, synthesis reactor, Boiler water- to-water heat exchanger, product cooler, high-pressure gas-liquid separator, low-pressure gas-liquid separator.
Synthesis air preheater is connected with reaction gas heat exchanger, then reacted startup heater is connected with synthesis reactor, closes High-pressure gas-liquid is connected to after reacted gas heat exchanger, boiler water- to-water heat exchanger and product cooler successively at the escape pipe of reactor Separator, high-pressure gas-liquid separator are connect with low-pressure gas-liquid separator again, and outlet and the mixed alcohol of low-pressure gas-liquid separator store up Tank connects.
As the further preferred of technical solution, it further includes middle pressure steam packet, sucking filling, cycle compressor to catalyze and synthesize section Machine.Middle pressure steam packet is bi-directionally connected with synthesis reactor, then in synthesis reactor in the heated vaporization of moisture and middle pressure steam packet Vapor-liquid separation constitutes thermal siphon Natural Circulation, removes reaction heat.It contracts for fixed output quotas to synthetic reaction process units initial operating stage middle pressure steam Raw low-pressure steam is pressurized using steam mechanical recompression MVR technologies, and (pressure is more than generated middle pressure steam 0.4MPa is less than 0.8MPa) it is incorporated to middle pressure steam pipe network, a large amount of emptying of device initial operating stage steam are avoided, it is effective real Existing Waste Heat Reuse.
Recycle gas compressor is added before synthesis gas preheater pipeline.The gas of high-pressure gas-liquid separator and low-pressure gas-liquid separator Xiang Guanyu suckings fill, the purification system of synthesis gas preparation section is connected, and suck to fill and be connected with recycle gas compressor, are formed back Road recycles.
The purpose is to：It is secondary anti-also to contain propyl alcohol, butanol etc. in addition to containing purpose product methanol, ethyl alcohol for gas after reaction Answer product.Since during catalyzing and synthesizing, conversion per pass is relatively low, therefore a large amount of unreacted synthesis gas must recycle and make With.Reaction gas reacted gas heat exchanger cooling first, and after further condensed through boiler water heat exchanger, product cooler, it is cold Solidifying temperature is 55~60 DEG C, and gas-liquid two-phase is directly entered high-pressure gas-liquid separator without isolation after condensation, and the high pressure after separation is anti- It answers gas to enter recycle compressor suction tank and makees recyclegas, liquid enters low-pressure gas-liquid separator, the low pressure reaction after separation Gas also makees recyclegas into recycle compressor suction tank, and liquid is mixed alcohol, removes mixed alcohol storage tank.
To prevent reduction synthetic gas density after the accumulation of the on-condensible gases such as nitrogen and carbon dioxide from influencing being smoothed out for reaction, A part of sidestream gas is extracted out from high-pressure gas-liquid separator outlet circulating air to be purified, and carbon dioxide and other impurities are removed Gas return system afterwards recycles.Side stream gas enters purification system from synthesic gas compressor entrance.
The method of the organic waste production low carbon mixed alcohol of the present invention comprising following steps:
(1) thermal cracking carbonizes, and cracking reactor is transported to after organic waste is fed and carries out thermal cracking carbonization reaction, instead Answer condition be 8~22KPa of vacuum degree, oxygen-free environment, 420~650 DEG C of reaction temperature, the reaction time be 1.5~4.5 hours to obtain the final product To charcoal, the generation raw material as synthesis gas；
(2) prepared by synthesis gas, and charcoal is transported to the charcoal that charcoal slurry tank is adjusted to a concentration of 80~85% after milling Water slurry, then be transferred in gasifier carries out pressurized gasification with compressed air and high steam and reacts, and reaction pressure is 2.8~ 8.7MPa, 1250~1400 DEG C of reaction temperature, gasification generate CO, H2、CO2And other synthesis gas pass through grey pulp separator into one Step removes solid, liquid waste, and processed synthesis gas is adjusted by gas, controls H2It is 1 with CO molar ratios:1.2~2.5；And it is right Synthesis gas is purified, and is finally transported to and is catalyzed and synthesized workshop section；
(3) it catalyzes and synthesizes, synthesis gas is pressurized to 10~12MPa by compressor, enters back into synthesis reactor, in temperature It at 280~350 DEG C, carries out catalyzing and synthesizing effect under the action of catalyst, 2000~5000h of volume space velocity is calculated with dry gas-1, raw At first, ethyl alcohol and the thick mixed alcohol of other alcohol, most of gas of thick mixed alcohol is removed by depressurizing, flashing, is finally separating out The mixed alcohol product come is transported to mixed alcohol storage tank.
The present invention catalyst be mixing Co -- Mo catalyst, Snam companies withThe MAS techniques that company develops jointly Alkaline assistant is modified ZnO/Cr2O3Catalyst, the Octamix technique Cu-Zn catalyst of Lurgi companies exploitation, french petroleum science The IFP technique Cu-Co catalyst of research institute (IFP) exploitation, the Sygmol techniques MoS of Dow Chemical Company exploitation2In catalyst One or more combination.
As the further preferred of technical solution, the catalyst is mixing Co -- Mo catalyst, modified ZnO/Cr2O3Catalysis Agent, Cu-Zn catalyst, Cu-Co catalyst, MoS2Two kinds of combinations in catalyst, it is 1 to match:0.2~1.0.
As the further preferred of technical solution, under existing catalyst action, section can be prepared by H in synthesis gas2With CO molar ratios are adjusted to 1:2.0~2.5.
As the further preferred of technical solution, organic waste is first dried before entering feeder to 15% or less water content And crush, then feed.
The reaction principle of the present invention：
C+H2O─H2+CO (i)
CO+H2O─H2+CO2 (ii)
CO+2H2─CH3OH (iii)
CH3OH+2H2+CO─C2H5OH+H2O (iv)
C2H5OH+2H2+CO─C3H7OH+H2O (v)
CO2+3H2─CH3OH+H2O (vi)
In conjunction with the device of the invention, concrete technology flow process is illustrated：
1, thermal cracking carbonizes section
Raw material is sorted by pretreatment, and removal inorganic matter, metal impurities are dried into drier, after dries pulverizing by Feeder delivers into pyrolysis reactor and carries out thermal cracking carbonization reaction, during which leakproofness is controlled by valve group, by vacuum pump It keeps being reaction pressure in pyrolysis reactor.It is anti-to control by controlling Automatic grate velocity of rotation in pyrolysis reactor Between seasonable, raw material is driven and stirred, the charcoal that reaction generates is brought to reactor outlet, synthesis gas is sent to by discharging conveyer Prepare section.
It reacts the gas generated and liquid all pumps piece-rate system with gas phase by vacuum pump, it is cold to pass through heavy oil successively Condenser and light-water condenser, the non-condensable gas that the bio-fuel-oil and light-water condenser that heavy oil condenser condenses out come out are led back Heating furnace burning utilizes；The process water that light-water condenser condenses out, which is then transported in the flour mill of synthesis gas workshop section, carries out profit With.
Fused salt is heated by fuel oil combustion when fused salt heating furnace starts, the heavy oil component that is generated by reaction after normal operation and Fixed gas combustion heating fused salt, tail gas remove drier drying material, go exhaust-gas treatment later, the fused salt of heating is by molten salt circulating pump Pumping circulation.
2, synthesis gas prepares section
Charcoal enters flour mill with process water and wears into charcoal slurry, and the concentration of charcoal water slurry is stored and adjust into charcoal slurry tank, Gasifier is sent by charcoal stock pump again, while being mixed into compressed air and high steam.Charcoal slurry is reacted in gasifier, and gasification generates CO、H2、CO2Etc. mixed gas, mixed gas enter grey pulp separator and remove solid, liquid waste, it is further anti-then to enter adjuster CO and H should be adjusted2Ratio, control H2It is 1 with CO molar ratios:1.2~2.5 become synthesis gas, and synthesis gas enters synthesis gas compression Machine pressurizes, subsequently into purification system.
Synthesis gas is after synthesic gas compressor comes out, and first purified preheater preheating, enters synthesis gas gas-liquid separator afterwards, Polishing filter is entered back into, CO is finally entered2Absorption tower carries out removing CO2The purified treatment of equal gaseous impurities, obtained purification are closed At gas, enters after exchanging heat using purifying, preheating device and catalyze and synthesize section.React startup stage CO and H2Ratio be not up to requirement When condition, then decontaminating syngas enters adjuster and continues to recycle, and further reacts, and reaches to send to again after requirement and catalyzes and synthesizes Section.
Purification system makees absorbent (NHD solvents) using polyethylene glycol dimethyl ether solution, and fresh NHD solvents are sent outside from battery limit (BL) To absorbent circulating pump, pumping goes absorbent heat exchanger to heat, then is sent to CO after being pressurizeed by absorbent force (forcing) pump2Absorption tower, mist Change spray mixed gas, absorbs the CO in gas2Etc. foreign gases, afterwards enter hp flash drum flash, insoluble gas bout at Air compressor recycles, and absorbent passes through absorbent heat exchanger, high pressure liquid heater successively, and atmospheric flashing tank is entered after heat exchange and is dodged It steams, insoluble gas goes fused salt heating furnace, absorbent to pump out-of-bounds after the failure of NHD solvents by absorbent circulating pump pumping circulation Area's exterior tank car transports recovery processing.
3, section is catalyzed and synthesized
It is mixed in circulating air compressor entrance and recyclegas, recycle methanol that the decontaminating syngas that section is come is prepared from synthesis gas It closes, after exchanging heat with synthesis air preheater, reaction gas heat exchanger, then reacted startup heater high pressure steam heating to reaction Temperature carries out catalysis reaction by being sent into synthetic catalyst bed at the top of synthesis reactor.Chemical reaction is transformed into methanol, ethyl alcohol Deng.It pressurizes the pressure (hydraulic) water that is pumped into for boiler water between pipe, by its heated vaporization in synthesis reactor and in middle pressure steam Vapor-liquid separation in packet constitutes thermal siphon Natural Circulation, removes reaction heat.It is steamed to being pressed in synthetic reaction process units initial operating stage The low-pressure steam that drum generates is pressurized using steam mechanical recompression MVR technologies, and (pressure is big for generated middle pressure steam In 0.4MPa, it is less than 0.8MPa) it is incorporated to middle pressure steam pipe network, a large amount of emptying of device initial operating stage steam are avoided, effectively Realize Waste Heat Reuse.Corresponding steam pipe network is incorporated to after steam pressure reaches requirement.
Gas after reaction also contains the side reaction products such as propyl alcohol, butanol in addition to containing purpose product methanol, ethyl alcohol.By During catalyzing and synthesizing, conversion per pass is relatively low, therefore a large amount of unreacted synthesis gas must recycle.Reaction gas Reacted gas heat exchanger cooling first, and after further condensed through boiler water heat exchanger, product cooler, condensation temperature is 55~ 60 DEG C, gas-liquid two-phase is directly entered high-pressure gas-liquid separator without isolation after condensation, and the reaction under high pressure gas after separation, which enters, to follow Ring compressor suction tank makees recyclegas, and liquid enters low-pressure gas-liquid separator, and the low pressure reaction gas after separation, which also enters, to follow Ring compressor suction tank makees recyclegas, and liquid is mixed alcohol, removes mixed alcohol storage tank.
To prevent reduction synthetic gas density after the accumulation of the on-condensible gases such as nitrogen and carbon dioxide from influencing being smoothed out for reaction, A part of sidestream gas is extracted out from high-pressure gas-liquid separator outlet circulating air to be purified, and carbon dioxide and other impurities are removed Gas return system afterwards recycles.Side stream gas enters purification system from synthesic gas compressor entrance.
The pyrolysis reactor of the present invention is anaerobic low temperature pyrolyzer reaction system, such as U.S. Union Carbide Corp The moving bed smelting process Purox systems of exploitation, the rotary kiln class pyrolytic process of Aalen-Unterkochen companies of Germany research and development The twin tower circulating fluidized bed pyrolysis system that PKA systems, the weak former and Kobe of the cast stove moment pyrolysis system of Garrett and Japan are developed System etc..Other devices that can realize organic matter thermal cracking can also be used.
Gasifier can use the known equipment for producing synthesis gas, such as fixed bed pressured gasification in the present invention (Lurgi), water coal slurry pressure gasification (GE, opposed multiinjector, polynary slurry) and dry powder coal pressure gasification technology (Shell, GSP) etc..Other devices that can realize production synthesis gas can also be used.
Beneficial effects of the present invention：
1, the present invention produces the mixed alcohols such as first, ethyl alcohol using organic waste, can solve the bands such as garbage loading embeading, burning The problem of environmental pollutions such as " dioxin " come, while can realize landfill minimizing, innoxious, recycling organic waste, Turn waste into wealth, while the production cost of methanol, ethyl alcohol can be reduced.
2, the present invention prepares the H of section by strictly controlling synthesis gas2With CO molar ratios, promote the synthesis for catalyzing and synthesizing section anti- Should more fully it improve the conversion ratio of methanol, ethyl alcohol, reduce the generation of by-product.
3, active principle (CO+H in the purified synthesis gas of the present invention2) content accounts for 80% or so, methane content<0.1%.Carbon Conversion ratio reaches 95~98%, high conversion rate, while gasification does not generate the pollutants such as tar, naphthalene, phenol, waste water treatment letter It is single, easily reach discharge index.
4, the present invention uses multicomponent catalyst collective effect, improves the efficiency of production first, ethyl alcohol, improves conversion ratio, simultaneously The dosage of catalyst is few, and effect is good.
5, device and method using the present invention, the conversion ratio that organic waste is converted into charcoal is 62~69%, raw The conversion ratio that object charcoal produces mixed alcohol product is 97~99%.
6, the present invention provides the complete production methods from organic waste to mixed alcohol, by the integrated and strong of process Change, change and optimization technological process reduce the dosage of steam and recirculated water, the energy of the production of entire technological process are greatly lowered Consumption.
Description of the drawings
Fig. 1 is the process flow chart of thermal cracking charing section of the present invention；
Fig. 2 is the process flow chart that synthesis gas of the present invention prepares section；
Fig. 3 is the process flow chart that the present invention catalyzes and synthesizes section.
Reference numeral：101. feeder, 102. cracking reactors, 103. heavy oil condensers, 104. light-water condensers, 105. Discharge conveyer, 106. fused salt heating furnaces, 107. driers, 108. molten salt circulating pumps, 109. petroleum pumps, 110. fixed gases pump, 111. technique water pump, 112. vacuum pumps, 201. flour mills, 202. charcoals starch tank, 203. charcoal stock pumps, 204. gasifiers, 205. lime-ash Separator, 206. adjusters, 207. synthesic gas compressors, 208. purifying, preheating devices, 209. synthesis gas gas-liquid separators, 210. is net Change filter, 211.CO2Absorption tower, 212. hp flash drums, 213. atmospheric flashing tanks, 214. absorbent circulating pumps, 215. inhale Agent force (forcing) pump is received, 216. high pressure liquid heaters, 217. absorbent heat exchangers, 218. gas phases adjustment pipe, 301. synthesize air preheaters, 302. reaction gas heat exchangers, 303. reactions start heater, 304. synthesis reactor, 305. middle pressure steam packets, 306. boiler waters Heat exchanger, 307. product coolers, 308. high-pressure gas-liquid separators, 309. low-pressure gas-liquid separators, 310. suckings fill, and 311. follow Ring air compressor.
Specific implementation mode
Invention is further explained below in conjunction with the accompanying drawings, but not as limitation of the present invention.
Embodiment 1
Organic waste produces the device (as shown in Figures 1 to 3) of low carbon mixed alcohol, including organic castoff heat cracking charing Section, synthesis gas prepare section, catalyze and synthesize section.
1, thermal cracking carbonizes section：Including reaction system, heating system and piece-rate system.Structure is as follows：
(1) reaction system, drier 107 is connected with feeder 101, and feeder 101 is further through pipeline and cracking reaction The feed inlet of device 102 is connected, and the discharge nozzle of cracking reactor 102 is connected with discharging conveyer 105, discharging conveyer 105 and conjunction The flour mill 201 that section is prepared at gas is connected by pipeline.Automatic grate, velocity of rotation control are provided in cracking reactor 102 Reaction time of the raw material processed in pyrolysis reactor.Cracking reactor 102 is connected with vacuum pump 112, is protected by vacuum pump 112 The negative pressure in pyrolysis reactor 102 is held, the outlet of vacuum pump 112 is connect with piece-rate system.
(2) heat pipe that goes out of heating system, fused salt heating furnace 106 is directly connect with cracking reactor 102, cracking reactor 102 fused salt outlet is connect by molten salt circulating pump 108 with fused salt heating furnace 106, and thermal cycle is formed.Fused salt heating furnace 106 Gas outlet is connected with drier 107 and torch.
(3) piece-rate system, after the outlet of vacuum pump 112 successively with 104 phase of heavy oil condenser 103 and light-water condenser Even, the condensate pipe of light-water condenser 104 is transported to the flour mill 201 that synthesis gas prepares workshop section by technique water pump 111；Light-water The fixed gas pipe of condenser 104 is connect by fixed gas pump 110 with fused salt heating furnace 106.The condenser pipe of heavy oil condenser 103 is logical Petroleum pump 109 is crossed to connect with fused salt heating furnace 106.
2, synthesis gas prepares section：Including gasification system, purification system.Structure is as follows：
(1) gasification system, flour mill 201 are connected with charcoal slurry tank 202；Charcoal slurry tank 202 passes through charcoal stock pump 203 and gasifier 204 are connected, and gasifier 204 is equipped with compressed air inlet and high pressure steam inlet, and the escape pipe of gasifier 204 is detached with lime-ash Device 205 is connected, and the slag notch of gasifier 204 is connected with fixed-end forces system.The gaseous phase outlet pipe of grey pulp separator 205 passes through three Pass joint is connect with adjuster 206 and gas phase adjustment pipe 218, and the residue outlet of grey pulp separator 205 is connected with fixed-end forces system. Gas phase adjustment pipe 218, which is connected to, catalyzes and synthesizes Duan Lian.
(2) purification system, adjuster 206 are connect by synthesic gas compressor 207 with purifying, preheating device 208；Purifying, preheating The escape pipe of device 208 successively with synthesis gas gas-liquid separator 209, polishing filter 210 and CO2Absorption tower connection 211；CO2It absorbs The top gas phase outlet of tower 211 is connect after being exchanged heat by purifying, preheating device 208 with gas phase adjustment pipe 218, gas phase adjustment Manage and catalyze and synthesize section connection.
(3) absorbent transport system, fresh absorbent delivery pipe fill 213 and the company of absorbent circulating pump 214 with atmospheric flashing It connects, the outlet of absorbent circulating pump 214 is connect with absorbent heat exchanger 217, and absorbent heat exchanger 217 passes through absorbent force (forcing) pump 215 are connected to CO2211 top of absorption tower；CO2The absorbent sewer pipe of 211 bottom of absorption tower fills 212 with high pressure flash, inhales successively It receives agent heat exchanger 217, high pressure liquid heater 216, atmospheric flashing and fills 213 connections, atmospheric flashing fills 213 and absorbent circulating pump 214 are connected by pipeline.
3, section is catalyzed and synthesized, synthesis air preheater 301 is connected with reaction gas heat exchanger 302, then reacted startup heater 303 are connected with synthesis reactor 304, and middle pressure steam packet 305 is bi-directionally connected with synthesis reactor 304.Synthesis reactor 304 goes out Reacted gas heat exchanger 302, boiler water- to-water heat exchanger 306 and product cooler 307 are connected to high-pressure gas-liquid point to tracheae later successively From device 308, high-pressure gas-liquid separator 308 is connect with low-pressure gas-liquid separator 309 again, the outlet of low-pressure gas-liquid separator 309 It is connect with mixed alcohol storage tank.Recycle gas compressor 311,308 He of high-pressure gas-liquid separator are provided with before synthesis gas preheater pipeline The purification system that the gas phase pipe of low-pressure gas-liquid separator 309 fills 310, synthesis gas preparation section with sucking is connected, and sucks and fill 310 It is connected with recycle gas compressor 311.
In conjunction with the device of the invention, the method (as shown in Figures 1 to 3) that low carbon mixed alcohol is produced to organic waste is said It is bright：
1, thermal cracking carbonizes section
Raw material by pretreatment sort, removal inorganic matter, metal impurities, into drier be dried to water content 15% with Under, pyrolysis reactor (the moving bed melting of U.S. Union Carbide Corp exploitations is delivered by feeder after crushing Technique Purox systems, anaerobic low temperature pyrolyzer reaction system) thermal cracking carbonization reaction is carried out, leakproofness is during which controlled by valve group, It is 8~10KPa to keep the vacuum degree in pyrolysis reactor by vacuum pump, and 570~650 DEG C of reaction temperature controls Automatic grate Velocity of rotation come control the reaction time be 2.5~3.5 hours, drive and stir raw material, reaction generate charcoal bring to anti- Device is answered to export, sending to synthesis gas by discharging conveyer prepares section.
It reacts the gas generated and liquid all pumps piece-rate system with gas phase by vacuum pump, it is cold to pass through heavy oil successively Condenser and light-water condenser, the non-condensable gas that the bio-fuel-oil and light-water condenser that heavy oil condenser condenses out come out are led back Heating furnace burning utilizes；The process water that light-water condenser condenses out, which is then transported in the flour mill of synthesis gas workshop section, carries out profit With.Fused salt is heated by fuel oil combustion when fused salt heating furnace starts, the heavy oil component that is generated by reaction after normal operation and is not coagulated Gas combustion heating fused salt, tail gas remove drier drying material, and exhaust-gas treatment, the fused salt of heating is gone to be pumped by molten salt circulating pump later Cycle.
2, synthesis gas prepares section
Charcoal enters flour mill with process water and wears into charcoal slurry and be adjusted to a concentration of 80% charcoal water slurry, is starched into charcoal Tank stores, then is sent into gasifier (fixed bed pressured gasification (Lurgi)) by charcoal stock pump, while compressed air and high steam is added Pressurized gasification reaction is carried out, reaction pressure is 4.0~6.0MPa, 1350~1400 DEG C of reaction temperature, gasification generation CO, H2、CO2 Equal mixed synthesis gas, synthesis gas enter grey pulp separator and remove solid, liquid waste, then further react adjustment CO into adjuster With H2Ratio, control synthesis gas in H2Molar ratio with CO is 1:1.2~1.5, synthesis gas enters synthesic gas compressor pressurization, Purified preheater preheating, synthesis gas gas-liquid separator, polishing filter finally enter CO successively after out2Absorption tower carries out Remove CO2The purified treatment of equal gaseous impurities, obtained decontaminating syngas enter catalysis after exchanging heat using purifying, preheating device and close At section.
3, section is catalyzed and synthesized
Decontaminating syngas is mixed into circulating air compressor with recyclegas, recycle methanol and is pressurized to 10~12MPa, passes through After synthesizing air preheater, reaction gas heat exchanger heat exchange, then reacted startup heater high pressure steam heating is to 290~300 DEG C Reaction temperature, by be sent at the top of synthesis reactor synthetic catalyst bed (french petroleum research institute (IFP) exploitation The Sygmol technique MoS2 catalyst that IFP technique Cu-Co catalyst is developed with Dow Chemical Company is 1 according to mass ratio:1 mixing It is made) catalysis reaction is carried out, 4000~5000h of volume space velocity is calculated with dry gas-1, catalysis generation methanol, ethyl alcohol, propyl alcohol, butanol Etc. thick mixed alcohol.Since during catalyzing and synthesizing, conversion per pass is relatively low, therefore a large amount of unreacted synthesis gas must recycle It uses.Reaction gas reacted gas heat exchanger cooling first, and after further condensed through boiler water heat exchanger, product cooler, Condensation temperature is 55~60 DEG C, and gas-liquid two-phase is directly entered high-pressure gas-liquid separator without isolation after condensation, the high pressure after separation Reaction gas enters recycle compressor suction tank and makees recyclegas, and liquid enters low-pressure gas-liquid separator, and the low pressure after separation is anti- Gas is answered also to make recyclegas into recycle compressor suction tank, liquid is mixed alcohol finished product, removes mixed alcohol storage tank.
Boiler water pressurizes the pressure (hydraulic) water that is pumped into, by its heated vaporization in synthesis reactor and in middle pressure steam packet In vapor-liquid separation constitute thermal siphon Natural Circulation, remove reaction heat.To synthetic reaction process units initial operating stage middle pressure steam It contracts for fixed output quotas raw low-pressure steam, is pressurized using steam mechanical recompression MVR technologies, (pressure is more than generated middle pressure steam 0.4MPa is less than 0.8MPa) it is incorporated to middle pressure steam pipe network, a large amount of emptying of device initial operating stage steam are avoided, it is effective real Existing Waste Heat Reuse.Corresponding steam pipe network is incorporated to after steam pressure reaches requirement.
To prevent reduction synthetic gas density after the accumulation of the on-condensible gases such as nitrogen and carbon dioxide from influencing being smoothed out for reaction, A part of sidestream gas is extracted out from high-pressure gas-liquid separator outlet circulating air to be purified, and carbon dioxide and other impurities are removed Gas return system afterwards recycles.Side stream gas enters purification system from synthesic gas compressor entrance.
Method using the present invention, the conversion ratio that organic waste prepares charcoal are 65~69%.Charcoal production is mixed The conversion ratio for closing alcohol product is 97~99%.
Embodiment 2
The device of organic waste production low carbon mixed alcohol, method are same as Example 1, difference lies in：
1, thermal cracking carbonizes section
The rotary kiln class pyrolytic process PKA systems that pyrolysis reactor is researched and developed using Aalen-Unterkochen companies of Germany It unites (anaerobic low temperature pyrolyzer reaction system), thermal cracking carbonization reaction condition：Vacuum degree be 15~22KPa, reaction temperature 450~ 520 DEG C, the reaction time is 2.5~4.0 hours.
2, synthesis gas prepares section
Charcoal enters flour mill with process water and wears into charcoal slurry and be adjusted to a concentration of 85% charcoal water slurry, gasifier (water coal slurry pressure gasification (opposed multiinjector)), the reaction pressure in gasifier are 6.0~8.7MPa, reaction temperature 1250~ 1300 DEG C, gasification generates CO, H2、CO2Equal mixed synthesis gas.The H after gas adjusts2Molar ratio with CO is 1:1.5~2.0, warp Purified decontaminating syngas enters after exchanging heat using purifying, preheating device and catalyzes and synthesizes section.
3, section is catalyzed and synthesized
Catalyst bed in synthesis reactor using Snam companies withThe MAS technique alkalinity that company develops jointly The Octamix technique Cu-Zn catalyst that additive modification ZnO/Cr2O3 catalyst is developed with Lurgi companies is 1 according to mass ratio: 0.2~0.3 mixed catalyst being mixed, reaction condition are：Pressure 12MPa, 310~325 DEG C of temperature calculate body with dry gas Long-pending 3000~4000h of air speed-1。
Method using the present invention, the conversion ratio that organic waste prepares charcoal are 62~65%.Charcoal production is mixed The conversion ratio for closing alcohol product is 98~99%.
Embodiment 3
The device of organic waste production low carbon mixed alcohol, method are same as Example 1, difference lies in：
1, thermal cracking carbonizes section
Pyrolysis reactor uses the cast stove moment pyrolysis system (anaerobic low temperature pyrolyzer reaction system) of Garrett, heat Crack carbonization reaction condition：Vacuum degree is 18KPa, and 530~550 DEG C of reaction temperature, the reaction time is 3.0~4.5 hours.
2, synthesis gas prepares section
Charcoal enters flour mill with process water and wears into charcoal slurry and be adjusted to a concentration of 80% charcoal water slurry, gasifier water Coal slurry pressurized gasification (GE), the reaction pressure in gasifier are 2.8~4.0MPa, 1300~1380 DEG C of reaction temperature, gasification life At CO, H2、CO2Equal mixed synthesis gas.The H after gas adjusts2Molar ratio with CO is 1:2.0~2.5, it is purified after purification Synthesis gas enters after exchanging heat using purifying, preheating device and catalyzes and synthesizes section.
3, section is catalyzed and synthesized
Catalyst bed in synthesis reactor using Snam companies withThe MAS technique alkalinity that company develops jointly The IFP technique Cu-Co catalyst of additive modification ZnO/Cr2O3 catalyst and french petroleum research institute (IFP) exploitation, according to Mass ratio is 1:1 mixed catalyst being mixed, reaction condition are：10~12MPa of pressure, 300~350 DEG C of temperature, with dry Gas calculates 40000~4500h of air speed of volume-1。
Method using the present invention, the conversion ratio that organic waste prepares charcoal are 62~64%.Charcoal production is mixed The conversion ratio for closing alcohol product is 97~98%.
Embodiment 4
The device of organic waste production low carbon mixed alcohol, method are same as Example 1, difference lies in：
1, thermal cracking carbonizes section
Using the weak former twin tower circulating fluidized bed pyrolysis system developed with Kobe of Japan, (anaerobic low temperature is split pyrolysis reactor Solve reaction system), thermal cracking carbonization reaction condition：Vacuum degree is 10~17KPa, 600~650 DEG C of reaction temperature, reaction time It is 1.5~2.5 hours.
2, synthesis gas prepares section
Charcoal enters flour mill with process water and wears into charcoal slurry and be adjusted to a concentration of 80~85% charcoal water slurry, gasifies Device (water coal slurry pressure gasification of polynary slurry), the reaction pressure in gasifier are 4.5~6.5MPa, reaction temperature 1325~ 1390 DEG C, gasification generates CO, H2、CO2Equal mixed synthesis gas.The H after gas adjusts2Molar ratio with CO is 1:1.5~2.0, warp Purified decontaminating syngas enters after exchanging heat using purifying, preheating device and catalyzes and synthesizes section.
3, section is catalyzed and synthesized
Catalyst bed in synthesis reactor using Snam companies withThe MAS technique alkalinity that company develops jointly The Sygmol technique MoS2 catalyst that additive modification ZnO/Cr2O3 catalyst is developed with Dow Chemical Company is 1 according to mass ratio: 0.3~0.5 mixed catalyst being mixed, reaction condition are：10~12MPa of pressure, 280~320 DEG C of temperature, in terms of dry gas Calculate the air speed 2000-3000h of volume-1。
Method using the present invention, the conversion ratio that organic waste prepares charcoal are 60~65%.Charcoal production is mixed The conversion ratio for closing alcohol product is 98~99%.

Claims (10)

1. organic waste produces the device of low carbon mixed alcohol, it is characterised in that：It include organic castoff heat cracking charing section, Synthesis gas prepares section, catalyzes and synthesizes section；
The organic waste thermal cracking charing section includes reaction system, heating system；Reaction system include feeder (101), Cracking reactor (102), vacuum pump (112), discharging conveyer (105)；The feeder (101) passes through pipeline and cracking reaction The feed inlet of device (102) is connected, and Automatic grate, cracking reactor (102) and vacuum pump are provided in cracking reactor (102) (112) it connects, the discharge nozzle of cracking reactor (102) is connected with discharging conveyer (105), discharging conveyer (105) and synthesis The flour mill (201) that gas prepares section is connected by pipeline；The heating system includes fused salt heating furnace (106), cracking reactor (102) it directly connect, cracks with cracking reactor (102) with molten salt circulating pump (108), the heat pipe that goes out of fused salt heating furnace (106) The fused salt outlet of reactor (102) is connect by molten salt circulating pump (108) with fused salt heating furnace (106)；
It includes gasification system, purification system that the synthesis gas, which prepares section,；Gasification system includes flour mill (201), charcoal slurry tank (202), charcoal stock pump (203), gasifier (204) and grey pulp separator (205)；Flour mill (201) is connected with charcoal slurry tank (202)； Charcoal slurry tank (202) is connected by charcoal stock pump (203) with gasifier (204), and gasifier (204) is equipped with compressed air inlet and height Steam inlet, the escape pipe of gasifier (204) is pressed to be connected with grey pulp separator (205), the slag notch and solid waste of gasifier (204) Processing system is connected；The gaseous phase outlet pipe of grey pulp separator (205) is connect with adjuster (206) and gas phase adjustment pipe (218), ash The residue outlet of pulp separator (205) is connected with fixed-end forces system；
The purification system includes adjuster (206), synthesic gas compressor (207), purifying, preheating device (208), synthesis gas gas-liquid Separator (209), polishing filter (210) and CO2Absorption tower (211)；Adjuster (206) passes through synthesic gas compressor (207) Connect with purifying, preheating device (208), the escape pipe of purifying, preheating device (208) successively with synthesis gas gas-liquid separator (209), purification Filter (210) and CO2Absorption tower (211) connects, CO2The top gas phase outlet on absorption tower (211) passes through purifying, preheating device (208) it adjusts pipe (218) with gas phase after exchanging heat to connect, gas phase adjustment pipe (218) and the synthesis air preheater for catalyzing and synthesizing section (301) it connects；
The section that catalyzes and synthesizes includes synthesis air preheater (301), reaction gas heat exchanger (302), reaction startup heater (303), synthesis reactor (304), boiler water- to-water heat exchanger (306), product cooler (307), high-pressure gas-liquid separator (308), Low-pressure gas-liquid separator (309)；Synthesis air preheater (301) is connected with reaction gas heat exchanger (302), then reacted startup heating Device (303) is connected with synthesis reactor (304), the escape pipe of synthesis reactor (304) successively reacted gas heat exchanger (302), High-pressure gas-liquid separator (308), high-pressure gas-liquid separation are connected to after boiler water- to-water heat exchanger (306) and product cooler (307) Device (308) is connect with low-pressure gas-liquid separator (309), and the outlet of low-pressure gas-liquid separator (309) is connect with mixed alcohol storage tank.
2. the device of organic waste production low carbon mixed alcohol according to claim 1, it is characterised in that：It is carbonized in cracking Dry materials device (107) is added before the feeder (101) of workshop section；After the outlet of vacuum pump (112) successively with heavy oil condenser (103) it is connected with light-water condenser (104), the condensate pipe of light-water condenser (104) is transported to conjunction by technique water pump (111) The flour mill (201) of workshop section is prepared at gas；The fixed gas pipe of light-water condenser (104) is added by fixed gas pump (110) with fused salt Hot stove (106) connects；The condenser pipe of heavy oil condenser (103) is connect by petroleum pump (109) with fused salt heating furnace (106).
3. the device of organic waste production low carbon mixed alcohol according to claim 1, it is characterised in that：The synthesis gas It further includes absorbent transport system to prepare section comprising high pressure flash fills (212), atmospheric flashing fills (213), absorbent circulating pump (214), absorbent force (forcing) pump (215), high pressure liquid heater (216), absorbent heat exchanger (217)；Fresh absorbent delivery pipe (213) are filled with atmospheric flashing and absorbent circulating pump (214) is connect, absorbent circulating pump (214) outlet and absorbent heat exchanger (217) it connects, absorbent heat exchanger (217) is connected to CO by absorbent force (forcing) pump (215)2Absorption tower (211) top；CO2It inhales The absorbent sewer pipe for receiving tower (211) bottom fills (212), absorbent heat exchanger (217), high pressure liquid heating with high pressure flash successively Device (216), atmospheric flashing fill (213) connection, and atmospheric flashing fills (213) and connect by pipeline with absorbent circulating pump (214).
4. the device of organic waste production low carbon mixed alcohol according to claim 1, it is characterised in that：The catalysis is closed Further include middle pressure steam packet (305) at section, suck filling (310) and recycle gas compressor (311), middle pressure steam packet (305) and conjunction It is bi-directionally connected at reactor (304)；Recycle gas compressor (311) is arranged before synthesizing air preheater (301) pipeline, high-pressure gas-liquid The gas phase pipe of separator (308) and low-pressure gas-liquid separator (309) fills (310) with sucking and synthesis gas prepares the purification system of section It is connected；Sucking fills (310) and is connected with recycle gas compressor (311).
5. the method for the organic waste production low carbon mixed alcohol using 4 any described device of Claims 1 to 4, feature exist In：It includes the following steps:
(1) thermal cracking carbonizes, and cracking reactor is transported to after organic waste is fed and carries out thermal cracking carbonization reaction, reacts item Part is 8~22KPa of vacuum degree, and oxygen-free environment, 420~650 DEG C of reaction temperature, the reaction time is to be given birth to for 1.5~4.5 hours Object charcoal, the generation raw material as synthesis gas；
(2) prepared by synthesis gas, and charcoal is transported to the charcoal water slurry that charcoal slurry tank is adjusted to a concentration of 80~85% after milling, It is transferred in gasifier again, carrying out pressurized gasification with compressed air and high steam reacts, and reaction pressure is 2.8~8.7MPa, instead 1250~1400 DEG C of temperature, gasification is answered to generate CO, H2、CO2And other synthesis gas further remove solid, liquid by grey pulp separator Waste, processed synthesis gas control H by air doctor2It is 1 with CO molar ratios:1.2~2.5；And synthesis gas is carried out Purification, is finally transported to and catalyzes and synthesizes workshop section；
(3) catalyze and synthesize, synthesis gas is pressurized to 10~12MPa by compressor, enters back into synthesis reactor, temperature 280~ It at 350 DEG C, carries out catalyzing and synthesizing effect under the action of catalyst, 2000~15000h of volume space velocity is calculated with dry gas-1, generate The thick mixed alcohol of first, ethyl alcohol and other alcohol removes most of gas of thick mixed alcohol by depressurizing, flashing, is finally separating out Obtain mixed alcohol product.
6. the method for organic waste production low carbon mixed alcohol according to claim 5, it is characterised in that：The catalyst For mixing Co -- Mo catalyst, modified ZnO/Cr2O3Catalyst, Cu-Zn catalyst, Cu-Co catalyst, MoS2One in catalyst Kind or more than one combinations.
7. the method for organic waste production low carbon mixed alcohol according to claim 6, it is characterised in that：The catalyst For mixing Co -- Mo catalyst, modified ZnO/Cr2O3Catalyst, Cu-Zn catalyst, Cu-Co catalyst, MoS2Two in catalyst Kind combination, it is 1 to match:0.2~1.0.
8. the method for organic waste production low carbon mixed alcohol according to claim 5, it is characterised in that：The organic waste Gurry is first dried to 15% or less water content and is crushed before entering feeder, then is fed.
9. the method for organic waste production low carbon mixed alcohol according to claim 5, it is characterised in that：The step (1) when thermal cracking, the organic matter in material is thermal decomposited to form gas phase, detaches cracking instead by vacuum pump rapidly under vacuum conditions Device is answered, heavy oil condenser is conveyed through successively and light-water condenser carries out gas-liquid condensation separation；Heavy oil condenser condenses out The non-condensable gas that bio-fuel-oil and light-water condenser are separated leads back fused salt heating furnace and carries out burning utilization；Light-water condenser The process water condensed out is then transported in the flour mill of synthesis gas workshop section and is utilized.
10. the method for organic waste production low carbon mixed alcohol according to claim 5, it is characterised in that：The step (2) gas adjustment is that processed synthesis gas first passes through adjuster processing in, and then pressurization carries out hot friendship by purifying, preheating device It changes, carrying out gas-liquid separation using synthesis gas gas-liquid separator removes liquid phase, and synthesis gas enters back into polishing filter filtering and impurity removing, Finally it is passed through CO2Absorption tower removes CO2And other gases be purified after synthesis gas；Purified synthesis gas is using purification Preheater exchanges heat, and detects purified synthesis gas and meets H2It is 1 with CO molar ratios:After 1.2~2.5, using gas tune Homogeneous tube, which is transported to, catalyzes and synthesizes workshop section；Match it is incongruent in the case of, then continue to flow back into adjuster carrying out cycle adjustment.
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