Method and device for preparing synthesis gas from organic hazardous waste and biomass

Abstract

The invention relates to the technical field of solid waste treatment, and provides a method and a device for preparing synthesis gas from organic hazardous waste and biomass. According to the method, organic hazardous waste and biomass are adopted as raw materials, and the synthesis gas is prepared through the self-heating entrained-flow bed. According to the invention, the organic hazardous waste slurry and the biomass-based powder are respectively fed, so that the feeding adjustment in any proportion can be realized, the organic hazardous waste treatment capacity is large, the gasification efficiency is high, and the carbon emission is low; and meanwhile, the feeding mode can realize independent atomization of the organic hazardous waste slurry and the biomass-based powder, also has a reaction coupling effect, and can improve the gasification efficiency and the content of effective components in the synthesis gas. In conclusion, the synthesis gas is prepared from the organic hazardous waste and the biomass, efficient treatment and resource utilization of the organic hazardous waste and the biomass can be achieved at the same time, fossil energy consumption is reduced, meanwhile, carbon emission is small, environmental pollution is small, the obtained synthesis gas can be used for preparing various high-added-value products, remarkable environmental and economic benefits are achieved, and the method is suitable for industrial production. The application prospect is wide.

Description

Technical Field

[0001] The present invention relates to the technical field of solid waste treatment, and in particular to a method and device for preparing synthesis gas by using organic hazardous waste and biomass. Background Art

[0002] Hazardous organic waste is a type of organic waste with certain hazards generated during industrial production, such as waste plastics, waste rubber, waste oil, and distillation residues. Hazardous organic waste is difficult to manage due to its complex composition, poor biodegradability, and toxic and harmful properties. Currently, the main treatment methods are incineration or landfill. However, incineration cannot treat some hazardous organic wastes, and the incineration process easily produces highly toxic organic pollutants such as dioxins, as well as atmospheric pollutants such as nitrogen oxides and sulfur oxides, which can easily cause secondary pollution. The landfill method has the risk of leakage, a long treatment cycle, and requires a large area of ​​land to build a landfill. With the development of cities and the increase in the amount of hazardous organic waste generated, suitable landfill sites are becoming increasingly difficult to obtain.

[0003] Gasification is a new method for treating organic hazardous waste. It has a high degree of harmlessness and significant reduction, and has great application prospects. At present, water-coal slurry gasification furnaces are usually used to collaboratively treat organic hazardous waste. This method requires mixing organic hazardous waste with coal to form a water-coal slurry, which is then fed into the gasifier along with oxygen for gasification under high temperature and high pressure. The organic hazardous waste undergoes a series of physical and chemical reactions under the high temperature, high pressure and reducing atmosphere of the gasifier, and is decomposed, gasified and converted into products such as synthesis gas and slag. However, this method can only replace part of the coal with organic hazardous waste. The amount of organic hazardous waste added is small, the consumption of petrochemical energy is high, and the gasification efficiency is low. Summary of the Invention

[0004] In light of this, the present invention provides a method and apparatus for producing syngas from hazardous organic waste and biomass. This method uses hazardous organic waste and biomass as raw materials to produce syngas via an autothermal entrained flow reactor, reducing fossil energy consumption, achieving high gasification efficiency, and reducing carbon emissions while increasing the processing capacity of hazardous organic waste.

[0005] In order to achieve the above-mentioned object of the invention, the present invention provides the following technical solutions:

[0006] A method for preparing synthesis gas using organic hazardous waste and biomass comprises the following steps:

[0007] The organic hazardous waste slurry, biomass-based powder and gasifying agent are introduced into an autothermal entrained flow reactor for gasification reaction to obtain synthesis gas; the gasifying agent is oxygen;

[0008] The gasifying agent is divided into a first part of gasifying agent and a second part of gasifying agent; the first part of gasifying agent is mixed with organic hazardous waste slurry to form a first mixed flow that enters the autothermal entrained flow reactor; the biomass-based powder transported by the carbon dioxide gas flow and the second part of gasifying agent form a second mixed flow that enters the autothermal entrained flow reactor; the second mixed flow is distributed around the first mixed flow.

[0009] Preferably, a central mixer and an outer ring mixer are provided on the top of the autothermal entrained flow reactor; the outer ring mixers are distributed around the central mixer; the organic hazardous waste slurry and the first part of the gasifying agent are introduced into the autothermal entrained flow reactor from the central mixer;

[0010] The biomass-based powder is transported by a carbon dioxide gas flow and introduced into the autothermal entrained flow reactor together with a second portion of a gasifying agent from an outer ring mixer.

[0011] Preferably, the central mixer is a sleeve-type structure, and the sleeve-type structure forms a feed channel; the central mixer has three or more feed channels; the organic hazardous waste slurry and the first part of the gasifying agent are respectively introduced into different feed channels of the central mixer;

[0012] The number of the outer ring mixers is more than 3; each outer ring mixer is formed by two cylindrical structures with different diameters nested together to form a telescopic structure, the center of the telescopic structure is the inner channel, and the gap between the two cylindrical structures is the outer channel; the biomass-based powder is introduced into the inner channel under the transport of carbon dioxide gas flow, and the second part of the gasifying agent is introduced into the outer channel.

[0013] Preferably, the lower calorific value of the organic hazardous waste slurry is ≥10000KJ / kg and the density is <1250kg / m 3 , moisture content <50wt%;

[0014] The biomass-based powder has a lower calorific value of ≥18000KJ / Kg and a bulk density of 200-600kg / m 3 , average particle size <0.8mm, moisture content <8wt%.

[0015] Preferably, the mass ratio of the biomass-based powder to carbon dioxide is 5 to 20:1; the ratio of the total mass of the gasifying agent to the total mass of the organic hazardous waste slurry and the biomass-based powder is 0.4 to 0.75:1;

[0016] The temperature of the gasification reaction is 1200-1500° C., and the pressure is 1-4 MPa.

[0017] Preferably, the gasification produces a mixture of crude synthesis gas and molten inorganic matter, and the method further comprises: subjecting the mixture to water quenching to produce hydrous ash synthesis gas and glassy slag;

[0018] The water-ash-containing synthesis gas is subjected to gas-liquid separation to obtain the ash-containing synthesis gas; the ash-containing synthesis gas is washed and deashed after being infiltrated to obtain the synthesis gas;

[0019] The quenching water quenching, gas-liquid separation and washing and ash removal also produce ash-containing water; the ash-containing water is sequentially subjected to pressure reduction and temperature concentration and negative pressure temperature reduction and concentration, and then filtered to obtain ash residue and recovered water; the content of solid suspended matter in the recovered water is 30-50 mg / L.

[0020] The present invention also provides a device for preparing synthesis gas using organic hazardous waste and biomass, comprising an autothermal fluidized bed reactor; a mixer is provided on the top of the autothermal fluidized bed reactor, and the mixer includes a central mixer and outer ring mixers distributed around the central mixer; the autothermal fluidized bed reactor is provided with a gas outlet.

[0021] Preferably, the self-heating fluidized bed reactor includes a reaction chamber and a cooling chamber from top to bottom; the bottom of the cooling chamber is a water bath area, and a cooling medium distributor is provided at the top of the cooling chamber; a downcomer and an upcomer are provided in the cooling chamber, and the downcomer is separately nested inside the upcomer.

[0022] Preferably, the device further comprises: a gas-liquid separator; the gas-liquid separator is provided with a gas outlet and a liquid outlet; the inlet of the gas-liquid separator is connected to the gas outlet of the autothermal entrained flow reactor;

[0023] an ash infiltrator, wherein the inlet of the ash infiltrator is connected to the gas outlet of the gas-liquid separator;

[0024] A scrubber is provided, wherein the inlet of the scrubber is communicated with the outlet of the ash wetting device.

[0025] Preferably, the device further comprises an ash-containing water treatment system; the ash-containing water treatment system comprises a decompression and temperature reducer; the decompression and temperature reducer is provided with a liquid outlet and a steam outlet; the inlet of the temperature reducer receives external water supply and lower drainage of the cooling chamber, the gas-liquid separator and the scrubber;

[0026] A negative pressure cooler, wherein the inlet of the negative pressure cooler is connected to the liquid outlet of the negative pressure cooler; the negative pressure cooler is provided with a liquid outlet and a steam outlet;

[0027] A negative pressure steam condenser, wherein the inlet of the negative pressure steam condenser is connected to the steam outlet of the negative pressure cooler;

[0028] A negative pressure steam-water separator; the inlet of the negative pressure steam-water separator is connected to the outlet of the negative pressure steam condenser; the negative pressure steam-water separator is provided with a gas outlet and a liquid outlet;

[0029] A negative pressure generator; the inlet of the negative pressure generator is connected to the gas outlet of the negative pressure steam-water separator;

[0030] Atmospheric pressure steam-water separator; the inlet of the atmospheric pressure steam-water separator is connected to the outlet of the negative pressure generator;

[0031] A sedimentation buffer device; the inlet of the sedimentation buffer device is connected to the liquid outlet of the negative pressure cooler;

[0032] Filter device; the inlet of the filter device is connected to the outlet of the sedimentation buffer device;

[0033] A circulating grey water device, wherein the inlet of the circulating grey water device is respectively connected with the liquid outlet of the filtering device, the liquid outlet of the negative pressure steam-water separator and the liquid outlet of the normal pressure steam-water separator.

[0034] The present invention provides a method for preparing synthesis gas by using organic hazardous waste and biomass, comprising the following steps: introducing organic hazardous waste slurry, biomass-based powder and a gasifying agent into an autothermal entrained flow reactor for gasification reaction to obtain synthesis gas; the gasifying agent is oxygen; the gasifying agent is divided into a first part of gasifying agent and a second part of gasifying agent; the first part of gasifying agent is mixed with the organic hazardous waste slurry to form a first mixed flow which enters the autothermal entrained flow reactor; the biomass-based powder conveyed by a carbon dioxide gas flow and the second part of gasifying agent form a second mixed flow which enters the autothermal entrained flow reactor; the second mixed flow is distributed on the periphery of the first mixed flow. The present invention adopts organic hazardous waste and biomass as raw materials, and prepares synthesis gas through an autothermal fluidized bed reactor, and no petrochemical resources need to be consumed during the reaction process; the present invention feeds the organic hazardous waste slurry and the biomass-based powder separately, and can realize the feed adjustment of any proportion, the processing capacity of organic hazardous waste is large, the gasification efficiency is high, and the carbon emission is low; further, the present invention mixes the organic hazardous waste slurry and the gasifier in the central mixer and feeds the biomass-based powder and the gasifier from the outer ring mixer. This feeding method can realize the independent atomization of the organic hazardous waste slurry and the biomass-based powder, and at the same time has a reaction coupling effect, which can improve the uniformity of the organic hazardous waste slurry and the biomass-based powder in the reactor, avoid the mixing of the organic hazardous waste slurry and the biomass-based powder to form larger agglomerated particles, thereby further improving the gasification efficiency, and the effective components in the obtained synthesis gas The content of carbon dioxide (CO and H2) is significantly improved; in addition, the organic hazardous waste used in the present invention is a zero-carbon or negative-carbon raw material, and biomass has low-carbon characteristics, which is beneficial to reducing the content of greenhouse gases such as CO2 in the synthesis gas. At the same time, the present invention uses carbon dioxide to transport biomass-based powder. Carbon dioxide is used as both a transport gas and a reaction raw material to participate in the reaction (C+CO2→2CO), which can further reduce the emission of carbon dioxide in the entire treatment process. Moreover, conventional gasification reactions use steam as a gasifying agent, and steam is generated by combustion. The combustion process will emit a large amount of CO2. The present invention uses oxygen as a gasifying agent and uses CO2 as a reaction raw material, which can reduce overall carbon emissions. The molar ratio of carbon dioxide equivalent and hydrogen equivalent (CO2e / H2) certified by carbon footprint is much lower than that of synthesis gas produced by fossil energy gasification.

[0035] In summary, the present invention uses organic hazardous waste and biomass to prepare synthesis gas, which can simultaneously achieve efficient treatment and resource utilization of organic hazardous waste and biomass, reduce landfill and incineration pollution, and reduce fossil energy consumption. At the same time, carbon emissions are low and environmental pollution is small. The obtained synthesis gas has a high content of effective ingredients and can be used to prepare a variety of high value-added products (methanol, ammonia, high-purity hydrogen, SAF, etc.), or as a clean fuel for power generation or heating, with high economic benefits; therefore, the method provided by the present invention has significant environmental and economic benefits and broad application prospects. BRIEF DESCRIPTION OF THE DRAWINGS

[0036] Figure 1 A schematic structural diagram of the device for producing synthesis gas using hazardous organic waste and biomass provided by the present invention;

[0037] Figure 2 is a structural diagram of the gray water treatment system;

[0038] Figures 1 and 2 Middle: 1 - self-heating entrained flow reactor, 1-1 - reaction chamber, 1-2 - cooling chamber, 2-1 - central mixer, 2-2 - outer ring mixer, 3 - riser, 4 - downcomer, 5 - cooling medium distributor, 6 - gas-liquid separator, 7 - ash soaker, 8 - scrubber, 9 - first pressure pump, 10 - upper slag lock valve, 11 - slag collection device, 12 - lower slag lock valve, 13 - pressure reducer and temperature reducer, 14 - negative pressure temperature reducer, 15 - negative pressure steam condenser, 1 6—negative pressure steam-water separator, 17—negative pressure generator, 18—normal pressure steam-water separator, 19—sedimentation buffer device, 20—slag water pump, 21—filtration device, 22—circulating ash water device, 23—ash water pump, 24—inorganic salt recovery device, 25—heat recovery device, 26—second pressure pump, 27—multi-layer tower tray, 28—second demister, 29—gas guide downpipe, 30—gas guide uppipe, 31—first demister, 32—liquid level control valve. DETAILED DESCRIPTION

[0039] The present invention provides a method for preparing synthesis gas using organic hazardous waste and biomass, comprising the following steps:

[0040] The organic hazardous waste slurry, biomass-based powder and gasifying agent are introduced into an autothermal entrained flow reactor for gasification reaction to obtain synthesis gas; the gasifying agent is oxygen;

[0041] The gasifying agent is divided into a first part of gasifying agent and a second part of gasifying agent; the first part of gasifying agent is mixed with organic hazardous waste slurry to form a first mixed flow that enters the autothermal entrained flow reactor; the biomass-based powder transported by the carbon dioxide gas flow and the second part of gasifying agent form a second mixed flow that enters the autothermal entrained flow reactor; the second mixed flow is distributed around the first mixed flow.

[0042] In the present invention, the lower calorific value of the organic hazardous waste slurry is preferably ≥10000KJ / kg, specifically 10000-15000KJ / kg, and the density is preferably <1250kg / m 3 , specifically 1000~1250kg / m 3 The water content is preferably less than 50 wt %, more preferably 30 to 46 wt %. The present invention controls the calorific value, density and water content of the organic hazardous waste slurry within the above ranges, thereby facilitating safe and efficient operation of the autothermal entrained flow reactor and improving gasification efficiency.

[0043] In the present invention, the organic hazardous waste slurry is prepared from organic hazardous waste, and the organic hazardous waste preferably includes one or more of waste plastics, waste rubber, waste oil, distillation residue, antibiotic fermentation residue and halogen-containing hydrocarbons; in a specific embodiment of the present invention, the organic hazardous waste is a mixture of distillation residue and antibiotic fermentation residue; the organic hazardous waste is a zero-carbon or negative-carbon input material; the organic hazardous waste is preferably modified and / or formulated to form a homogeneous fluid with rheological properties, namely the organic hazardous waste slurry; specifically, the preparation method of the organic hazardous waste slurry is preferably selected according to the type and characteristics of the organic hazardous waste. For example, when the organic hazardous waste is an acidic liquid hazardous waste, it is preferably neutralized by adding alkaline substances or alkaline organic hazardous waste to adjust the pH value to 6-8 to remove the acidity and corrosiveness of the organic hazardous waste. When the organic hazardous waste is semi-liquid and semi-solid, it is preferably evaporated to obtain a liquid and a solid, and the liquid is recovered as a liquid raw material for preparing the organic hazardous waste slurry. The solid is preferably mixed with the liquid hazardous waste to form the organic hazardous waste slurry. The mixing method is preferably shearing or wet grinding. When the organic hazardous waste is difficult to flow at room temperature, it is preferably heated to make it fluid and achieve pumpability. In the present invention, an auxiliary agent can also be added when preparing the organic hazardous waste slurry. The auxiliary agent is preferably a mixture of a naphthalene-based high-efficiency water reducer, sodium lignin sulfonate, and sodium hydroxide. The mass fraction of the naphthalene-based high-efficiency water reducer in the mixture is preferably 20% to 70%, the mass fraction of the sodium lignin sulfonate is preferably 25% to 75%, and the mass fraction of the sodium hydroxide is preferably 3% to 8%. The present invention improves the pumpability of the organic hazardous waste slurry by adding auxiliary agents to obtain a homogeneous fluid.

[0044] In the present invention, the lower calorific value of the biomass-based powder is preferably ≥18000KJ / Kg, specifically 18000-20000KJ / Kg, and the bulk density is preferably 200-600kg / m 3 , average particle size <0.8mm, moisture content <8wt%. The present invention controls the particle size and moisture content of the biomass-based powder within the above ranges, which is conducive to fluidization and high-pressure transportation of the biomass-based powder. At the same time, due to the small particle size, large specific surface area, and large contact area with the gasifying agent, rapid gasification is easily achieved, and the raw material conversion utilization rate is high.

[0045] In the present invention, the biomass-based powder preferably includes one or more of biomass powder and biochar; the biomass powder is preferably obtained by dehydrating biomass and then crushing it; the dehydration method is preferably drying or baking, and the drying or baking temperature is preferably 100-200°C; the biochar is preferably obtained by pyrolyzing biomass and then crushing it; the pyrolysis temperature is preferably 300-700°C; in the present invention, the biomass preferably includes one or more of agricultural biomass, forestry biomass and biomass fungus residue, specifically one or more of straw, sawdust and bamboo; the biomass has renewable and low-carbon characteristics; in a specific embodiment of the present invention, the biomass-based powder can be a mixture of biochar and biomass powder, specifically a mixture of bamboo charcoal and bamboo powder.

[0046] In the present invention, a central mixer and an outer ring mixer are provided on the top of the autothermal fluidized flow reactor; the outer ring mixers are distributed around the central mixer, preferably evenly distributed around the central mixer; the central mixer and the outer ring mixer are both parallel to the axis of the autothermal fluidized flow reactor; the organic hazardous waste slurry and the first part of the gasification agent are preferably introduced into the autothermal fluidized flow reactor from the central mixer; the biomass-based powder is preferably transported by a carbon dioxide gas flow, and is introduced into the autothermal fluidized flow reactor from the outer ring mixer with the second part of the gasification agent.

[0047] In the present invention, the central mixer is preferably a sleeve-type structure, and the sleeve-type structure forms a feed channel; the feed channels of the central mixer are preferably more than 3, specifically 3 to 5; the organic hazardous waste slurry and the first part of the gasification agent are preferably introduced from different channels of the central mixer respectively. When the central mixer has 3 feed channels, the 3 channels are recorded from the inside to the outside as the inner channel, the middle channel and the outer channel. The gasification agent is preferably introduced into the inner channel and the outer channel, and the organic hazardous waste slurry is preferably introduced into the middle channel; the present invention utilizes a central mixer to feed the organic hazardous waste slurry and the gasification agent. At the outlet of the central mixed gas end, the high-pressure gasification agent can quickly cut and disperse the organic hazardous waste slurry, achieve sufficient mixing of gas and liquid, and thus improve the gasification efficiency.

[0048] In the present invention, the number of the outer ring mixers is preferably three or more, specifically three to six. Each outer ring mixer is preferably formed by nesting two cylindrical structures of different diameters to form a telescopic structure, with the center of the telescopic structure serving as the inner channel and the gap between the two cylindrical structures serving as the outer channel. The biomass-based powder is preferably introduced through the inner channel under the conveyance of a carbon dioxide gas flow, and the second portion of the gasifying agent is preferably introduced through the outer channel. In the present invention, introducing the biomass-based powder through the inner channel of the outer ring mixer effectively prevents the influence of the sleeve support on the conveying process.

[0049] The present invention introduces organic hazardous waste slurry and biomass-based powder from different mixers into a self-heating entrained flow reactor, and can realize the feeding of organic hazardous waste slurry and biomass-based powder in any proportion. If the organic hazardous waste slurry and biomass-based powder are mixed and fed, in order to ensure the pumpability of the slurry entering the furnace, the addition amount of biomass-based powder needs to be less than 30wt%. If the biomass addition amount is too low, it is difficult to realize large-scale use of biomass; if the biomass-based powder addition amount is too high, it is easy to cause the slurry to be unable to flow, difficult to transport, and unable to achieve gasification in the furnace.

[0050] The present invention mixes the organic hazardous waste slurry and the biomass-based powder with the gasifying agent respectively and then passes them into the self-heating fluidized bed reactor, which can achieve uniform dispersion of the organic hazardous waste slurry and the biomass-based powder in the furnace, increase the contact area between the material and the gasifying agent, and improve the gasification efficiency; if the biomass-based powder and the organic hazardous waste slurry are fed into the gasification furnace through different channels of the same burner, the organic hazardous waste slurry and the biomass-based powder are easily mixed at the end of the burner to form larger agglomerated particles, the specific surface area is greatly reduced, the contact area with the gasifying agent is reduced, and complete conversion cannot be achieved in the gasification reaction, the carbon conversion rate is reduced to below 95%, and the raw material utilization efficiency is significantly reduced. Moreover, the present invention feeds the organic hazardous waste slurry and the biomass-based powder separately, and can also facilitate the adjustment of the feed amounts of the organic hazardous waste slurry and the biomass-based powder. The content of H2 and CO in the synthesis gas can be conveniently adjusted by adjusting the ratio of the organic hazardous waste slurry and the biomass-based powder. When preparing synthesis gas with a higher H2 content, the feed amount of the organic hazardous waste slurry can be increased, and when preparing synthesis gas with a higher CO content, the feed amount of the biomass-based powder can be increased.

[0051] In the present invention, the mass ratio of the biomass-based powder and carbon dioxide is preferably 5-20:1, more preferably 10-15:1; the pressure of the carbon dioxide is preferably 0.4-1.5 MPa higher than the pressure of the gasification reaction; the ratio of the total mass of the gasifying agent to the total mass of the organic hazardous waste slurry and the biomass-based powder is preferably 0.4-0.75:1, more preferably 0.5-0.6:1; the pressure of the gasifying agent is preferably 0.4-1.5 MPa higher than the pressure of the gasification reaction and not lower than the pressure of carbon dioxide; specifically, the mass ratio of the first part of the gasifying agent and the organic hazardous waste slurry is preferably 0.5-0.7:1, and the mass ratio of the second part of the gasifying agent and the biomass-based powder is preferably 0.2-0.5:1; the temperature of the gasification reaction is preferably 1200-1500°C, more preferably 1300-1350°C, and the pressure of the gasification reaction is preferably 1-4 MPa, specifically 1-1.15 MPa. In the present invention, after oxygen enters the autothermal entrained flow reactor as a gasifying agent, it undergoes a combustion reaction with C and H in the raw materials, releasing a large amount of heat and forming a high-temperature environment. At the same time, the present invention controls the oxygen flow rate so that some C and H do not react with oxygen, but only form high-temperature C. The high-temperature C undergoes an endothermic reaction with the CO2 entering the furnace to generate the target gas CO of the gasification reaction (C+CO2→2CO). In addition, in the art, conventional gasification reactions use steam as a gasifying agent, utilizing steam to react with high-temperature C to generate the target product gas (C+H2O→CO+H2). If steam is used as a gasifying agent, it needs to be supplied externally, and the source of steam is generated by combustion. The combustion process will emit a large amount of CO2. The present invention uses oxygen as a gasifying agent and uses CO2 as a reaction raw material to reduce overall carbon emissions.

[0052] In the present invention, the gasification obtains a mixture of crude synthesis gas and molten inorganic matter, and the method preferably further comprises: subjecting the mixture to quenching water quenching to obtain water-containing ash synthesis gas and glassy slag; the water-containing ash synthesis gas is preferably subjected to gas-liquid separation to obtain ash-containing synthesis gas; the ash-containing synthesis gas is preferably washed and deashed after infiltration to obtain the synthesis gas; the quenching water quenching, gas-liquid separation and washing and deashing also obtain ash-containing water; the ash-containing water is sequentially subjected to pressure reduction and temperature concentration and negative pressure cooling and concentration, and then filtered to obtain ash slag and recycled water; the content of suspended solids in the recycled water is 30 to 50 mg / L; the ash is preferably returned for use in the preparation of organic hazardous waste slurry; the recycled water is preferably partially used as flushing water for cooling high-temperature gas and slag and flushing glassy slag, and the remaining part is used for inorganic salt recovery. The present invention has no special requirements for the method of recovering the inorganic salt, which can be specifically recovered by evaporation; the present invention controls the suspended matter in the recycled water within the above-mentioned range, which is beneficial to improving the heat exchange efficiency during the recovery of inorganic salts and avoiding the precipitation of suspended matter during the evaporation recovery of inorganic salts; the remaining liquid after recovering the inorganic salts is used as circulating ash water, and the circulating ash water is preferably returned to the washing and deashing step after heating and pressurizing for recycling.

[0053] The present invention also provides a device for preparing synthesis gas using organic hazardous waste and biomass, comprising an autothermal fluidized bed reactor 1; a mixer is provided on the top of the autothermal fluidized bed reactor 1, and the mixer includes a central mixer 2-1 and outer ring mixers 2-2 distributed around the central mixer 2-1; the autothermal fluidized bed reactor 1 is provided with a gas outlet.

[0054] In the present invention, the structure and quantity of the central mixer 2-1 and the outer ring mixer 2-2 are consistent with the above solution and will not be described in detail here.

[0055] In the present invention, the self-heating entrained flow reactor 1 includes a reaction chamber 1-1 and a cooling chamber 1-2 from top to bottom; the lining of the reaction chamber 1-1 is a high temperature resistant and corrosion resistant material with a heat storage function; the bottom of the cooling chamber 1-2 is a water bath area, and a cooling medium distributor 5 is provided on the top of the cooling chamber 1-2; the cooling chamber 1-2 is preferably provided with a downcomer 4 and an upcomer 3, the downcomer 4 is separately nested inside the upcomer 3, and a gap is left between the outer wall of the downcomer 4 and the inner wall of the upcomer 3; the bottoms of the downcomer 4 and the upcomer 3 are preferably immersed in the cooling water in the water bath area. In the present invention, in the reaction chamber 1-1, the raw materials react with the gasifying agent with oxygen to generate synthesis gas (mainly composed of CO and H2). The gasification reaction utilizes the heat released by the combustion of part of the raw materials, which supplies the endothermic gasification reaction, thereby maintaining the heat balance of the gasification reaction. No external heat source is required, energy saving and high efficiency are achieved, and a highly reducing gas with the main components of CO and H2 is generated in the reaction chamber 1-1, which can achieve the toxicity removal of organic hazardous waste. The high-temperature synthesis gas generated by the gasification reaction and the unreacted molten inorganic matter are mixed and flowed into the cooling chamber 1-2 of the autothermal entrained flow reactor. The gas is rapidly cooled and the gas-liquid-solid three-phase separation is carried out in the cooling chamber 1-2. The downcomer 4 provided in the cooling chamber serves as a guide. The gas is directly contacted with the ash water from the cooling medium distributor 5 in the downcomer 4 for cooling. After rapid cooling, the water-insoluble molten inorganic matter automatically sinks into the lower cooling water in the form of glassy slag. The cooled gas and the steam generated by the heated ash water rise out of the cooling chamber 1-2 along the annular gap between the outer wall of the downcomer 4 and the inner wall of the riser 3, becoming a saturated gas containing a small amount of water and fine ash, i.e., the water-ash synthesis gas.

[0056] In the present invention, the bottom of the autothermal entrained flow reactor 1 is preferably connected to the slag collection device 11, and a locking slag valve 10 is preferably provided between the bottom of the autothermal entrained flow reactor 1 and the slag collection device 11; the slag collection device 11 is preferably provided with a flushing water inlet and a circulating slag water outlet, and the circulating slag water outlet is preferably connected to the water bath area at the bottom of the autothermal entrained flow reactor 1; the bottom of the slag collection device 11 is preferably provided with a lower locking slag valve 12; the slag collection device 11 can specifically be a slag collection tank. In the present invention, the glassy slag cooled in the water bath area and the cooling water that has not been converted into steam remain in the water bath at the bottom of the cooling chamber 1-2, and the glassy slag enters the slag collection device 11 through the locking slag valve 10 by gravity and the action of the circulating slag water flow. The upper part of the slag collection device 11 is also connected to flushing water, and the liquid-solid mixture in the slag collection device 11 is regularly discharged through the lower locking slag valve 12 under the action of the flushing water.

[0057] In the present invention, the device preferably also includes a gas-liquid separator 6; the gas-liquid separator 6 is provided with a gas outlet and a liquid outlet; the inlet of the gas-liquid separator 6 is connected to the gas outlet of the autothermal fluidized bed reactor 1; the top of the gas-liquid separator 6 is preferably provided with a first demister 31, and the water-ash-containing synthesis gas enters the gas-liquid separator 6 for gas-liquid separation to obtain ash-containing synthesis gas.

[0058] In the present invention, the device preferably also includes an ash infiltrator 7, the inlet of the ash infiltrator 7 is connected to the gas outlet of the gas-liquid separator 6; the ash-containing synthesis gas enters the ash infiltrator 7 for infiltration, and the fine ash particles entrained in the synthesis gas are forced to be wetted and enlarged through infiltration, which is conducive to the removal of entrained ash in the subsequent scrubber 8.

[0059] In the present invention, the device preferably further includes a scrubber 8, the inlet of the scrubber 8 and the outlet of the ash infiltrator 7 being connected; the lower part of the scrubber 8 is preferably a water bath area, and the water in the water bath area is preferably high-temperature and high-pressure circulating ash water, and the temperature of the high-temperature and high-pressure circulating ash water is preferably 120-200°C, and the pressure is preferably 0.2-0.5MPa higher than the scrubber pressure; the scrubber 8 is preferably provided with a gas guide downpipe 29 and a gas guide uppipe 30, and the gas guide downpipe 29 is preferably separately nested inside the gas guide uppipe 30, and a gap is preferably left between the outer wall of the gas guide downpipe 29 and the inner wall of the gas guide uppipe 30; the bottoms of the gas guide downpipe 29 and the gas guide uppipe 30 are preferably immersed in the water bath at the lower part of the scrubber 8; The scrubber 8 is preferably further provided with a multi-layer tower tray 27 and a second demister 28. The multi-layer tower tray 27 is preferably arranged above the gas guide downcomer 29 and the gas guide upcomer 30. Washing water is preferably introduced into the upper part of the multi-layer tower tray 27, and the washing water preferably comes from the condensate of the downstream process section or external water supply; the second demister 28 is preferably arranged at the top of the scrubber 8; the bottom of the scrubber 8 is preferably conical, and the bottom of the cone is preferably provided with a first ash water outlet for discharging ash-containing water with a high ash content; a second ash water outlet is preferably provided above the area where the lower part of the scrubber 8 is connected to the cone, for discharging ash-containing water with a low ash content; the second ash water outlet is preferably connected to the first pressure pump 9, and the outlet of the first pressure pump 9 is preferably connected to the inlet of the cooling medium distributor 5 and the ash infiltrator 7 respectively. In the present invention, the ash-containing gas after infiltration enters the water bath at the lower part of the scrubber 8 along the gas guide downpipe 29, and then rises along the annular gap between the outer wall of the gas guide downpipe 29 and the inner wall of the gas guide uppipe 30, passes through the multi-layer tower tray 27 and the second demister 28 in sequence, and is discharged from the top of the scrubber 8 to obtain the synthesis gas.

[0060] In the present invention, the device preferably further includes an ash-containing water treatment system; the ash-containing water treatment system includes: a decompression and temperature reducing device 13, the decompression and temperature reducing device 13 being provided with a liquid outlet and a steam outlet; the inlet of the decompression and temperature reducing device 13 receiving external water supply and lower drainage of the cooling chamber 1-2, the gas-liquid separator 6 and the scrubber 8; the decompression and temperature reducing device 13 is operated at a positive pressure, and the operating pressure is preferably 0.1 to 0.5 MPa; a negative pressure decompression device 14, the inlet of the negative pressure decompression device 14 being connected to the liquid outlet of the decompression and temperature reducing device 13, The negative pressure cooler 14 is provided with a liquid outlet and a steam outlet; the operating pressure of the negative pressure cooler 14 is preferably -0.09 to -0.06 MPa; a negative pressure steam condenser 15, the inlet of the negative pressure steam condenser 15 is connected to the steam outlet of the negative pressure cooler 14; a negative pressure steam-water separator 16; the inlet of the negative pressure steam-water separator 16 is connected to the outlet of the negative pressure steam condenser 15, and the negative pressure steam-water separator 16 is provided with a gas outlet and a liquid outlet; a negative pressure generator 17; the negative pressure generator 17 The inlet of the atmospheric pressure steam-water separator 18 is connected to the gas outlet of the negative pressure steam-water separator 16; the atmospheric pressure steam-water separator 18; the inlet of the atmospheric pressure steam-water separator 18 is connected to the outlet of the negative pressure generator 17, and the top of the atmospheric pressure steam-water separator 18 is preferably connected to the atmosphere; the sedimentation buffer device 19, the inlet of the sedimentation buffer device 19 is connected to the liquid outlet of the negative pressure cooler 14, and the pipeline connecting the inlet of the sedimentation buffer device 19 and the liquid outlet of the negative pressure cooler 14 is preferably provided with a liquid level control valve 32, the sedimentation buffer device 19 Specifically, it can be a sedimentation buffer tank; a filter device 21, the inlet of the filter device 21 is connected to the outlet of the sedimentation buffer device 19, and a slag water pump 20 is preferably provided on the pipeline connecting the inlet of the filter device 21 and the outlet of the sedimentation buffer device 19; a circulating gray water device 22, the inlet of the circulating gray water device 22 is respectively connected to the liquid outlet of the filter device 21, the liquid outlet of the negative pressure steam-water separator 16 and the liquid outlet of the normal pressure steam-water separator 18; the circulating gray water device 22 is specifically a circulating gray water tank.

[0061] In the present invention, the ash-containing water treatment system preferably also includes an ash water pump 23, an inorganic salt recovery device 24, a heat recovery device 25 and a second pressure pump 26; the inlet of the ash water pump 23 is connected to the outlet of the circulating ash water device 22, and the outlet of the ash water pump 23 is respectively connected to the flushing water inlet of the slag collection device 11 and the inlet of the inorganic salt recovery tank 24; the inlet of the heat recovery device 25 is respectively connected to the steam outlet at the top of the depressurizer 13 and the liquid outlet of the inorganic salt recovery device 24; the inlet of the second pressure pump 26 is connected to the outlet of the heat recovery device 25, and the outlet of the second pressure pump 26 is connected to the water bath area at the lower part of the scrubber 8.

[0062] In the present invention, the ash-containing water generated in the water bath of the cooling chamber 1-2, the ash-containing water in the lower part of the gas-liquid separator 6, and the ash-containing water with high ash content at the bottom of the water bath of the scrubber 8 are all discharged to the ash-containing water treatment system. In a specific embodiment of the present invention, the ash-containing water generated in the water bath of the cooling chamber 1-2, the ash-containing water in the lower part of the gas-liquid separator 6, and the ash-containing water with high ash content at the bottom of the water bath of the scrubber 8 can be directly discharged into the depressurizer 13, or can be discharged into the depressurizer 13 after being reduced in pressure by a pressure reducing valve; the ash-containing water with low ash content in the upper part of the water bath of the scrubber 8 is pressurized by the first pressure pump 9 and partially sent to the cooling medium distributor 5, and is evenly distributed on the inner wall of the downcomer 4 under the action of the cooling medium distributor 5, so as to quickly cool the gas and slag out of the reaction chamber 1-1; the remaining part is sent to the ash infiltrator 7 as infiltration water.

[0063] In the present invention, the ash-containing water treatment system is used to recover heat from the ash-containing water, realize water-ash separation, and recycle the inorganic salts dissolved in the water. Specifically, the ash-containing water discharged from the cooling chamber 1-2, the ash-containing water discharged from the gas-liquid separator 6, and the ash-containing water discharged from the scrubber 8 (ash-containing water with high ash content) enter the depressurizer 13. The steam generated in the depressurizer 13 is washed and deashed by the condensate of the downstream section or external water supply and then discharged from the top into the heat recovery device 25. The non-condensable gas in the steam is discharged from the top of the heat recovery device 25 to recover heat through combustion; the concentrated ash water generated at the bottom of the depressurizer 13 enters the negative pressure cooler 14, where it is cooled and The ash water is concentrated twice, and the slag water discharged from the bottom of the slag collection device 11 together with the external slag is also passed into the negative pressure cooler 14; the negative pressure in the negative pressure cooler 14 comes from the negative pressure generator 17; the negative pressure steam condenser 15 cools the high-temperature steam from the negative pressure cooler 14 and condenses it into liquid water; the negative pressure steam-water separator 16 separates the steam-water mixture produced in the negative pressure steam condenser 15; the atmospheric pressure steam-water separator 18 separates the steam-water mixture again after passing through the negative pressure generator 17. The secondary concentrated ash water generated by the negative pressure cooler 14 flows by gravity into the sedimentation buffer device 19 through the liquid level control valve 32, and is sent to the filter device 21 for separation of ash and water after being pressurized by the slag water pump 20. The separated ash is returned to the preparation of organic hazardous waste slurry; the separated water enters the circulating ash water device 22, is mixed with the water discharged from the lower part of the negative pressure steam-water separator 16 and the water discharged from the normal pressure steam-water separator 18, and is pressurized by the ash water pump 23. Part of the pressurized ash water returns to the slag collection device 11 for use as flushing water, and part is sent to the inorganic salt recovery device 24 to recover the soluble inorganic salts therein. The remaining ash water after the inorganic salt is recovered is sent to the heat recovery device 25 as circulating ash water; the circulating ash water is heated by the heat recovery device 25 and pressurized by the second pressure pump 26 to obtain high-temperature and high-pressure circulating ash water; the high-temperature and high-pressure circulating ash water is returned to the scrubber 8 for use.

[0064] The following will be combined with the embodiments of the present invention to clearly and completely describe the technical solutions of the present invention. Obviously, the embodiments described are only some embodiments of the present invention, not all embodiments. Based on the embodiments of the present invention, all other embodiments obtained by ordinary technicians in this field without making creative efforts are within the scope of protection of the present invention.

[0065] Example 1

[0066] use Figure 1 and Figure 2 The device in the gasification process is used to gasify organic hazardous waste and biomass to produce synthesis gas. The specific steps are as follows:

[0067] The preparation method of organic hazardous waste slurry is as follows: distillation residue and antibiotic fermentation residue are mixed in a mass ratio of 4:6, and then the pH value is adjusted to 7, and then mixed with water to form organic hazardous waste slurry. The main components of the organic hazardous waste slurry are water, organic matter containing carbon, hydrogen, oxygen, nitrogen, sulfur and some inorganic metal salts. The lower calorific value of the organic hazardous waste slurry is 11000KJ / kg, the water content is 46wt%, and the slurry density is 1120kg / m 3 .

[0068] The preparation method of the biomass-based powder comprises the following steps: mixing bamboo charcoal powder (obtained by grinding bamboo after pyrolysis) with bamboo powder (obtained by grinding bamboo after roasting) to obtain the biomass-based powder, wherein the mass fraction of the bamboo charcoal powder is 85% and the mass fraction of the bamboo powder is 15%. The biomass-based powder has a particle size of less than 0.8 mm, a moisture content of less than 8 wt%, a lower calorific value of 22,000 kJ / kg, and a bulk density of 520 kg / m 3 .

[0069] The organic hazardous waste slurry and oxygen are fed into the central mixer 2-1 at the top of the autothermal fluidized bed reactor 1. The central mixer 2-1 is a three-channel sleeve structure. Oxygen is introduced into the inner and outer channels of the central mixer 2-1, and the organic hazardous waste slurry is introduced into the middle channel. The biomass-based powder is fed into the outer ring mixer 2-2 at the top of the autothermal fluidized bed reactor 1 under high-pressure CO2 transportation. The outer ring mixer is provided in three sets, evenly distributed around the central mixer 2-1. The outer ring mixer 2-2 is a two-channel structure, wherein the inner channel is the biomass powder transported by the CO2 airflow, and the outer channel is oxygen. The central mixer 2-1 and the outer ring mixer 2-2 are both axially parallel to the reaction chamber 1-1 of the autothermal fluidized bed reactor 1. Among them, the flow rate of the organic hazardous waste slurry into the furnace is 150kg / h, and the pressure into the furnace is 1.2Mpa; the flow rate of the biomass-based powder into the furnace is 100kg / h, and the CO2 transportation flow rate is 5Nm 3 / h, pressure is 1.5MPa; oxygen pressure is 1.5MPa, total flow rate is 90Nm 3 / h, the oxygen is divided into two parts, the first part is introduced from the central mixer 2-1, and the second part is introduced from the outer ring mixer, and the flow ratio of the first part of oxygen to the second part of oxygen is 2:1; the gasification pressure is 1.0 MPa, and the gasification temperature is 1300℃.

[0070] In the reaction chamber 1-1 of the autothermal entrained flow reactor 1, hazardous organic waste and biomass undergo gasification reaction, and the generated high-temperature synthesis gas and the unreacted molten inorganic matter are mixed and flowed into the cooling chamber 1-2 of the autothermal entrained flow reactor 1. In the downcomer 4 of the cooling chamber 1-2, the downcomer is directly contacted with the ash water from the cooling medium distributor 5 for cooling. After rapid cooling, the molten inorganic matter insoluble in water automatically sinks into the lower water bath in the form of glassy slag. The cooled gas and the steam generated by the heated ash water rise along the annular gap between the outer wall of the downcomer 4 and the inner wall of the riser 3. The ash-containing synthesis gas rises out of the cooling chamber 1-2 to obtain water-containing ash synthesis gas; the water-containing ash synthesis gas enters the gas-liquid separator 5 for gas-liquid separation, and the obtained ash-containing gas enters the ash impregnator 6. The ash-containing gas after impregnation and humidification enters the scrubber 8, and enters the water bath at the bottom of the scrubber 8 along the gas guide downpipe 29. The gas then rises along the annular gap between the outer wall of the gas guide downpipe 29 and the inner wall of the gas guide uppipe 30, passes through the multi-layer tower tray 27 and the second demister 28 in sequence, and is discharged from the top of the scrubber 8 to obtain synthesis gas. The total flow rate of the generated synthesis gas is 251.5Nm 3 / h.

[0071] The cooled glassy slag and the cooling water that has not been converted into steam remain in the water bath at the bottom of the cooling chamber 1-2. The glassy slag is carried into the slag collecting device 11 by gravity and the flow of circulating slag water. The upper part of the slag collecting device 11 is simultaneously connected to flushing water. Under the action of the flushing water, the liquid-solid mixture in the slag collecting device 11 is regularly discharged through the lower slag lock valve 12.

[0072] The ash-containing water generated in the water bath of the cooling chamber 1-2, the ash-containing water at the bottom of the gas-liquid separator 6, and the ash-containing water with high ash content at the bottom of the water bath of the scrubber 8 are all discharged to the ash-containing water treatment system. The ash-containing water with low ash content at the upper part of the water bath of the scrubber 8 is pressurized by the first pressure pump 9 and sent to the cooling medium distributor 5. Under the action of the cooling medium distributor 5, the water is evenly distributed on the inner wall of the downcomer 4, so as to quickly cool the gas and slag leaving the reaction chamber 1-1; the remaining part is sent to the ash infiltrator as infiltration water.

[0073] The ash-containing water discharged from the cooling chamber 1-2, the ash-containing water discharged from the gas-liquid separator 6, and the ash-containing water discharged from the scrubber 8 (ash-containing water with high ash content) are respectively depressurized and enter the depressurizer 13. The steam generated in the depressurizer 13 is washed and ash-removed and then discharged from the top to the heat recovery device 25. The non-condensable gas in the steam is discharged from the top of the heat recovery device 25 and burned to recover heat; the once concentrated ash water generated at the lower part of the depressurizer 13 enters the negative pressure desuperheater 14, where it is cooled again and concentrated for a second time. At the same time, the slag water discharged from the bottom of the slag collection device 11 together with the discharged slag is also passed into the negative pressure desuperheater 14; the negative pressure steam condenser 15 cools the high-temperature steam from the negative pressure desuperheater 14 and condenses it into liquid water; the negative pressure steam-water separator 16 separates the steam-water mixture generated in the negative pressure steam condenser 15; and the atmospheric pressure steam-water separator 18 separates the steam-water mixture again after passing through the negative pressure generator 17. The secondary concentrated ash water generated by the negative pressure cooler 14 flows by gravity into the sedimentation buffer device 19 through the liquid level control valve 32, and is sent to the filter device 21 for separation of ash and water after being pressurized by the slag water pump 20. The separated ash is returned to the preparation of organic hazardous waste slurry; the separated recycled water (wherein the content of suspended solids is 30-50 mg / L) enters the circulating ash water device 22, is mixed with the water discharged from the lower part of the negative pressure steam-water separator 16 and the water discharged from the normal pressure steam-water separator 18, and is pressurized by the ash water pump 23. Part of the pressurized ash water returns to the slag collection device 11 for use as flushing water, and part is sent to the inorganic salt recovery device 24 to recover the soluble inorganic salts therein. The remaining ash water after the inorganic salt is recovered is sent to the heat recovery device 25 as circulating ash water; the circulating ash water is heated by the heat recovery device 25 and pressurized by the second pressure pump 26 to obtain high-temperature and high-pressure circulating ash water; the high-temperature and high-pressure circulating ash water is returned to the scrubber 8 for use.

[0074] The main components of the synthesis gas obtained in this example are shown in Table 1:

[0075] Table 1 Main components of the synthesis gas obtained in Example 1

[0076] Gas composition Volume percentage (VOL%) <![CDATA[Equivalent flow rate (Nm 3 / h)]]> CO 51.61 129.8 <![CDATA[H2]]> 30.3 76.2 <![CDATA[CO2]]> 18.01 45.3 <![CDATA[CH4]]> 0.0795 0.2 other trace / total / 251.5

[0077] According to the material balance calculation, the C conversion rate of the incoming materials is 98.23%.

[0078] Example 2

[0079] The other conditions are the same as those in Example 2, except that the flow rate of organic hazardous waste into the furnace is 100 kg / h, the pressure into the furnace is 1.35 MPa, the flow rate of biomass-based powder into the furnace is 150 kg / h, and the CO2 delivery flow rate is 7 Nm 3 / h, pressure is 1.6MPa; oxygen pressure is 1.7MPa, total flow rate is 85Nm 3 / h, the oxygen is divided into two parts, the first part is introduced from the central mixer 2-1, and the second part is introduced from the outer ring mixer, the flow ratio of the first oxygen and the second part of the oxygen is 0.9:1; the gasification pressure is 1.15MPa, and the gasification temperature is 1350℃.

[0080] The total flow rate of the synthesis gas obtained in this example is 258.6Nm 3 / h, the main components are shown in Table 2:

[0081] Table 2 Main components of the synthesis gas obtained in Example 2

[0082]

[0083]

[0084] According to the material balance calculation, the C conversion rate of the incoming materials is 98.56%.

[0085] Comparative Example 1

[0086] The types of raw materials, reaction temperature, pressure, and conditions for feeding the raw materials into the furnace are the same as those in Example 1. The only difference is that a single burner is used to feed the biomass-based powder and organic hazardous waste slurry through different channels, where the outermost ring is the epoxy channel, and from the outside to the inside are the biomass-based powder channel, the organic hazardous waste slurry channel, and the inner epoxy channel.

[0087] The total flow rate of the synthesis gas obtained in this example is 232.15Nm 3 / h, the main components are shown in Table 3:

[0088] Table 3 Main components of the synthesis gas obtained in Comparative Example 1

[0089] Gas composition Volume percentage (VOL%) <![CDATA[Equivalent flow rate (Nm 3 / h)]]> CO 49.03 113.82 <![CDATA[H2]]> 28.6 66.39 <![CDATA[CO2]]> 22.01 51.1 <![CDATA[CH4]]> 0.12 0.28 other trace / total / 232.15

[0090] According to the material balance calculation, the C conversion rate in the furnace material is 92.52%.

[0091] According to the above embodiments and comparative examples, it can be seen that the present invention feeds biomass-based powder and organic hazardous waste slurry separately, which can achieve independent atomization of the slurry and powder, and at the same time has a reaction coupling effect, effectively increasing the content of CO and H2 in the synthesis gas, and significantly improving the gasification efficiency.

[0092] The above is only a preferred embodiment of the present invention. It should be pointed out that for ordinary technicians in this technical field, several improvements and modifications can be made without departing from the principles of the present invention. These improvements and modifications should also be regarded as within the scope of protection of the present invention.

Claims

1. A method for preparing synthesis gas using organic hazardous waste and biomass, characterized in that: The following steps are involved: The organic hazardous waste slurry, biomass-based powder and gasifying agent are introduced into an autothermal entrained flow reactor for gasification reaction to obtain synthesis gas; the gasifying agent is oxygen; The gasifying agent is divided into a first part of gasifying agent and a second part of gasifying agent; the first part of gasifying agent is mixed with the organic hazardous waste slurry to form a first mixed flow that enters the autothermal entrained flow reactor; the biomass-based powder conveyed by the carbon dioxide gas flow and the second part of gasifying agent form a second mixed flow that enters the autothermal entrained flow reactor; The second mixed flow is distributed around the periphery of the first mixed flow.

2. The method according to claim 1, characterized in that The top of the autothermal entrained flow reactor is provided with a central mixer and an outer ring mixer; the outer ring mixers are distributed around the central mixer; the organic hazardous waste slurry and the first part of the gasifying agent are introduced into the autothermal entrained flow reactor from the central mixer; The biomass-based powder is transported by a carbon dioxide gas flow and introduced into the autothermal entrained flow reactor together with a second portion of a gasifying agent from an outer ring mixer.

3. The method according to claim 2, characterized in that The central mixer is a sleeve-type structure, which forms a feed channel; the central mixer has more than three feed channels; the organic hazardous waste slurry and the first part of the gasifying agent are respectively introduced into different feed channels of the central mixer; The number of the outer ring mixers is more than 3; each outer ring mixer is formed by two cylindrical structures with different diameters nested together to form a telescopic structure, the center of the telescopic structure is the inner channel, and the gap between the two cylindrical structures is the outer channel; the biomass-based powder is introduced into the inner channel under the transport of carbon dioxide gas flow, and the second part of the gasifying agent is introduced into the outer channel.

4. The method according to claim 1, wherein The lower calorific value of the organic hazardous waste slurry is ≥10000KJ / kg and the density is <1250kg / m 3 , moisture content <50wt%; The biomass-based powder has a lower calorific value of ≥18000KJ / Kg and a bulk density of 200-600kg / m 3 , average particle size <0.8mm, moisture content <8wt%; the biomass-based powder includes one or more of biomass powder and biomass charcoal.

5. The method according to claim 1, wherein The mass ratio of the biomass-based powder to carbon dioxide is 5 to 20:1; the ratio of the total mass of the gasifying agent to the total mass of the organic hazardous waste slurry and the biomass-based powder is 0.4 to 0.75:1; The temperature of the gasification reaction is 1200-1500° C., and the pressure is 1-4 MPa.

6. The method according to claim 1, wherein The gasification produces a mixture of crude synthesis gas and molten inorganic matter, and the method further comprises: subjecting the mixture to water quenching to produce hydrous ash synthesis gas and glassy slag; The water-ash-containing synthesis gas is subjected to gas-liquid separation to obtain the ash-containing synthesis gas; the ash-containing synthesis gas is washed and deashed after being infiltrated to obtain the synthesis gas; The quenching water quenching, gas-liquid separation and washing and ash removal also produce ash-containing water; the ash-containing water is sequentially subjected to pressure reduction and temperature concentration and negative pressure temperature reduction and concentration, and then filtered to obtain ash residue and recovered water; the content of solid suspended matter in the recovered water is 30-50 mg / L.

7. A device for producing synthesis gas using organic hazardous waste and biomass, characterized in that: The invention comprises an autothermal fluidized bed reactor (1); a mixer is provided on the top of the autothermal fluidized bed reactor (1), and the mixer comprises a central mixer (2-1) and outer ring mixers (2-2) distributed around the central mixer (2-1); and the autothermal fluidized bed reactor (1) is provided with a gas outlet.

8. The device according to claim 7, characterized in that The autothermal fluidized bed reactor (1) comprises, from top to bottom, a reaction chamber (1-1) and a cooling chamber (1-2); the bottom of the cooling chamber (1-2) is a water bath area, and a cooling medium distributor (5) is provided on the top of the cooling chamber (1-2); a downcomer (4) and an upcomer (3) are provided in the cooling chamber (1-2), and the downcomer (4) is separately nested inside the upcomer (3).

9. The device according to claim 7 or 8, characterized in that It also includes: a gas-liquid separator (6); the gas-liquid separator (6) is provided with a gas outlet and a liquid outlet; the inlet of the gas-liquid separator (6) is connected to the gas outlet of the autothermal entrained flow reactor (1); an ash infiltrator (7), the inlet of the ash infiltrator (7) being in communication with the gas outlet of the gas-liquid separator (6); A scrubber (8), wherein the inlet of the scrubber (8) is communicated with the outlet of the ash wetting device (7).

10. The device according to claim 9, characterized in that The system also includes an ash-containing water treatment system; the ash-containing water treatment system includes a pressure-reducing and temperature-reducing device (13); the pressure-reducing and temperature-reducing device (13) is provided with a liquid outlet and a steam outlet; the inlet of the temperature-reducing and pressure-reducing device (13) receives external water supply and lower drainage of the cooling chamber (1-2), the gas-liquid separator (6) and the scrubber (8); A negative pressure cooler (14), wherein the inlet of the negative pressure cooler (14) is connected to the liquid outlet of the pressure reducing cooler (13); the negative pressure cooler (14) is provided with a liquid outlet and a steam outlet; a negative pressure steam condenser (15), wherein the inlet of the negative pressure steam condenser (15) is connected to the steam outlet of the negative pressure cooler (14); A negative pressure steam-water separator (16); the inlet of the negative pressure steam-water separator (16) is connected to the outlet of the negative pressure steam condenser (15); the negative pressure steam-water separator (16) is provided with a gas outlet and a liquid outlet; A negative pressure generator (17); the inlet of the negative pressure generator (17) is connected to the gas outlet of the negative pressure steam-water separator (16); Atmospheric pressure steam-water separator (18); the inlet of the atmospheric pressure steam-water separator (18) is connected to the outlet of the negative pressure generator (17); a sedimentation buffer device (19); an inlet of the sedimentation buffer device (19) is connected to a liquid outlet of the negative pressure cooler (14); A filtering device (21); the inlet of the filtering device (21) is connected to the outlet of the sedimentation buffer device (19); A circulating grey water device (22); the inlet of the circulating grey water device (22) is respectively connected to the liquid outlet of the filtering device (21), the liquid outlet of the negative pressure steam-water separator (16), and the liquid outlet of the normal pressure steam-water separator (18).

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