Method and device for preparing synthesis gas by using organic hazardous waste and biomass

Abstract

The present application relates to solid waste treatment technical field, provide a kind of preparation syngas method and device using organic dangerous waste and biomass.The present application uses organic dangerous waste and biomass as raw material, preparation syngas by self-heating type gas flow bed.The present application will be organic dangerous waste slurry and biomass-based powder respectively feed, can realize the feed adjustment of arbitrary ratio, organic dangerous waste processing capacity, gasification efficiency is high, carbon emission is low;While this feeding mode can realize the independent atomization of organic dangerous waste slurry and biomass-based powder, also has the coupling effect of reaction, can improve gasification efficiency and the content of effective component in syngas.Summarized above, the present application uses organic dangerous waste and biomass to prepare syngas, can realize the efficient treatment and resource utilization of organic dangerous waste and biomass simultaneously, reduce fossil energy consumption, while carbon emission is less, environmental pollution is small, the obtained syngas can be used to prepare a variety of high value-added products, with remarkable environmental and economic benefits, wide application prospect.

Description

Technical Field

[0001] This invention relates to the field of solid waste treatment technology, and in particular to a method and apparatus for preparing syngas using organic hazardous waste and biomass. Background Technology

[0002] Organic hazardous waste refers to organic waste generated during industrial production that possesses certain risks, such as waste plastics, waste rubber, waste oil, and distillation residues. Organic hazardous waste is characterized by its complex composition, poor biodegradability, and toxicity, making its treatment difficult. Currently, the main treatment methods are incineration or landfill. However, incineration cannot treat some organic hazardous wastes and easily generates highly toxic organic pollutants such as dioxins, as well as air pollutants such as nitrogen oxides and sulfur oxides, potentially causing secondary pollution. Landfilling carries the risk of leakage, has a long treatment cycle, and requires large areas of land for construction. With urban development and the increasing generation of organic hazardous waste, suitable landfill sites are becoming increasingly difficult to obtain.

[0003] Gasification is a novel method for treating organic hazardous waste, offering high levels of harmlessness and significant volume reduction, making it highly promising for application. Currently, water-coal slurry gasifiers are commonly used for the co-treatment of organic hazardous waste. This method requires mixing organic hazardous waste and coal to create a water-coal slurry, which is then fed into the gasifier along with oxygen. Under high temperature and pressure, the organic hazardous waste undergoes a series of physical and chemical reactions within the gasifier, being decomposed, gasified, and converted into products such as syngas and slag. However, this method can only replace a portion of the coal with organic hazardous waste, resulting in a small amount of organic hazardous waste added, high petrochemical energy consumption, and low gasification efficiency. Summary of the Invention

[0004] In view of this, the present invention provides a method and apparatus for preparing syngas using organic hazardous waste and biomass. The present invention uses organic hazardous waste and biomass as raw materials to prepare syngas through a self-heating fluidized bed reactor, reducing the consumption of fossil fuels, providing a large capacity for treating organic hazardous waste, high gasification efficiency, and low carbon emissions.

[0005] To achieve the above-mentioned objectives, the present invention provides the following technical solution:

[0006] A method for producing syngas using organic hazardous waste and biomass includes the following steps:

[0007] Organic hazardous waste slurry, biomass-based powder, and gasifying agent are fed into a self-heating fluidized bed reactor for gasification to obtain syngas; the gasifying agent is oxygen.

[0008] The gasifying agent is divided into a first gasifying agent and a second gasifying agent; the first gasifying agent is mixed with organic hazardous waste slurry to form a first mixed flow which enters the self-heating fluidized bed reactor; the biomass-based powder transported by carbon dioxide gas flow and the second gasifying agent form a second mixed flow which enters the self-heating fluidized bed reactor; the second mixed flow is distributed around the first mixed flow.

[0009] Preferably, the self-heating fluidized bed reactor is provided with a central mixer and an outer ring mixer at the top; the outer ring mixer is distributed around the central mixer; the organic hazardous waste slurry and the first part of the gasification agent are introduced into the self-heating fluidized bed reactor through the central mixer;

[0010] The biomass-based powder is transported by a carbon dioxide gas stream and, together with the second part of the gasifying agent, is introduced into the self-heating fluidized bed reactor from the outer ring mixer.

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

[0012] The number of outer ring mixers is three or more; each outer ring mixer consists of two nested cylindrical structures of different diameters forming a sleeve structure, with the center of the sleeve structure being the inner channel and the gap between the two cylindrical structures being the outer channel; the biomass-based powder is introduced through the inner channel under the transport of carbon dioxide gas flow, and the second part of the gasifying agent is introduced through the outer channel.

[0013] Preferably, the organic hazardous waste slurry has a lower heating value ≥10000 KJ / kg and a density <1250 kg / m³. 3 Moisture content <50wt%;

[0014] The biomass-based powder has a lower heating value ≥18000KJ / Kg and a bulk density of 200~600kg / m³. 3 The average particle size is <0.8 mm, and the moisture content is <8 wt%.

[0015] Preferably, the mass ratio of the biomass-based powder to carbon dioxide is 5–20:1; 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 0.4–0.75:1.

[0016] The temperature of the gasification reaction is 1200–1500℃, and the pressure is 1–4 MPa.

[0017] Preferably, the gasification yields a mixture of crude syngas and molten inorganic matter, and the method further includes: subjecting the mixture to rapid water quenching to obtain aqueous ash syngas and glassy slag;

[0018] The water-containing ash syngas is subjected to gas-liquid separation to obtain ash-containing syngas; the ash-containing syngas is then wetted and washed to remove ash, thus obtaining the syngas.

[0019] The quenching, gas-liquid separation, and washing and ash removal processes also yield ash-containing water. The ash-containing water is then subjected to depressurization and cooling for concentration and negative pressure cooling for concentration, followed by filtration to obtain ash residue and recycled water. The content of suspended solids in the recycled water is 30–50 mg / L.

[0020] The present invention also provides an apparatus for producing syngas from organic hazardous waste and biomass, comprising a self-heating fluidized bed reactor; a mixer is provided at the top of the self-heating fluidized bed reactor, the mixer comprising a central mixer and an outer ring mixer distributed around the central mixer; the self-heating 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 a riser are provided inside the cooling chamber, and the downcomer is separately nested inside the riser.

[0022] Preferably, the apparatus further includes: 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 self-heating fluidized bed reactor;

[0023] A dust impregnator, wherein the inlet of the dust impregnator is connected to the gas outlet of the gas-liquid separator;

[0024] A washer, the inlet of which is connected to the outlet of the ash impregnator.

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

[0026] A negative pressure cooling device, wherein the inlet of the negative pressure cooling device is connected to the liquid outlet of the negative pressure cooling device; the negative pressure cooling device 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] Negative pressure generator; the inlet of the negative pressure generator is connected to the gas outlet of the negative pressure steam-water separator;

[0030] An 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 settling buffer device; the inlet of the settling buffer device is connected to the liquid outlet of the negative pressure cooler;

[0032] Filtering device; the inlet of the filtering device is connected to the outlet of the settling buffer device;

[0033] The circulating ash water device has its inlet connected to the liquid outlet of the filter device, the liquid outlet of the negative pressure steam-water separator, and the liquid outlet of the normal pressure steam-water separator.

[0034] This invention provides a method for preparing syngas using organic hazardous waste and biomass, comprising the following steps: passing organic hazardous waste slurry, biomass-based powder, and a gasifying agent into a self-heating fluidized bed reactor for gasification reaction to obtain syngas; the gasifying agent is oxygen; the gasifying agent is divided into a first gasifying agent and a second gasifying agent; the first gasifying agent is mixed with the organic hazardous waste slurry to form a first mixed stream which enters the self-heating fluidized bed reactor; the biomass-based powder and the second gasifying agent, transported by carbon dioxide gas flow, form a second mixed stream which enters the self-heating fluidized bed reactor; the second mixed stream is distributed around the first mixed stream. This invention uses organic hazardous waste and biomass as raw materials to produce syngas through a self-heating fluidized bed reactor, eliminating the need for petrochemical resources during the reaction. The invention feeds the organic hazardous waste slurry and biomass-based powder separately, allowing for arbitrary ratio adjustments. It achieves high processing capacity of organic hazardous waste, high gasification efficiency, and low carbon emissions. Furthermore, the invention mixes the organic hazardous waste slurry and gasifying agent in a central mixer, while the biomass-based powder and gasifying agent are mixed and fed from an outer ring mixer. This feeding method enables independent atomization of the organic hazardous waste slurry and biomass-based powder, while also providing a reaction coupling effect. This improves the uniformity of the organic waste slurry and biomass-based powder within the reactor, preventing the formation of large agglomerates, thereby further improving gasification efficiency and increasing the effective components in the resulting syngas. The content of CO and H2 is significantly increased. In addition, the organic hazardous waste used in this invention is a zero-carbon or negative-carbon raw material. Biomass has low-carbon characteristics, which is conducive to reducing the content of greenhouse gases such as CO2 in syngas. At the same time, this invention uses carbon dioxide to transport biomass-based powder. Carbon dioxide is used as both transport gas and reactant in the reaction (C + CO2 → 2CO), which can further reduce the amount of carbon dioxide emissions in the entire treatment process. Furthermore, conventional gasification reactions use steam as a gasifying agent, which is generated by combustion and emits a large amount of CO2. This invention uses oxygen as a gasifying agent and CO2 as a reactant, which can reduce overall carbon emissions. The molar ratio of carbon dioxide equivalent to hydrogen equivalent (CO2e / H2) certified by carbon footprint is much lower than that of syngas produced by fossil fuel gasification.

[0035] In summary, this invention utilizes organic hazardous waste and biomass to produce syngas, achieving efficient treatment and resource utilization of both simultaneously. This reduces pollution from landfilling and incineration, lowers fossil fuel consumption, and results in low carbon emissions and minimal environmental pollution. The syngas produced has a high content of effective components and can be used to prepare various high-value-added products (methanol, ammonia, high-purity hydrogen, SAF, etc.) or as a clean fuel for power generation or heating, yielding high economic benefits. Therefore, the method provided by this invention has significant environmental and economic benefits and broad application prospects. Attached Figure Description

[0036] Figure 1 A schematic diagram of the apparatus for producing syngas from organic hazardous waste and biomass provided by the present invention;

[0037] Figure 2 This is a schematic diagram of the greywater treatment system;

[0038] Figures 1-2 In the middle: 1—Self-heating fluidized bed reactor, 1-1—Reaction chamber, 1-2—Cooling chamber, 2-1—Central mixer, 2-2—Outer ring mixer, 3—Rising pipe, 4—Downcomer, 5—Cooling medium distributor, 6—Gas-liquid separator, 7—Ash impregnator, 8—Scrubber, 9—First pressurizing pump, 10—Upper slag valve, 11—Slag collection device, 12—Lower slag valve, 13—Pressure reducing and cooling device, 14—Negative pressure cooling device, 15—Negative pressure steam condenser, 1 6—Negative pressure steam-water separator, 17—Negative pressure generator, 18—Atmospheric pressure steam-water separator, 19—Sedimentation buffer device, 20—Slag water pump, 21—Filter device, 22—Circulating ash water device, 23—Ash water pump, 24—Inorganic salt recovery device, 25—Heat recovery device, 26—Second pressurizing pump, 27—Multi-layer tray, 28—Second demister, 29—Gas guide downpipe, 30—Gas guide uppipe, 31—First demister, 32—Liquid level control valve. Detailed Implementation

[0039] This invention provides a method for preparing syngas using organic hazardous waste and biomass, comprising the following steps:

[0040] Organic hazardous waste slurry, biomass-based powder, and gasifying agent are fed into a self-heating fluidized bed reactor for gasification to obtain syngas; the gasifying agent is oxygen.

[0041] The gasifying agent is divided into a first gasifying agent and a second gasifying agent; the first gasifying agent is mixed with organic hazardous waste slurry to form a first mixed flow which enters the self-heating fluidized bed reactor; the biomass-based powder transported by carbon dioxide gas flow and the second gasifying agent form a second mixed flow which enters the self-heating fluidized bed reactor; the second mixed flow is distributed around the first mixed flow.

[0042] In this invention, the lower heating value of the organic hazardous waste slurry is preferably ≥10000 KJ / kg, specifically 10000~15000 KJ / kg, and the density is preferably <1250kg / m³. 3 Specifically, it can be 1000-1250 kg / m³ 3 The moisture content is preferably <50wt%, more preferably 30-46wt%. This invention controls the calorific value, density, and moisture content of the organic hazardous waste slurry within the above range, which facilitates the safe and efficient operation of the self-heating fluidized bed reactor and improves gasification efficiency.

[0043] In this invention, the organic hazardous waste slurry is prepared from organic hazardous waste, which preferably includes one or more of waste plastics, waste rubber, waste oil, distillation residue, antibiotic fermentation residue, and halogenated hydrocarbons. In a specific embodiment of this 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, which is 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 acidic liquid hazardous waste, it is preferable to neutralize it by adding alkaline substances or alkaline organic hazardous waste to adjust the pH value to 6-8, thereby removing the acidity and corrosiveness of the organic hazardous waste. The invention addresses the following: When the organic hazardous waste is semi-liquid and semi-solid, it is preferable to evaporate the semi-liquid and semi-solid hazardous waste to obtain liquid and solid, with the liquid being recycled as a liquid raw material for preparing organic hazardous waste slurry; the solid is preferably mixed with the liquid hazardous waste to form organic hazardous waste slurry; the mixing method is preferably shearing or wet milling; when the organic hazardous waste is difficult to flow at room temperature, it is preferable to heat it to make it flowable and achieve pumpability; in this invention, additives can also be added when preparing the organic hazardous waste slurry, preferably a mixture of naphthalene-based high-efficiency water-reducing agent, sodium lignosulfonate, and sodium hydroxide, wherein the mass fraction of the naphthalene-based high-efficiency water-reducing agent in the mixture is preferably 20%–70%, the mass fraction of sodium lignosulfonate is preferably 25%–75%, and the mass fraction of sodium hydroxide is preferably 3%–8%. This invention improves the pumpability of organic hazardous waste slurry by adding additives, resulting in a homogeneous fluid.

[0044] In this invention, the lower heating value of the biomass-based powder is preferably ≥18000 KJ / Kg, specifically 18000~20000 KJ / Kg, and the bulk density is preferably 200~600 kg / m³. 3 The average particle size is <0.8mm and the moisture content is <8wt%. This invention controls the biomass-based powder and its particle size and moisture content within the above range, which is beneficial for achieving fluidization and high-pressure conveying of the biomass-based powder. At the same time, due to the small particle size and large specific surface area, the contact area with the gasifying agent is large, which facilitates rapid gasification and results in a high raw material conversion and utilization rate.

[0045] In this invention, the biomass-based powder preferably includes one or more of biomass powder and biochar; the biomass powder is preferably obtained by dehydrating and pulverizing biomass; 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 pyrolysis and pulverizing biomass; the pyrolysis temperature is preferably 300-700°C; in this invention, the biomass preferably includes one or more of agricultural biomass, forestry biomass, and biomass fungal residue, specifically one or more of straw, sawdust, and bamboo; the biomass has renewable and low-carbon characteristics; in a specific embodiment of this 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 this invention, a central mixer and an outer ring mixer are provided at the top of the self-heating fluidized bed reactor; the outer ring mixer is distributed around the central mixer, preferably evenly distributed around the central mixer; both the central mixer and the outer ring mixer are parallel to the axial direction of the self-heating fluidized bed reactor; the organic hazardous waste slurry and the first part of the gasifying agent are preferably introduced into the self-heating fluidized bed reactor through the central mixer; the biomass-based powder is preferably transported by carbon dioxide gas flow and introduced into the self-heating fluidized bed reactor through the outer ring mixer along with the second part of the gasifying agent.

[0047] In this invention, the central mixer is preferably a sleeve-type structure, which forms a feeding channel; the central mixer preferably has three or more feeding channels, specifically three to five; the organic hazardous waste slurry and the first part of the gasifying agent are preferably introduced from different channels of the central mixer. When the central mixer has three feeding channels, the three channels are referred to as the inner channel, middle channel, and outer channel from the inside to the outside. The inner channel and the outer channel preferably carry the gasifying agent, and the middle channel preferably carries the organic hazardous waste slurry; this invention utilizes the central mixer to feed the organic hazardous waste slurry and the gasifying agent. At the outlet of the central mixing gas end, the high-pressure gasifying agent can quickly cut and disperse the organic hazardous waste slurry, achieving full gas-liquid mixing, thereby improving the gasification efficiency.

[0048] In this invention, the number of outer ring mixers is preferably three or more, specifically three to six; each outer ring mixer preferably consists of two nested cylindrical structures of different diameters forming a sleeve structure, with the center of the sleeve 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 carbon dioxide pneumatic conveying, and the second part of the gasifying agent is preferably introduced through the outer channel. This invention, by introducing the biomass-based powder through the inner channel of the outer ring mixer, effectively prevents the sleeve support from affecting the conveying process.

[0049] This invention introduces organic hazardous waste slurry and biomass-based powder into a self-heating fluidized bed reactor through different mixers, enabling the feeding of organic hazardous waste slurry and biomass-based powder in any proportion. If organic hazardous waste slurry and biomass-based powder are mixed and fed together, the amount of biomass-based powder added must be less than 30 wt% to ensure the pumpability of the slurry entering the furnace. If the amount of biomass added is too low, it is difficult to achieve large-scale use of biomass. If the amount of biomass-based powder added is too high, it is easy to cause the slurry to be unable to flow, making it difficult to transport and preventing gasification in the furnace.

[0050] This invention mixes organic hazardous waste slurry and biomass-based powder with a gasifying agent and then introduces them into a self-heating fluidized bed reactor. This achieves uniform dispersion of the organic hazardous waste slurry and biomass-based powder within the furnace, increases the contact area between the materials and the gasifying agent, and improves gasification efficiency. If biomass-based powder and organic hazardous waste slurry are fed into the gasifier through different channels of the same burner, the organic hazardous waste slurry and biomass-based powder tend to mix at the burner end, forming larger agglomerated particles. This significantly reduces the specific surface area, decreases the contact area with the gasifying agent, and prevents complete conversion during the gasification reaction. The carbon conversion rate drops below 95%, and the raw material utilization efficiency is significantly reduced. Furthermore, this invention allows for the separate feeding of organic hazardous waste slurry and biomass-based powder, facilitating the adjustment of the feeding amounts of organic hazardous waste slurry and biomass-based powder. The content of H2 and CO in the syngas can be easily adjusted by regulating the ratio of organic hazardous waste slurry and biomass-based powder. When preparing syngas with a high H2 content, the feeding amount of organic hazardous waste slurry can be increased; when preparing syngas with a high CO content, the feeding amount of biomass-based powder can be increased.

[0051] In this invention, the preferred mass ratio of biomass-based powder to carbon dioxide is 5–20:1, more preferably 10–15:1; the preferred pressure of carbon dioxide is 0.4–1.5 MPa higher than the pressure of the gasification reaction; the preferred mass ratio of the total mass of the gasifying agent to the total mass of the organic hazardous waste slurry and biomass-based powder is 0.4–0.75:1, more preferably 0.5–0.6:1; the preferred pressure of the gasifying agent is 0.4–1.5 MPa higher than the pressure of the gasification reaction and not lower than the pressure of carbon dioxide; specifically, the preferred mass ratio of the first part of the gasifying agent to the organic hazardous waste slurry is 0.5–0.7:1, and the preferred mass ratio of the second part of the gasifying agent to the biomass-based powder is 0.2–0.5:1; the preferred temperature of the gasification reaction is 1200–1500°C, more preferably 1300–1350°C, and the preferred pressure of the gasification reaction is 1–4 MPa, specifically 1–1.15 MPa. In this invention, oxygen, as a gasifying agent, enters the self-heating fluidized bed reactor and reacts with C and H in the raw materials to produce a large amount of heat through combustion, creating a high-temperature environment. Simultaneously, by controlling the oxygen flow rate, this invention ensures that some C and H do not react with the oxygen, instead forming high-temperature C. This high-temperature C then reacts endothermally with the CO2 entering the furnace to generate the target gas CO (C + CO2 → 2CO). Furthermore, conventional gasification reactions in this field use steam as a gasifying agent, utilizing the steam to react with the high-temperature C to generate the target product gas (C + H2O → CO + H2). If steam is used as the gasifying agent, it requires an external supply, and the steam source is generated by combustion, which emits a large amount of CO2. This invention uses oxygen as the gasifying agent and CO2 as the reaction raw material, thus reducing overall carbon emissions.

[0052] In this invention, the gasification yields a mixture of crude syngas and molten inorganic matter. Preferably, the method further includes: subjecting the mixture to rapid water quenching to obtain aqueous ash-containing syngas and glassy slag; preferably, the aqueous ash-containing syngas undergoes gas-liquid separation to obtain ash-containing syngas; preferably, the ash-containing syngas is wetted and then washed to remove ash, yielding the syngas; the rapid water quenching, gas-liquid separation, and washing to remove ash also yield ash-containing water; the ash-containing water is sequentially concentrated by depressurization and cooling followed by negative pressure and cooling, and then filtered to obtain ash slag and recycled water; the content of suspended solids in the recycled water is 30–50 mg. / L; the ash residue is preferably returned for use in the preparation of organic hazardous waste slurry; the recovered water is preferably used partly as flushing water for cooling high-temperature gas and molten slag and flushing glassy slag, and the remaining part is used for inorganic salt recovery. The present invention does not have special requirements for the method of inorganic salt recovery, which can be evaporation recovery; the present invention controls the suspended solids in the recovered water within the above range, which is beneficial to improving the heat exchange efficiency during inorganic salt recovery and avoiding the precipitation of suspended solids during evaporation recovery of inorganic salts; the remaining liquid after inorganic salt recovery is used as circulating ash water, which is preferably returned to the washing and ash removal step for recycling after being heated and pressurized.

[0053] The present invention also provides an apparatus for producing syngas using organic hazardous waste and biomass, including a self-heating fluidized bed reactor 1; a mixer is provided at the top of the self-heating fluidized bed reactor 1, the mixer including a central mixer 2-1 and an outer ring mixer 2-2 distributed around the central mixer 2-1; the self-heating fluidized bed reactor 1 is provided with a gas outlet.

[0054] In this invention, the structure and quantity of the central mixer 2-1 and the outer ring mixer 2-2 are consistent with the above scheme, and will not be repeated here.

[0055] In this invention, the self-heating fluidized bed reactor 1 comprises, from top to bottom, a reaction chamber 1-1 and a cooling chamber 1-2. The lining of the reaction chamber 1-1 is made of a high-temperature and corrosion-resistant material, which has 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 at the top of the cooling chamber 1-2. Preferably, a downcomer 4 and an ascender 3 are provided in the cooling chamber 1-2. The downcomer 4 is separately nested inside the ascender 3, and a gap is left between the outer wall of the downcomer 4 and the inner wall of the ascender 3. The bottoms of the downcomer 4 and the ascender 3 are preferably immersed in the cooling water of the water bath area. In this invention, the raw materials react with the gasifying agent in the reaction chamber 1-1 to generate syngas (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 heat to the endothermic gasification reaction, thereby maintaining the heat balance of the gasification reaction. No external heat source is required, which is energy-saving and efficient. The highly reducing gas with CO and H2 as the main components is generated in the reaction chamber 1-1 can achieve the detoxification of organic hazardous waste. The high-temperature syngas generated by the gasification reaction is mixed with unreacted molten inorganic matter in a parallel flow and enters the cooling chamber 1-2 of the self-heating fluidized bed reactor. In the cooling chamber 1-2, the gas is rapidly cooled and the gas-liquid-solid three-phase separation is carried out. The downcomer 4 installed in the cooling chamber acts as a guide. In the downcomer 4, the ash water from the cooling medium distributor 5 is directly contacted and cooled. The molten inorganic matter, which is insoluble in water, automatically sinks into the lower cooling water in the form of glassy slag after rapid cooling. The cooled gas and the vapor 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, namely the water-containing ash syngas.

[0056] In this invention, the bottom of the self-heating fluidized bed reactor 1 is preferably connected to the slag collection device 11, and a locking slag valve 10 is preferably also provided between the bottom of the self-heating fluidized bed 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 self-heating fluidized bed reactor 1; a locking slag valve 12 is preferably provided at the bottom of the slag collection device 11; the slag collection device 11 can specifically be a slag collection tank. In this invention, the glassy slag cooled in the water bath area and the cooling water that has not been converted into steam remain in the lower water bath of the cooling chamber 1-2. 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 simultaneously connected to flushing water, and the liquid-solid mixture in the slag collection device 11 is periodically discharged through the locking slag valve 12 under the action of the flushing water.

[0057] In this invention, the device preferably further 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 self-heating fluidized bed reactor 1; the top of the gas-liquid separator 6 is preferably provided with a first demister 31, and the water-containing ash synthesis gas enters the gas-liquid separator 6 for gas-liquid separation to obtain ash-containing synthesis gas.

[0058] In this invention, the device preferably further includes an ash wetting device 7, the inlet of which is connected to the gas outlet of the gas-liquid separator 6; the ash-containing syngas enters the ash wetting device 7 for wetting, and the fine ash particles entrained in the syngas are forced to wet and enlarge through wetting, which is beneficial for the removal of entrained ash in the subsequent scrubber 8.

[0059] In this invention, the device preferably further includes a washer 8, the inlet of which is connected to the outlet of the ash impregnator 7; the lower part of the washer 8 is preferably a water bath area, the water in the water bath area is preferably high-temperature and high-pressure circulating ash water, the temperature of which is preferably 120-200℃, and the pressure is preferably 0.2-0.5 MPa higher than the washer pressure; the washer 8 preferably has a gas guide downpipe 29 and a gas guide uppipe 30, 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 bottom of the gas guide downpipe 29 and the gas guide uppipe 30 is preferably immersed in the water bath at the bottom of the washer 8; Preferably, the scrubber 8 is further provided with a multi-layer tray 27 and a second demister 28. The multi-layer tray 27 is preferably located above the gas guide downpipe 29 and the gas guide uppipe 30. Washing water is preferably introduced into the upper part of the multi-layer tray 27. The washing water is preferably from the condensate of the downstream section or external water supply. The second demister 28 is preferably located at the top of the scrubber 8. The bottom of the scrubber 8 is preferably conical. The bottom of the cone is preferably provided with a first ash water outlet for discharging ash water with high ash content. A second ash water outlet is preferably provided above the area where the lower part of the scrubber 8 connects to the cone for discharging ash water with low ash content. The second ash water outlet is preferably connected to a first pressurizing pump 9. The outlet of the first pressurizing pump 9 is preferably connected to the inlet of the cooling medium distributor 5 and the ash impregnator 7, respectively. In this invention, the ash-containing gas after impregnation enters the lower water bath of the scrubber 8 along the gas guide downpipe 29. Then, the gas 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 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 this invention, the device preferably further includes an ash-containing water treatment system; the ash-containing water treatment system includes: a pressure-reducing and cooling device 13, which is provided with a liquid outlet and a steam outlet; the inlet of the pressure-reducing and cooling device 13 receives external water supply and the lower drainage from the cooling chamber 1-2, the gas-liquid separator 6, and the scrubber 8; the pressure-reducing and cooling device 13 operates under positive pressure, preferably with an operating pressure of 0.1–0.5 MPa; and a negative pressure cooling device 14, the inlet of which is connected to the liquid outlet of the pressure-reducing and cooling device 13. The negative pressure cooling device 14 is provided with a liquid outlet and a steam outlet; the operating pressure of the negative pressure cooling device 14 is preferably -0.09 to -0.06 MPa; a negative pressure steam condenser 15, the inlet of which is connected to the steam outlet of the negative pressure cooling device 14; a negative pressure steam-water separator 16, the inlet of which 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 is connected to the gas outlet of the negative pressure steam-water separator 16; an 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 open to the atmosphere; a settling buffer device 19, the inlet of the settling buffer device 19 is connected to the liquid outlet of the negative pressure cooler 14, and a liquid level control valve 32 is preferably installed on the pipeline connecting the inlet of the settling buffer device 19 and the liquid outlet of the negative pressure cooler 14; the settling buffer device 19 Specifically, it can be a settling buffer tank; a filter device 21, the inlet of which is connected to the outlet of the settling buffer device 19, and preferably a slag pump 20 is installed on the pipeline connecting the inlet of the filter device 21 and the outlet of the settling buffer device 19; a circulating ash water device 22, the inlet of which is 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 ash water device 22 is specifically a circulating ash water tank.

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

[0062] In this invention, the ash-containing water generated by the water bath in 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 in scrubber 8 are all discharged to the ash-containing water treatment system. In a specific embodiment of this invention, the ash-containing water generated by the water bath in 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 in scrubber 8 can be directly discharged into the pressure reducing and cooling device 13, or it can be discharged into the pressure reducing and cooling device 13 after being depressurized by a pressure reducing valve. The ash-containing water with low ash content at the top of the water bath in scrubber 8 is partially sent to the cooling medium distributor 5 after being pressurized by the first pressurizing pump 9. Under the action of the cooling medium distributor 5, it is evenly distributed on the inner wall of the downcomer 4 to rapidly cool the gas and slag exiting the reaction chamber 1-1. The remaining part is sent to the ash impregnator 7 as impregnation water.

[0063] In this invention, the ash-containing water treatment system is used to recover heat from the ash-containing water, achieve water-ash separation, and simultaneously recover and reuse dissolved inorganic salts in the water. Specifically, the ash-containing water discharged from cooling chambers 1-2, the ash-containing water discharged from gas-liquid separator 6, and the ash-containing water (high ash content) discharged from scrubber 8 enters the pressure-reducing and cooling unit 13. The steam generated in the pressure-reducing and cooling unit 13 is washed and deashed by condensate from downstream processes or external water supply and then discharged from the top into the heat recovery unit 25. The non-condensable gases in the steam are discharged from the top of the heat recovery unit 25 for combustion and heat recovery. The concentrated ash water generated at the bottom of the pressure-reducing and cooling unit 13 enters the negative pressure cooling unit 14 for further cooling and... The ash water is concentrated twice, and the slag water discharged from the bottom of the slag collection device 11 along with the external slag discharge is also fed 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, causing it to condense into liquid water; the negative pressure steam-water separator 16 separates the steam-water mixture generated in the negative pressure steam condenser 15; the atmospheric pressure steam-water separator 18 separates the steam-water mixture after passing through the negative pressure generator 17 again. The secondary concentrated ash water generated by the negative pressure cooling device 14 flows by gravity into the settling buffer device 19 via the level control valve 32. After being pressurized by the slag water pump 20, it is sent to the filter device 21 for the separation of ash and water. The separated ash is returned to prepare organic hazardous waste slurry. The separated water enters the circulating ash water device 22, mixes with the water discharged from the bottom of the negative pressure steam-water separator 16 and the water discharged from the atmospheric pressure steam-water separator 18, and is then pressurized by the ash water pump 23. Part of the pressurized ash water is returned to the slag collection device 11 for use as rinsing water, and part is sent to the inorganic salt recovery device 24 to recover the soluble inorganic salts. The remaining ash water after the inorganic salt recovery is sent to the heat recovery device 25 as circulating ash water. After being heated by the heat recovery device 25, the circulating ash water is pressurized by the second pressurizing 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 technical solutions of this invention will be clearly and completely described below with reference to the embodiments thereof. Obviously, the described embodiments are only a part of the embodiments of this invention, and not all of them. Based on the embodiments of this invention, all other embodiments obtained by those skilled in the art without creative effort are within the scope of protection of this invention.

[0065] Example 1

[0066] use Figure 1 and Figure 2 The device in the process gasifies organic hazardous waste and biomass to produce syngas. The specific steps are as follows:

[0067] The preparation method of the organic hazardous waste slurry is as follows: Distillation residue and antibiotic fermentation residue are mixed at a mass ratio of 4:6, then the pH value is adjusted to 7, and finally mixed with water to form the organic hazardous waste slurry. The main components of the organic hazardous waste slurry are water, organic matter containing carbon, hydrogen, oxygen, nitrogen, and sulfur, and a mixture of some inorganic metal salts. The lower heating value of the organic hazardous waste slurry is 11000 KJ / kg, the water content is 46 wt%, and the slurry density is 1120 kg / m³. 3 .

[0068] The preparation method of biomass-based powder is as follows: bamboo charcoal powder (obtained by grinding bamboo after pyrolysis) and bamboo powder (obtained by grinding bamboo after roasting) are mixed to obtain biomass-based powder, wherein the mass fraction of bamboo charcoal powder is 85% and the mass fraction of bamboo powder is 15%; the particle size of the biomass-based powder is <0.8mm, the moisture content is <8wt%, the lower heating value is 22000KJ / kg, and the bulk density is 520kg / m³. 3 .

[0069] Organic hazardous waste slurry and oxygen are fed into the central mixer 2-1 at the top of the self-heating fluidized bed reactor 1. The central mixer 2-1 has a three-channel sleeve structure. Oxygen is introduced into the inner and outer channels of the central mixer 2-1, while the organic hazardous waste slurry is introduced into the middle channel. Biomass-based powder is fed into the outer ring mixer 2-2 at the top of the self-heating fluidized bed reactor 1 under high-pressure CO2 transport. Three outer ring mixers are set up and evenly distributed around the central mixer 2-1. The outer ring mixer 2-2 has a two-channel structure, with the inner channel for biomass powder transported by CO2 gas flow and the outer channel for oxygen. Both the central mixer 2-1 and the outer ring mixer 2-2 are axially parallel to the reaction chamber 1-1 of the self-heating fluidized bed reactor 1. The inlet flow rate of the organic hazardous waste slurry is 150 kg / h, and the inlet pressure is 1.2 MPa; the inlet flow rate of the biomass-based powder is 100 kg / h, and the CO2 transport flow rate is 5 Nm³. 3 / h, pressure is 1.5MPa; oxygen pressure is 1.5MPa, total flow rate is 90Nm 3 / h, 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 part oxygen to the second part oxygen is 2:1. The vaporization pressure is 1.0MPa and the vaporization temperature is 1300℃.

[0070] In the reaction chamber 1-1 of the self-heating fluidized bed reactor 1, organic hazardous waste and biomass undergo a gasification reaction. The generated high-temperature syngas mixes with unreacted molten inorganic matter and enters the cooling chamber 1-2 of the self-heating fluidized bed reactor 1 in parallel flow. In the downcomer 4 of the cooling chamber 1-2, the molten inorganic matter comes into direct contact with ash water from the cooling medium distributor 5 for cooling. After rapid cooling, the water-insoluble molten inorganic matter automatically settles into the lower water bath as glassy slag. The cooled gas and the vapor generated by the heated ash water flow upwards along the annular gap between the outer wall of the downcomer 4 and the inner wall of the riser 3. The gas rises out of cooling chamber 1-2 to obtain syngas containing water and ash. This syngas then enters gas-liquid separator 5 for gas-liquid separation. The resulting ash-containing gas enters ash wetting tank 6. After wetting and humidifying, the ash-containing gas enters scrubber 8 and flows along gas downcomer 29 into the lower water bath of scrubber 8. The gas then rises along the annular gap between the outer wall of gas downcomer 29 and the inner wall of gas upcomer 30, passing sequentially through multi-layer tray 27 and the second demister 28, before exiting from the top of scrubber 8 to obtain syngas. The total syngas flow rate is 251.5 Nm³. 3 / h.

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

[0072] The ash-containing water generated by the water bath in cooling chamber 1-2, the ash-containing water at the bottom of gas-liquid separator 6, and the ash-containing water with high ash content at the bottom of the water bath in scrubber 8 are all discharged to the ash-containing water treatment system. The ash-containing water with low ash content at the top of the water bath in scrubber 8 is pressurized by the first pressurizing pump 9 and then sent to the cooling medium distributor 5. Under the action of the cooling medium distributor 5, it is evenly distributed on the inner wall of the downcomer 4 to rapidly cool the gas and slag exiting the reaction chamber 1-1. The remaining part is sent to the ash impregnator as impregnation water.

[0073] Ash-containing water discharged from cooling chambers 1-2, gas-liquid separator 6, and scrubber 8 (ash-containing water with high ash content) are depressurized and then enter pressure-reducing cooling unit 13. The steam generated in pressure-reducing cooling unit 13 is washed and deashed, and then discharged from the top into heat recovery unit 25. Non-condensable gases in the steam are discharged from the top of heat recovery unit 25 for combustion and heat recovery. The concentrated ash water generated at the bottom of pressure-reducing cooling unit 13 enters negative pressure cooling unit 14 for further cooling and secondary concentration. At the same time, the slag water discharged from the bottom of slag collection device 11 along with the discharged slag is also introduced into negative pressure cooling unit 14. Negative pressure steam condenser 15 cools the high-temperature steam from negative pressure cooling unit 14, causing it to condense into liquid water. Negative pressure steam-water separator 16 separates the steam-water mixture generated in negative pressure steam condenser 15. Atmospheric pressure steam-water separator 18 further separates the steam-water mixture after passing through negative pressure generator 17. The secondary concentrated ash water generated by the negative pressure cooling device 14 flows by gravity into the settling buffer device 19 via the level control valve 32. After being pressurized by the slag water pump 20, it is sent to the filter device 21 for the separation of ash slag and water. The separated ash slag is returned to prepare organic hazardous waste slurry. The separated recycled water (with a solid suspended solids content of 30-50 mg / L) enters the circulating ash water device 22, mixes with the water discharged from the bottom of the negative pressure steam-water separator 16 and the water discharged from the atmospheric pressure steam-water separator 18, and is then pressurized by the ash water pump 23. Part of the pressurized ash water is returned to the slag collection device 11 for use as rinsing water, and part is sent to the inorganic salt recovery device 24 to recover the soluble inorganic salts. The remaining ash water after the inorganic salt recovery is sent to the heat recovery device 25 as circulating ash water. After being heated by the heat recovery device 25, the circulating ash water is pressurized by the second pressurizing 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 embodiment are shown in Table 1:

[0075] Table 1. Main components of the syngas 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 amounts / total / 251.5

[0077] According to material balance calculations, the C conversion rate in the furnace feed material is 98.23%.

[0078] Example 2

[0079] All other conditions are the same as in Example 2, except that: the flow rate of organic hazardous waste into the furnace is 100 kg / h, the inlet pressure is 1.35 MPa, the flow rate of biomass-based powder into the furnace is 150 kg / h, and the CO2 conveying flow rate is 7 Nm³. 3 / h, pressure is 1.6MPa; oxygen pressure is 1.7MPa, total flow rate is 85Nm 3 / h, 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 part oxygen to the second part oxygen is 0.9:1; the vaporization pressure is 1.15MPa, and the vaporization temperature is 1350℃.

[0080] The total syngas flow rate obtained in this embodiment is 258.6 Nm³. 3 / h, the main components are shown in Table 2:

[0081] Table 2. Main components of the syngas obtained in Example 2

[0082]

[0083]

[0084] According to material balance calculations, the C conversion rate in the furnace feed material is 98.56%.

[0085] Comparative Example 1

[0086] The types of raw materials, reaction temperature, pressure, and raw material feeding conditions used are the same as 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. The outermost ring is an 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 syngas flow rate obtained in this embodiment is 232.15 Nm³. 3 / h, the main components are shown in Table 3:

[0088] Table 3 shows the main components of the syngas 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 amounts / total / 232.15

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

[0091] As can be seen from the above embodiments and comparative examples, the present invention feeds biomass-based powder and organic hazardous waste slurry separately, which can achieve independent atomization of slurry and powder, while also having a reaction coupling effect, effectively increasing the content of CO and H2 in syngas and significantly improving gasification efficiency.

[0092] The above description is only a preferred embodiment of the present invention. It should be noted that for those skilled in the art, several improvements and modifications can be made without departing from the principle of the present invention, and these improvements and modifications should also be considered within the scope of protection of the present invention.

Claims

1. A method for preparing syngas using organic hazardous waste and biomass, characterized in that, Includes the following steps: Organic hazardous waste slurry, biomass-based powder, and gasifying agent are fed into a self-heating fluidized bed reactor for gasification to obtain syngas; the gasifying agent is oxygen. The gasifying agent is divided into a first gasifying agent and a second gasifying agent; the first gasifying agent is mixed with organic hazardous waste slurry to form a first mixed stream which enters the self-heating fluidized bed reactor; the biomass-based powder transported by carbon dioxide gas flow and the second gasifying agent form a second mixed stream which enters the self-heating fluidized bed reactor; the second mixed stream is distributed around the first mixed stream. The self-heating fluidized bed reactor is equipped with a central mixer and an outer ring mixer at the top; the outer ring mixer is distributed around the central mixer; the organic hazardous waste slurry and the first part of the gasification agent are introduced into the self-heating fluidized bed reactor through the central mixer; The biomass-based powder is transported by a carbon dioxide gas stream and, together with the second part of the gasifying agent, is introduced into the self-heating fluidized bed reactor from the outer ring mixer. The organic hazardous waste slurry has a lower heating value ≥10000KJ / kg and a density <1250kg / m³. 3 Moisture content <50wt%; The biomass-based powder has a lower heating value ≥18000KJ / Kg and a bulk density of 200~600kg / m³. 3 The average particle size is <0.8mm and the moisture content is <8wt%.

2. The method according to claim 1, characterized in that, The central mixer has a sleeve-type structure, which forms a feeding channel; the central mixer has three or more feeding channels; the organic hazardous waste slurry and the first part of the gasification agent are respectively introduced from different feeding channels of the central mixer; The number of outer ring mixers is three or more; each outer ring mixer consists of two nested cylindrical structures of different diameters forming a sleeve structure, with the center of the sleeve structure being the inner channel and the gap between the two cylindrical structures being the outer channel; the biomass-based powder is introduced through the inner channel under the transport of carbon dioxide gas flow, and the second part of the gasifying agent is introduced through the outer channel.

3. The method according to claim 1, characterized in that, The biomass-based powder includes one or more of biomass powder and biochar.

4. The method according to claim 1, characterized in that, The mass ratio of the biomass-based powder to carbon dioxide is 5~20:1; the ratio of the total mass of the gasifying agent to the total mass of the organic hazardous waste slurry and biomass-based powder is 0.4~0.75:

1. The temperature of the gasification reaction is 1200~1500℃ and the pressure is 1~4MPa.

5. The method according to claim 1, characterized in that, The gasification yields a mixture of crude syngas and molten inorganic matter. The method further includes: subjecting the mixture to rapid water quenching to obtain hydrated ash syngas and glassy slag. The water-containing ash syngas is subjected to gas-liquid separation to obtain ash-containing syngas; the ash-containing syngas is then wetted and washed to remove ash, thus obtaining the syngas. The quenching, gas-liquid separation, and washing and ash removal processes also yield ash-containing water. The ash-containing water is then subjected to depressurization and cooling for concentration and negative pressure cooling for concentration, followed by filtration to obtain ash residue and recycled water. The content of suspended solids in the recycled water is 30-50 mg / L.

6. The method according to claim 1, characterized in that, The apparatus used in the method for preparing syngas from organic hazardous waste and biomass includes a self-heating fluidized bed reactor (1); a mixer is provided on the top of the self-heating fluidized bed reactor (1), the mixer includes a central mixer (2-1) and an outer ring mixer (2-2) distributed around the central mixer (2-1); the self-heating fluidized bed reactor (1) is provided with a gas outlet.

7. The method according to claim 6, characterized in that, The self-heating fluidized bed reactor (1) includes a reaction chamber (1-1) and a cooling chamber (1-2) from top to bottom; 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).

8. The method according to claim 6 or 7, characterized in that, The device further 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 self-heating fluidized bed reactor (1); Ash impregnator (7), the inlet of which is connected to the gas outlet of the gas-liquid separator (6); The inlet of the washer (8) is connected to the outlet of the ash impregnator (7).

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

Images