CN112080323A - Solid-liquid carbon-containing waste comprehensive treatment and resource utilization system - Google Patents
Solid-liquid carbon-containing waste comprehensive treatment and resource utilization system Download PDFInfo
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/58—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels combined with pre-distillation of the fuel
- C10J3/60—Processes
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/72—Other features
- C10J3/82—Gas withdrawal means
- C10J3/84—Gas withdrawal means with means for removing dust or tar from the gas
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/72—Other features
- C10J3/86—Other features combined with waste-heat boilers
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0913—Carbonaceous raw material
- C10J2300/0946—Waste, e.g. MSW, tires, glass, tar sand, peat, paper, lignite, oil shale
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/16—Integration of gasification processes with another plant or parts within the plant
- C10J2300/1603—Integration of gasification processes with another plant or parts within the plant with gas treatment
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/16—Integration of gasification processes with another plant or parts within the plant
- C10J2300/1671—Integration of gasification processes with another plant or parts within the plant with the production of electricity
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/16—Integration of gasification processes with another plant or parts within the plant
- C10J2300/1687—Integration of gasification processes with another plant or parts within the plant with steam generation
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Abstract
The invention relates to the field of environmental protection, and aims to provide a comprehensive treatment and resource utilization system for solid-liquid carbon-containing waste. The system comprises an self-heating pyrolysis furnace, a gasification furnace, a semi-coke transition bin, a slag cooling device, a crude gas treatment system, a synthesis gas pretreatment system and a mixed gas treatment system. The comprehensive treatment and resource utilization system for the carbon-containing solid-liquid wastes integrates the solid wastes, dangerous wastes, waste liquid and other carbon-containing wastes into a whole, and the solid wastes, the dangerous wastes, the waste liquid and other carbon-containing wastes are pyrolyzed and gasified, so that integrated treatment is realized, and reduction, resource and harmless treatment is realized. Can realize the active removal of materials, intermediate products and products, balance the balance: the problem of the semicoke that pyrolysis furnace pyrolysis produced not directly utilize the occasion is solved, provide hot raw materials for the gasifier simultaneously. The self-heating type pyrolyzing furnace does not need to provide an independent heat source from the outside, and can obtain heat required by pyrolysis only by consuming part of carbon-containing wastes, thereby reducing energy consumption and saving investment of independent heat supply equipment.
Description
Technical Field
The invention belongs to the field of environmental protection, and particularly relates to a comprehensive treatment and resource utilization system for solid-liquid carbon-containing waste.
Background
The carbon-containing waste refers to various solid wastes, dangerous wastes, waste water and liquid wastes and the like containing carbon elements, and has a certain heat value and utilization value due to the carbon elements. At present, solid carbon-containing wastes, such as garbage, crop residues, sludge of sewage treatment plants, oily sludge of petrochemical enterprises and the like, are treated by adopting a traditional landfill method, a traditional incineration method or a traditional method which is simply treated and then transported and stacked, so that a large amount of land resources are occupied, and soil, water and atmosphere are polluted to different degrees. The treatment mode of carbon-containing liquid wastes, such as various waste water and waste liquid generated and discharged in industry and production life, mainly utilizes a waste water treatment device to treat tail liquid, realizes standard discharge, consumes a large amount of energy while realizing clean discharge, and is a waste of water resources.
Pyrolysis has the advantages of diversified resource utilization of products, reduction of dioxin emission and the like, and thus the pyrolysis is increasingly the first choice of solid waste treatment technology. However, most of the semicoke generated by pyrolysis is not suitable for being used as a raw material, and the utilization efficiency can only be improved by a combustion mode, but the semicoke is directly used for combustion and has the problems of high ash content, high hardness, low carbon conversion rate and the like, so that the utilization of the semicoke becomes a key problem of the pyrolysis technology. Gasification technology can produce high performance fuel gas coupled power generation and is therefore considered to be the major application technology in the future. However, if the carbonaceous waste is directly gasified, the carbonization products of tar, phenol and other substances cannot be completely gasified, which not only affects the gasification efficiency, but also causes equipment failure and secondary pollution. In conclusion, how to effectively and cleanly treat the solid-liquid carbon-containing waste with low cost and efficiently recycle the solid-liquid carbon-containing waste is a problem and a challenge which needs to be solved urgently in the economic and social development of China.
Disclosure of Invention
The invention overcomes the defects of the prior art and provides a comprehensive treatment and resource utilization system for carbon-containing solid-liquid waste, the carbon-containing waste is subjected to double-stage circulation treatment, the treatment energy consumption and cost are reduced, the cleaning utilization rate of the carbon-containing waste can be effectively improved, and the high-efficiency cleaning and energy quality grading utilization system for the carbon-containing waste is realized.
In order to solve the technical problem, the solution of the invention is as follows:
the system comprises an autothermal pyrolysis furnace, a gasification furnace, a semicoke transition bin, a slag cooling device, a crude gas treatment system, a synthesis gas pretreatment system and a mixed gas treatment system;
a feed inlet, an oxidant inlet and a fluidized air inlet are arranged on the side wall of the furnace body of the self-heating pyrolysis furnace; the furnace bottom is provided with a slag outlet, the outlet of the furnace top is sequentially connected with a primary cyclone separator and a secondary cyclone separator, and the outlet at the bottom of the primary cyclone separator is connected with the furnace body; the top outlet of the secondary cyclone separator is connected with a crude gas treatment system, and the bottom outlet of the secondary cyclone separator is connected with a semicoke transition bin; the crude gas treatment system comprises a quench tower, a first-stage electric tar precipitator, an intercooler and a second-stage electric tar precipitator which are sequentially connected, wherein the outlet of the second-stage electric tar precipitator is sequentially connected with a gas exhaust fan and a gas buffer tank, and the second-stage electric tar precipitator is also connected with a tar storage tank;
the top of the gasification furnace is provided with a feed inlet, an oxidant inlet and a gasifying agent inlet, the feed inlet is connected with the bottom outlet of the semicoke transition bin, and a slag outlet at the bottom of the gasification furnace is connected to a slag cooling device; the synthesis gas pretreatment system comprises a waste heat boiler and a mixing tank, wherein a gas outlet is formed in the side wall of the gasification furnace and connected to the waste heat boiler; a synthetic gas outlet of the waste heat boiler and the gas buffer tank are connected to a mixing tank, and the mixing tank is connected with a mixed gas treatment system;
the mixed gas treatment system comprises a fluidized gas pressurizing device, and a carbon monoxide conversion device, a decarburization device, a gas exhaust fan, a pressure swing adsorption device and a gas holder which are connected in sequence; wherein, the carbon monoxide conversion device is provided with a water inlet, an air inlet and a steam outlet, the water inlet is connected with a circulating cooling water outlet of the slag cooling device, the air inlet is connected with the mixing tank, and the steam outlet is connected to a gasifying agent inlet of the gasification furnace; the decarbonization device is provided with CO2An outlet and a pressure swing adsorption device are arranged in the H2The mixed gas outlet is simultaneously connected with the gas holder and the fluidized gas pressurizing device; the outlet of the fluidized gas pressurizing device is connected to the fluidized air inlet of the self-heating pyrolysis furnace;
and the systems or the equipment are connected through pipelines.
In the invention, the slag cooling device is a closed container and comprises a cold water tank and a heat exchanger arranged in the cold water tank.
In the invention, the semicoke transition bin is a closed cylindrical container, and the outlet at the bottom of the semicoke transition bin is connected to the feed inlet at the top of the gasification furnace through a lower end connecting pipe; a pressure valve is arranged on the lower end connecting pipe.
The invention further provides a method for realizing comprehensive treatment and resource utilization of solid-liquid carbon-containing waste by using the system, which comprises the following steps:
(1) feeding the carbon-containing waste subjected to grinding or shredding pretreatment into an autothermal pyrolysis furnace through a feed inlet, feeding oxygen from an oxidant inlet, and feeding fluidized air from a fluidized air inlet; the self-heating type pyrolyzing furnace is a normal-pressure low-temperature pyrolyzing furnace, and the temperature is controlled to be 500-600 ℃; in the furnace, part of the carbon-containing waste is combusted under the condition of oxygen to release heat, so that a heat source is provided for the pyrolysis process; pyrolyzing the rest carbon-containing wastes under an oxygen-free condition; the pyrolysis product passes through a primary cyclone separator and a secondary cyclone separator to obtain pyrolysis gas and semicoke; the pyrolysis gas is sent to a crude gas treatment system for purification treatment;
(2) the pyrolysis gas sent to the crude gas treatment system firstly enters a quench tower, is sprayed with water for cooling, carries with water vapor to sequentially pass through a primary electric tar precipitator, an intercooler and a secondary electric tar precipitator, and respectively separates tar and water in the crude gas; the tar is sent to a tar storage tank for storage, liquid water is used as cooling water of the quench tower for recycling, and the obtained pure coal gas is sent to a coal gas buffer tank for storage through a coal gas exhaust fan;
(3) the powder collected at the bottom of the primary cyclone separator is sent back to the self-heating pyrolysis furnace for continuous reaction, and the semicoke powder collected at the bottom of the secondary cyclone separator is temporarily stored in a semicoke transition bin and then fed from a feed inlet at the top of the gasification furnace; under the carrying of oxygen fed from an oxidant inlet at the top of the furnace and saturated steam fed from an oxidant inlet of the gasification agent, carrying out cracking gasification on semi-coke powder in the furnace, feeding the generated synthesis gas into a synthesis gas pretreatment system through a gas outlet of the furnace body, and discharging liquid ash slag into a slag cooling device through a slag outlet at the bottom of the furnace; the gasification furnace is a high-temperature pressurized gasification furnace, the temperature in the gasification furnace is controlled to be 1500-1600 ℃, and the pressure is 0.2-2 MPa;
(4) the synthesis gas sent to the synthesis gas pretreatment system firstly enters a waste heat boiler, and the released heat heats cooling water in the waste heat boiler into saturated steam which is output for heating or power generation; the cooled synthetic gas and clean coal gas from the coal gas buffer tank enter a mixing tank together to be mixed into uniform-heating and homogeneous mixed gas, and then the mixed gas is sent to a mixed gas treatment system;
(5) the mixed gas from the mixing tank firstly enters a carbon monoxide conversion device, the carbon monoxide in the mixed gas reacts with the circulating cooling effluent water from the slag cooling device to generate hydrogen and carbon dioxide, and the redundant water is heated into saturated steam by heat released by the carbon monoxide conversion reaction and is sent to a gasification furnace as a gasification agent; the mixed gas after carbon monoxide conversion enters a decarbonization device, and carbon dioxide gas in the mixed gas is separated and sent out; the residual mixed gas enters a pressure swing adsorption device through a gas exhaust fan to extract hydrogen; sending the residual mixed gas after extracting hydrogen into a gas holder; part of the extracted gas is sent into the pyrolysis furnace through a fluidizing gas pressurizing device and is used as fluidizing air of the pyrolysis furnace to ensure fluidization of bed materials.
In the invention, in the step (1), the carbon-containing waste is one or more of coal, biomass, petroleum coke, blue carbon, garbage, crop residue, industrial wastewater and waste liquid, sludge, oil sand or waste activated carbon.
In the invention, the operating temperature of the carbon monoxide conversion device is 180-280 ℃; the water in the carbon monoxide conversion device is supplied by a circulating cooling water outlet of the slag cooling device.
According to the invention, an annular channel is arranged on the outer wall of the gasification furnace along the periphery of the furnace, 4-8 gasification agent feed inlets which are communicated with the gasification furnace are uniformly distributed on the annular channel, and the gasification agent enters the gasification furnace to participate in gasification in a pressure-equalizing and homogeneous manner.
Description of the inventive principles:
the comprehensive treatment and resource utilization system for solid-liquid carbon-containing wastes mainly comprises an autothermal pyrolysis furnace, a gasification furnace, a crude gas treatment system, a synthesis gas pretreatment system and a mixed gas treatment system;
solid-liquid carbon-containing waste is ground and cut into pieces, then is sent into the self-heating pyrolysis furnace through the feed inlet, and enters the pyrolysis furnace together with oxygen sent from the oxidant inlet and fluidized air sent from the fluidized air inlet, and a small amount of carbon-containing waste is combusted under the condition of a small amount of oxygen to release heat so as to provide a heat source for the pyrolysis process; and performing low-temperature pyrolysis on the rest large amount of carbon-containing wastes under an anaerobic condition, allowing pyrolysis products to pass through a primary cyclone separator and a secondary cyclone separator to obtain pyrolysis gas and semicoke, purifying and extracting tar from the pyrolysis gas by a gas treatment system to obtain pure coal gas, conveying the pure coal gas into a coal gas buffer tank by a coal gas discharge fan for storage, and allowing the semicoke to enter a semicoke transition bin for temporary storage.
The pyrolysis gas after passing through the two-stage cyclone separator firstly enters a quench tower, is sprayed with water for cooling, carries with water vapor, sequentially passes through a first-stage electric tar precipitator, an intercooler and a second-stage electric tar precipitator, separates tar and water in the crude gas respectively, sends the tar into a storage tank for storage, and uses liquid water as a cooling water source of the quench tower to finally obtain pure coal gas.
Sending the semicoke powder in the semicoke transition bin into the top of a gasification furnace, carrying the semicoke powder by oxygen sent from an oxidant inlet and saturated steam sent from a gasification agent inlet, and then sending the semicoke powder into the gasification furnace for pyrolysis gasification, and gasifying and decomposing the pyrolysis semicoke to generate synthesis gas in the high-temperature gasification process; the generated synthetic gas is sent into a waste heat boiler through a gas outlet, and the residual high-temperature liquid ash is discharged through a slag outlet arranged at the bottom of the boiler and sent into a slag cooling device.
The high-temperature synthesis gas from the gas outlet of the gasification furnace enters a waste heat boiler to release a large amount of heat, and the cooling water introduced into the waste heat boiler pipe is heated to become saturated steam for output, so that the saturated steam can be used for heating or power generation; the cooled synthetic gas and the clean gas from the gas buffer tank are mixed in the mixing tank to form uniform-heating and homogeneous mixed gas.
The mixed gas from the mixing tank enters a carbon monoxide conversion device, and carbon monoxide in the mixed gas reacts with water to generate hydrogen and carbon dioxide; the water in the carbon monoxide conversion device is provided with a source by cooling water at the outlet of the slag cooling device. And the mixed gas after carbon monoxide conversion enters a decarburization device, and carbon dioxide gas in the mixed gas is separated out and stored or used for producing dry ice. And the residual mixed gas enters a pressure swing adsorption device through a gas exhaust fan, hydrogen is extracted, and the hydrogen is sent to a tar hydrogenation device to produce a light fuel oil product. The residual mixed gas after hydrogen extraction is sent into a gas cabinet for storage and outward transportation; wherein, part of the gas is extracted to be used as fluidized air of the pyrolysis furnace and is sent into the pyrolysis furnace through a fluidized gas pressurizing device, thereby ensuring the fluidization of bed materials.
Compared with the mode of separate processing and low-order utilization in the prior art, the invention has the beneficial effects that:
1. the comprehensive treatment and resource utilization system for the carbon-containing solid-liquid wastes integrates the solid wastes, dangerous wastes, waste liquid and other carbon-containing wastes into a whole, and the solid wastes, the dangerous wastes, the waste liquid and other carbon-containing wastes are pyrolyzed and gasified, so that integrated treatment is realized, and reduction, resource and harmless treatment is realized. The system can perform double-stage circulation comprehensive treatment on the carbon-containing wastes such as solid wastes, sludge, waste water and waste liquid in various industries, reduce the energy consumption and cost of separate treatment, effectively improve the cleaning utilization rate of the carbon-containing wastes, and realize high-efficiency cleaning and energy quality grading utilization of the carbon-containing wastes. The intermediate product and the final product can be recycled, so that the treatment energy consumption is saved, and the development trend of comprehensive utilization of the carbon-containing waste is met.
2. The invention can realize the active removal of materials, intermediate products and products, and balance the balance between the collection and the payment: semicoke generated by pyrolysis of the self-heating pyrolysis furnace is directly used as a raw material of the gasification furnace, and fluidized air required by the pyrolysis furnace is directly derived from residual gas after hydrogen is extracted by pressure swing adsorption; the water required by the carbon monoxide conversion device is derived from cooling water at the outlet of the slag cooling device, and saturated steam from the carbon monoxide conversion device is used for providing a gasification agent required by the gasification furnace; saturated steam output by the waste heat boiler can be used for heating or power generation; the hydrogen extracted by the pressure swing adsorption device can be used for tar hydrogenation, thereby realizing material balance, comprehensive treatment and resource utilization of the whole system.
3. The invention combines the pyrolysis furnace and the gasification furnace, utilizes the semicoke generated by pyrolysis of the pyrolysis furnace as the raw material of the gasification furnace directly, solves the problem that the semicoke generated by pyrolysis of the pyrolysis furnace is not directly utilized, provides hot raw material for the gasification furnace at the same time, saves the cost of cooling and storing the semicoke, increases the initial temperature of the semicoke gasification furnace, improves the thermal efficiency of the gasification furnace on one hand, and simultaneously operates the pyrolysis furnace and the gasification furnace on the other hand, two devices can share the oxygen generation system and the gas treatment system, thereby reducing the equipment investment.
4. Different from the conventional pyrolysis furnace, the self-heating pyrolysis furnace provided by the invention has the advantages that the carbon-containing waste enters the pyrolysis furnace together with the oxidant and the fluidized air through the feeding hole, and a small amount of carbon-containing waste is combusted under the condition of a small amount of oxygen to release heat so as to provide a heat source for the pyrolysis process; and the rest of the carbon-containing wastes are pyrolyzed at low temperature under the oxygen-free condition. The self-heating type pyrolyzing furnace does not need to provide an independent heat source from the outside, and can obtain heat required by pyrolysis only by consuming part of carbon-containing wastes, thereby reducing energy consumption and saving investment of independent heat supply equipment.
Drawings
Fig. 1 is a flowchart of the present embodiment.
The reference numbers in the figures are: 1, an autothermal pyrolysis furnace; 2, gasifying a furnace; 3 a semicoke transition bin; 4, a slag cooling device; 5 a crude gas treatment system; 6 synthesis gas pretreatment system, 7 mixed gas treatment system, 101 feed inlet, 102 oxidant inlet, 103 fluidized air inlet, 104 slag outlet, 105 two-stage cyclone separator, 106 coal gas exhaust fan, 107 coal gas buffer tank, 201 gasifier feed inlet, 202 oxidant inlet, 203 gasifying agent inlet, 204 gas outlet, 205 slag outlet, 301 lower end connecting pipe, 302 pressure valve, 401 cold water tank, 402 heat exchanger, 501 quench tower, 502 two-stage electric tar precipitator, 503 intercooler, 504 tar storage tank, 601 waste heat boiler, 602 mixing tank, 701 carbon monoxide shift unit, 702 decarburization device, 703 gas exhaust fan 704, pressure swing adsorption device, 705 gas holder, 706 fluidized gas pressurizing device.
Detailed Description
The invention will be further elucidated with reference to the following figures and examples:
as shown in fig. 1, the comprehensive treatment and resource utilization system for solid-liquid carbon-containing waste comprises an autothermal pyrolysis furnace 1, a gasification furnace 2, a semicoke transition bin 3, a slag cooling device 4, a crude gas treatment system 5, a synthesis gas pretreatment system 6 and a mixed gas treatment system 7.
The self-heating type pyrolyzing furnace 1 is a normal-pressure low-temperature pyrolyzing furnace, and the temperature is controlled to be 500-600 ℃. A feed inlet 101, an oxidant inlet 102 and a fluidized air inlet 103 are arranged at the lower end of the side wall of the furnace body, and a slag outlet 104 is arranged at the bottom of the furnace; after being pretreated by grinding or chopping, the carbon-containing waste is fed into the pyrolysis furnace 1 through the feed inlet 101, and enters the self-heating pyrolysis furnace 1 together with oxygen fed from the oxidant inlet 102 and fluidized air fed from the fluidized air inlet 103, and a small amount of carbon-containing waste is combusted under the condition of a small amount of oxygen to release heat so as to provide a heat source for the pyrolysis process; performing low-temperature pyrolysis on the rest of the carbon-containing wastes under an anaerobic condition, and allowing pyrolysis products to pass through a two-stage cyclone separator 105 to obtain pyrolysis gas and semicoke; the pyrolysis gas rough gas removal treatment system 5 purifies and extracts tar to finally obtain pure gas, and the pure gas is sent to a gas buffer tank 107 for storage through a gas exhaust fan 106; the semicoke enters the semicoke transition bin 3 for temporary storage.
In the present invention, the carbonaceous waste does not need to be pulped. The carbon-containing waste is directly fed into the pyrolysis furnace after being pretreated by grinding, chopping and the like. Since the grinding and chopping processes are conventional processes, they will not be described in detail.
The raw gas treatment system 5 comprises a quench tower 501, a two-stage electrical tar precipitator 502 (a first-stage electrical tar precipitator and a second-stage electrical tar precipitator), and an intercooler 503 (arranged between the two-stage electrical tar precipitator 502); the pyrolysis gas after passing through the two-stage cyclone separator 105 firstly enters a quench tower 501, water is sprayed for cooling, then water vapor is carried, tar and water in the crude gas are respectively separated through a two-stage electric tar precipitator 502 and an intercooler 503, the tar is sent to a tar storage tank 504 for storage, liquid water is used as a cooling water source of the quench tower 501, and finally pure gas is obtained.
The semicoke transition bin 3 is a closed cylindrical container made of high-temperature-resistant metal materials, the upper end of the semicoke transition bin is connected with an outlet of the two-stage cyclone separator 105, and the lower end of the semicoke transition bin is connected with an inlet at the top end of the gasification furnace; the semicoke powder that comes out by two-stage cyclone falls into semicoke transition bin 3 and temporarily stores, and rethread lower extreme connecting pipe 301 gets into in gasifier 2 as the gasification raw materials, installs pressure valve 302 on lower extreme connecting pipe 301 to the volume of the semicoke powder that the control got into the gasifier.
A feed inlet 201, an oxidant inlet 202 and a gasifying agent inlet 203 are arranged at the top of the gasification furnace 2; sending the semi-coke powder in the semi-coke transition bin 3 into the gasification furnace 2 from the feeding hole 201, sending oxygen from the oxidant inlet 202, and sending saturated steam from the gasification agent inlet 203; under the carrying of oxygen and saturated steam, the semi-coke powder enters the gasification furnace 2 for pyrolysis gasification, and the generated synthesis gas is sent to the waste heat boiler 601 through the gas outlet 204. The residual high-temperature liquid ash is discharged from a slag outlet 205 arranged at the bottom of the furnace and is sent into the slag cooling device 4.
The gasification furnace 2 is a high-temperature pressurized gasification furnace, and the gasification furnace gasifies and decomposes the pyrolysis semicoke in the high-temperature gasification process to generate synthesis gas; the temperature of the gasification furnace is controlled to be 1500-1600 ℃, and the pressure is 0.2-2 MPa.
The slag cooling device 4 is a closed container and comprises a cold water tank 401 and a heat exchanger 402 arranged in the cold water tank, liquid high-temperature ash slag discharged from a slag outlet 205 of the gasification furnace falls into the cold water tank 401, is subjected to water bath quenching, is condensed into bead-shaped solid small slag particles after being cooled, belongs to common solid waste, and can be recycled after being fished out; the heat exchanger 402 can be a shell-and-tube coiled heat exchanger, cooling water is introduced into the tube, and the cooling water is discharged from the cold water tank 401 after exchanging heat with hot water outside the tube.
The synthesis gas pretreatment system 6 comprises a waste heat boiler 601 and a mixing tank 602, wherein high-temperature synthesis gas from the gas outlet 204 of the gasification furnace enters the waste heat boiler 601, releases a large amount of heat, heats cooling water introduced into a pipe of the waste heat boiler to form saturated steam, and outputs the saturated steam which can be used for heating or power generation; the cooled synthesis gas and the coal gas from the coal gas buffer tank 107 are mixed in the mixing tank 602 to form a uniformly-heated and homogeneous mixed gas.
The mixed gas treatment system 7 includes a carbon monoxide shift converter 701, a decarbonizing apparatus 702, a gas exhaust fan 703, a pressure swing adsorption apparatus 704, a gas holder 705, and a fluidized gas pressurizing apparatus 706. The mixed gas from the mixing tank 602 enters a carbon monoxide conversion device 701, and carbon monoxide in the mixed gas reacts with water to generate hydrogen and carbon dioxide; the operating temperature of the carbon monoxide conversion device 701 is 180-280 ℃. The water in the carbon monoxide conversion device 701 is provided with a source by the outlet cooling water of the slag cooling device 4. The mixed gas after carbon monoxide conversion enters the decarburization device 702, and carbon dioxide gas in the mixed gas is separated out and stored or used for producing dry ice. The residual mixed gas enters a pressure swing adsorption device 704 through a gas exhaust fan 703, hydrogen is extracted, and the hydrogen is sent to a tar hydrogenation device to produce a light fuel oil product. The residual mixed gas after hydrogen extraction is sent to a gas holder 705 for storage and outward transportation; wherein a part of the gas is extracted as fluidizing air of the pyrolysis furnace and is sent into the pyrolysis furnace 1 through a fluidizing air pressurizing device 706, so as to ensure the fluidization of bed materials.
Different from a conventional single pyrolysis and gasification device, the invention carries out pyrolysis gasification coupling treatment on various different types of carbon-containing wastes, the materials generated by pyrolysis and gasification are mutually utilized, the heat source is from the materials, the external heat source is not required to be provided, the process flows are interlocked end to end, and the comprehensive treatment, the resource utilization and the circular economy can be realized.
Example 1
Grinding and chopping 1000kg/h carbon-containing waste (heat value 5800kCal/kg), feeding into the pyrolysis furnace through a feed inlet at the lower end of the pyrolysis furnace, and feeding oxygen (287 Nm) into the pyrolysis furnace together with an oxidant inlet3H, 20 ℃) and fluidized air (515 Nm) fed from the fluidized air inlet3The waste materials enter a pyrolysis furnace together at 40 ℃ (600 ℃), wherein 154kg/h of the carbon-containing waste materials are combusted under the condition of a small amount of oxygen to release heat, and a heat source is provided for the pyrolysis process; the rest 846kg/h of carbon-containing waste is pyrolyzed at low temperature under the anaerobic condition, and pyrolysis products pass through a primary cyclone separator and a secondary cyclone separator to obtain pyrolysis gas (551 Nm)3H, water and tar content, 600 ℃) and semicoke (595kg/h, 600 ℃), a pyrolysis gas degassing treatment system for purifying, precipitating water 383kg/h, extracting 85kg/h of tar, and finally obtaining 929Nm pyrolysis gas3And h, entering a gas buffer tank for storage.
The semicoke is sent to the top of the gasification furnace through a semicoke transition bin in oxygen (259 Nm)3The raw materials enter a gasification furnace to be cracked and gasified under the carrying of 394kg/h, 120.24 ℃ and saturated steam (20 ℃), and the parameters of the gasification furnace are as follows: 1600 ℃ and 0.3 MPa. Generated syngas (1457Nm3And h, 1100 ℃ is fed into a waste heat boiler through an air outlet, and the residual high-temperature liquid ash (100kg/h, 1500 ℃) is discharged through a slag outlet and fed into a slag cooling device.
High temperature syngas (1457 Nm) to waste heat boiler3The temperature of 1100 ℃ exchanges heat with cooling water (352kg/h, 20 ℃, 4MPa) introduced into the waste heat boiler, the cooling water is heated into saturated steam (352kg/h, 248 ℃, 3.82MPa) to be output, and the saturated steam can be used for heating or power generation; cooled syngas (1457Nm3A mixed gas (929 Nm) of clean gas and fluidized air from a gas buffer tank at the temperature of/h, 567 DEG C3At 40 deg.C/h, mixing in a mixing tank to obtain a uniformly-heated and homogeneous mixed gas (2386 Nm)3/h，370℃)。
The liquid high-temperature ash slag (100kg/h, 1500 ℃) entering the slag cooling device is subjected to water bath shock cooling in a cold water tank, is condensed into bead-shaped solid small slag particles (100kg/h, 200 ℃) after being cooled, and can be recycled after being fished out; inlet parameters of circulating cooling water: 978kg/h, 20 ℃, exit parameters: 978kg/h, 55.5 ℃.
Gas mixture from mixing tank (2386 Nm)3The mixture enters a carbon monoxide conversion device (200 ℃) at 370 ℃ first, and carbon monoxide (792 Nm) in the mixed gas3H, 370 ℃) and water (584kg/h, 120.24 ℃ saturated steam) sprayed into the shift unit to generate hydrogen and carbon dioxide; the circulating cooling water is provided by outlet cooling water (978kg/h, 55.5 ℃) of the slag cooling device so as to take away heat emitted by the transformation reaction, and the parameters of the outlet circulating cooling water are as follows: 978kg/h, 120.24 ℃ and saturated steam, wherein 584kg/h is sprayed into a conversion device to participate in the carbon monoxide conversion reaction, and the rest 394kg/h is introduced into a gasification furnace as a gasification agent.
Gas mixture after carbon monoxide shift (3113 Nm)3The mixture enters a decarbonization device again at 150 ℃ to remove carbon dioxide gas (966 Nm)3H) separated off, stored or used for producing dry ice. The rest mixed gas enters a pressure swing adsorption device through a gas exhaust fan to remove hydrogen (1523 Nm)3H) extracting, and sending to a tar hydrogenation device to produce a light fuel oil product. Residual mixed gas (CH) after hydrogen extraction4，624Nm3H) sending the materials into a gas holder for storage and outward transportation; in which 515Nm are drawn3The gas is used as fluidized air of the pyrolysis furnace.
Example 2
Grinding and chopping 1000kg/h carbon-containing waste (with a calorific value of 1569kCal/kg), feeding the carbon-containing waste into a pyrolysis furnace through a feed inlet at the lower end of the pyrolysis furnace, and feeding oxygen (1299 Nm/h) into an oxidant inlet3H, 20 ℃) and fluidized air (515 Nm) fed from the fluidized air inlet3The wastes/h and 40 ℃) enter a pyrolysis furnace together (600 ℃), wherein 487kg/h of the carbon-containing wastes are combusted under the condition of a small amount of oxygen to release heat, so that a heat source is provided for the pyrolysis process; the rest 513kg/h carbon-containing waste is pyrolyzed at low temperature under the oxygen-free condition, and pyrolysis products are subjected to a primary cyclone separator and a secondary cyclone separator to obtain pyrolysis gas (346 Nm/m)3Water and tar at 600 deg.C and semicoke at 340kg/h, 600 deg.C, purifying by pyrolysis gas-removing treatment system to obtain water 411kg/h, and extracting30kg/h of tar, and finally obtaining 617Nm of pyrolysis gas3And h, entering a gas buffer tank for storage.
The semicoke is sent to the top of the gasification furnace through a semicoke transition bin in oxygen (89 Nm)3The cracking gasification is carried out in a gasification furnace under the conditions of temperature/h, 20 ℃) and saturated steam (136kg/h, 120.24 ℃), and the parameters of the gasification furnace are as follows: 1600 ℃ and 0.3 MPa. Generated syngas (608 Nm)3And h, 1100 ℃ is fed into a waste heat boiler through an air outlet, and the residual high-temperature liquid ash (11.5kg/h, 1500 ℃) is discharged through a slag outlet and fed into a slag cooling device.
High temperature syngas entering waste heat boiler (608 Nm)3The temperature of 1100 ℃ exchanges heat with cooling water (144kg/h, 20 ℃, 4MPa) introduced into the waste heat boiler, the cooling water is heated into saturated steam (144kg/h, 248 ℃, 3.82MPa) to be output, and the saturated steam can be used for heating or power generation; cooled syngas (608 Nm)3H, 567 ℃) and the mixed gas (617 Nm) of the clean gas and the fluidized air from the gas buffer tank3At 40 deg.C, the mixture is mixed in a mixing tank to obtain a uniformly-heated and homogeneous mixed gas (1225 Nm)3/h，317℃)。
Liquid high-temperature ash (11.5kg/h, 1500 ℃) entering a slag cooling device is subjected to water bath shock cooling in a cold water tank, and is condensed into bead-shaped solid small slag particles (11.5kg/h, 200 ℃) after being cooled, and the small slag particles can be recycled after being fished out; inlet parameters of circulating cooling water: 113kg/h, 20 ℃, exit parameters: 113kg/h, 55.5 ℃.
Mixture from mixing tank (1225 Nm)3The mixture enters a carbon monoxide conversion device (200 ℃) at 317 ℃, and carbon monoxide (267 Nm) in the mixed gas enters3H, 317 ℃) and water (180kg/h, 120.24 ℃ saturated steam) sprayed into the conversion device react to generate hydrogen and carbon dioxide; the circulating cooling water is provided by outlet cooling water (113kg/h, 55.5 ℃) of the slag cooling device and a strand of cooling water (218kg/h, 55.5 ℃) so as to take away heat emitted by the shift reaction, and the parameters of the outlet circulating cooling water are as follows: 331kg/h, 120.24 ℃ and saturated steam, wherein 180kg/h is sprayed into the conversion device to participate in the carbon monoxide conversion reaction, and the residual 151kg/h is introduced into the gasification furnace as a gasification agent.
Carbon monoxide shifted mixture (1449 Nm)3The mixture enters a decarbonization device again at 150 ℃ to remove carbon dioxide gas (354 Nm)3H) separated off, stored or used for producing dry ice. The rest mixed gas enters a pressure swing adsorption device through a gas exhaust fan to remove hydrogen (575 Nm)3H) extracting, and sending to a tar hydrogenation device to produce a light fuel oil product. Residual mixed gas (CH) after hydrogen extraction4，520Nm3H) storing in a gas holder, extracting 515Nm during operation3The gas is used as fluidized air of the pyrolysis furnace.
Claims (7)
1. A comprehensive treatment and resource utilization system for solid-liquid carbon-containing wastes comprises an autothermal pyrolysis furnace, and is characterized by further comprising a gasification furnace, a semicoke transition bin, a slag cooling device, a crude gas treatment system, a synthesis gas pretreatment system and a mixed gas treatment system; wherein the content of the first and second substances,
a feed inlet, an oxidant inlet and a fluidized air inlet are arranged on the side wall of the furnace body of the self-heating pyrolysis furnace; the furnace bottom is provided with a slag outlet, the outlet of the furnace top is sequentially connected with a primary cyclone separator and a secondary cyclone separator, and the outlet at the bottom of the primary cyclone separator is connected with the furnace body; the top outlet of the secondary cyclone separator is connected with a crude gas treatment system, and the bottom outlet of the secondary cyclone separator is connected with a semicoke transition bin; the crude gas treatment system comprises a quench tower, a first-stage electric tar precipitator, an intercooler and a second-stage electric tar precipitator which are sequentially connected, wherein the outlet of the second-stage electric tar precipitator is sequentially connected with a gas exhaust fan and a gas buffer tank, and the second-stage electric tar precipitator is also connected with a tar storage tank;
the top of the gasification furnace is provided with a feed inlet, an oxidant inlet and a gasifying agent inlet, the feed inlet is connected with the bottom outlet of the semicoke transition bin, and a slag outlet at the bottom of the gasification furnace is connected to a slag cooling device; the synthesis gas pretreatment system comprises a waste heat boiler and a mixing tank, wherein a gas outlet is formed in the side wall of the gasification furnace and connected to the waste heat boiler; a synthetic gas outlet of the waste heat boiler and the gas buffer tank are connected to a mixing tank, and the mixing tank is connected with a mixed gas treatment system;
the mixed gas treatment system comprises a fluidized gas pressurizing device, a carbon monoxide conversion device, a decarbonization device and a gas discharge device which are sequentially connectedA fan, a pressure swing adsorption device and a gas holder; wherein, the carbon monoxide conversion device is provided with a water inlet, an air inlet and a steam outlet, the water inlet is connected with a circulating cooling water outlet of the slag cooling device, the air inlet is connected with the mixing tank, and the steam outlet is connected to a gasifying agent inlet of the gasification furnace; the decarbonization device is provided with CO2An outlet and a pressure swing adsorption device are arranged in the H2The mixed gas outlet is simultaneously connected with the gas holder and the fluidized gas pressurizing device; the outlet of the fluidized gas pressurizing device is connected to the fluidized air inlet of the self-heating pyrolysis furnace;
and the systems or the equipment are connected through pipelines.
2. The system of claim 1, wherein the cold slag device is a closed vessel comprising a cold water tank and a heat exchanger disposed in the cold water tank.
3. The system of claim 1, wherein the semi-coke transition bin is a closed cylindrical container, and a bottom outlet of the semi-coke transition bin is connected to a feed inlet at the top of the gasification furnace through a lower end connecting pipe; a pressure valve is arranged on the lower end connecting pipe.
4. The method for realizing comprehensive treatment and resource utilization of solid-liquid carbon-containing waste by using the system of claim 1 is characterized by comprising the following steps of:
(1) feeding the carbon-containing waste subjected to grinding or shredding pretreatment into an autothermal pyrolysis furnace through a feed inlet, feeding oxygen from an oxidant inlet, and feeding fluidized air from a fluidized air inlet; the self-heating type pyrolyzing furnace is a normal-pressure low-temperature pyrolyzing furnace, and the temperature is controlled to be 500-600 ℃; in the furnace, part of the carbon-containing waste is combusted under the condition of oxygen to release heat, so that a heat source is provided for the pyrolysis process; pyrolyzing the rest carbon-containing wastes under an oxygen-free condition; the pyrolysis product passes through a primary cyclone separator and a secondary cyclone separator to obtain pyrolysis gas and semicoke; the pyrolysis gas is sent to a crude gas treatment system for purification treatment;
(2) the pyrolysis gas sent to the crude gas treatment system firstly enters a quench tower, is sprayed with water for cooling, carries with water vapor to sequentially pass through a primary electric tar precipitator, an intercooler and a secondary electric tar precipitator, and respectively separates tar and water in the crude gas; the tar is sent to a tar storage tank for storage, liquid water is used as cooling water of the quench tower for recycling, and the obtained pure coal gas is sent to a coal gas buffer tank for storage through a coal gas exhaust fan;
(3) the powder collected at the bottom of the primary cyclone separator is sent back to the self-heating pyrolysis furnace for continuous reaction, and the semicoke powder collected at the bottom of the secondary cyclone separator is temporarily stored in a semicoke transition bin and then fed from a feed inlet at the top of the gasification furnace; under the carrying of oxygen fed from an oxidant inlet at the top of the furnace and saturated steam fed from an oxidant inlet of the gasification agent, carrying out cracking gasification on semi-coke powder in the furnace, feeding the generated synthesis gas into a synthesis gas pretreatment system through a gas outlet of the furnace body, and discharging liquid ash slag into a slag cooling device through a slag outlet at the bottom of the furnace; the gasification furnace is a high-temperature pressurized gasification furnace, the temperature in the gasification furnace is controlled to be 1500-1600 ℃, and the pressure is 0.2-2 MPa;
(4) the synthesis gas sent to the synthesis gas pretreatment system firstly enters a waste heat boiler, and the released heat heats cooling water in the waste heat boiler into saturated steam which is output for heating or power generation; the cooled synthetic gas and clean coal gas from the coal gas buffer tank enter a mixing tank together to be mixed into uniform-heating and homogeneous mixed gas, and then the mixed gas is sent to a mixed gas treatment system;
(5) the mixed gas from the mixing tank firstly enters a carbon monoxide conversion device, the carbon monoxide in the mixed gas reacts with the circulating cooling effluent water from the slag cooling device to generate hydrogen and carbon dioxide, and the redundant water is heated into saturated steam by heat released by the carbon monoxide conversion reaction and is sent to a gasification furnace as a gasification agent; the mixed gas after carbon monoxide conversion enters a decarbonization device, and carbon dioxide gas in the mixed gas is separated and sent out; the residual mixed gas enters a pressure swing adsorption device through a gas exhaust fan to extract hydrogen; sending the residual mixed gas after extracting hydrogen into a gas holder; part of the extracted gas is sent into the pyrolysis furnace through a fluidizing gas pressurizing device and is used as fluidizing air of the pyrolysis furnace to ensure fluidization of bed materials.
5. The method of claim 4, wherein in step (1), the carbon-containing waste is one or more of coal, biomass, petroleum coke, blue carbon, garbage, crop residue, industrial wastewater waste, sludge, oil sands, or waste activated carbon.
6. The method of claim 4, wherein the carbon monoxide shift converter is operated at a temperature of 180 to 280 ℃; the water in the carbon monoxide conversion device is supplied by a circulating cooling water outlet of the slag cooling device.
7. The method according to claim 4, wherein an annular channel is arranged on the outer wall of the gasification furnace along the periphery of the furnace, 4-8 gasification agent feed inlets which are introduced into the gasification furnace are uniformly distributed on the annular channel, and the gasification agent enters the gasification furnace to participate in gasification in a pressure-equalizing and homogeneous manner.
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