CN114618870B - Multi-source waste resource utilization method - Google Patents
Multi-source waste resource utilization method Download PDFInfo
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- CN114618870B CN114618870B CN202210436352.6A CN202210436352A CN114618870B CN 114618870 B CN114618870 B CN 114618870B CN 202210436352 A CN202210436352 A CN 202210436352A CN 114618870 B CN114618870 B CN 114618870B
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Classifications
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
- B09B—DISPOSAL OF SOLID WASTE NOT OTHERWISE PROVIDED FOR
- B09B3/00—Destroying solid waste or transforming solid waste into something useful or harmless
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B32/00—Carbon; Compounds thereof
- C01B32/50—Carbon dioxide
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F11/00—Treatment of sludge; Devices therefor
- C02F11/02—Biological treatment
- C02F11/04—Anaerobic treatment; Production of methane by such processes
-
- 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
- C10J3/46—Gasification of granular or pulverulent flues in suspension
-
- 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
- C10J3/46—Gasification of granular or pulverulent flues in suspension
- C10J3/48—Apparatus; Plants
- C10J3/50—Fuel charging devices
-
- 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
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0953—Gasifying agents
- C10J2300/0959—Oxygen
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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
-
- 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
- C10J2300/1615—Stripping
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Combustion & Propulsion (AREA)
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- Health & Medical Sciences (AREA)
- Molecular Biology (AREA)
- Hydrology & Water Resources (AREA)
- Water Supply & Treatment (AREA)
- Inorganic Chemistry (AREA)
- Processing Of Solid Wastes (AREA)
Abstract
The invention discloses a multi-source waste resource utilization method, which realizes multi-source solid waste cooperative resource utilization, realizes cooperative anaerobic digestion of kitchen solid waste and sludge, cooperative hydrothermal carbonization of biogas residues and garden waste, and cooperative high-temperature gasification of hydrothermal carbon and byproduct wastewater, effectively improves the solid waste pretreatment efficiency, reduces carbon emission in the recovery process, improves the energy and resource recovery efficiency, reduces waste discharge, and finally realizes higher economic benefit and full life cycle negative carbon emission.
Description
Technical Field
The invention relates to the technical field of solid waste recycling, in particular to a multisource waste recycling method.
Background
According to statistics, the solid waste generated by China is more than 100 hundred million tons every year, so that the problems of environmental pollution and resource waste are very serious. The reasonable resource utilization of the solid wastes can not only avoid resource waste, but also realize the effects of energy conservation, emission reduction and carbon fixation, is an effective way for realizing the aim of 'double carbon', and is an important national strategy for realizing the resource utilization of the solid wastes.
Currently, the major solid waste treatment methods at home and abroad include physical, thermochemical and biological methods.
The typical physical treatment method is a landfill method, and the solid waste landfill treatment process is simple and mature in technology. However, the landfill treatment not only wastes valuable land resources, but also has the problems of long period, secondary pollution of percolate and the like; on the other hand, the organic solid waste in landfills also generates a large amount of greenhouse gases such as methane by the decomposition action of microorganisms.
The biological method mainly aims at aerobic composting or anaerobic digestion treatment of perishable organic solid wastes which have high organic matter content and are easy to biodegrade. The aerobic composting process is simple to operate, mature in technology and capable of realizing resource utilization of solid wastes, but has the problems of long period, large occupied area, limited product fertilizer efficiency quality and safety level and the like. Meanwhile, the biogas slurry and biogas residues generated after anaerobic fermentation are large in production amount, the difficulty in local absorption and utilization is large, and secondary pollution is caused by improper disposal. Therefore, the difficult problems of multi-source solid waste anaerobic fermentation biogas residue digestion and resource gradient utilization need to be solved urgently.
Thermochemical processes are processes that modify the physical, chemical, biological characteristics or composition of solid waste by pyrolysis and deep oxidation of the waste. Incineration is one of the widely used thermochemical disposal methods. However, the solid waste incineration device has large investment and serious gas pollution, and generally needs drying treatment before the incineration of the high-water-content solid waste, thereby not only consuming energy, but also generating a large amount of malodorous tail gas which is difficult to treat.
Therefore, it is desirable to provide a reliable and effective method for treating solid waste.
Disclosure of Invention
In order to solve the defects and shortcomings in the prior art, the invention provides a multi-source waste resource utilization method.
In order to achieve the purpose, the invention provides the following technical scheme:
a resource utilization method of multi-source wastes is characterized in that: the method comprises the following steps:
1) Obtaining kitchen liquid waste and kitchen solid waste through kitchen waste;
2) Mixing the kitchen solid waste obtained in the step 1) with municipal sludge, and then obtaining methane, carbon dioxide, biogas residue and a first byproduct water through an anaerobic digestion process;
3) Mixing the biogas residues obtained in the step 2) with garden wastes, and then carrying out a hydrothermal carbonization process to obtain hydrothermal carbon and a second byproduct water;
4) Mixing the hydrothermal carbon and the second byproduct water obtained in the step 3) and the first byproduct water obtained in the step 2) with industrial organic solid waste and coal to form solid waste coal slurry, and then gasifying at high temperature to obtain slag and synthesis gas.
As a further preferred embodiment of the present invention, in step 1), kitchen waste is pretreated to obtain kitchen liquid waste and kitchen solid waste; the pretreatment step comprises the steps of sorting, cutting, crushing and filtering which are sequentially carried out.
As a further preferred embodiment of the present invention, the step 2) anaerobic digestion process comprises the following steps:
2.1 Feeding the sludge into a slurrying tank for mixing, and introducing reclaimed water and steam into the slurrying tank;
2.2 Feeding the sludge discharged from the slurrying tank and the kitchen solid waste into a mixing tank, and detecting the water content of the mixed slurry in the mixing tank in real time;
2.3 When the water content of the mixed slurry in the mixing tank is greater than or equal to a first preset water content, feeding the mixed slurry in the mixing tank into an anaerobic digestion tank for anaerobic digestion to respectively obtain biogas and biogas slurry;
2.4 Delivering the marsh gas obtained in the step 2.3) into a marsh gas cabinet, and purifying the marsh gas to obtain methane and liquid carbon dioxide;
2.5 Feeding the biogas slurry obtained in the step 2.3) into a biogas slurry storage tank, and detecting the water content of the biogas slurry in the biogas slurry storage tank in real time;
2.6 When the water content of the biogas slurry in the biogas slurry storage tank is greater than or equal to a second preset water content, filtering liquid in the biogas slurry storage tank to obtain biogas residues and biogas slurry, adding a medicament into the biogas residues for dehydration treatment and detecting the water content of the biogas residues in real time, wherein filtrate generated in the biogas residue dehydration step is used as a coal water source material;
2.7 When the water content of the biogas residue is more than or equal to a third preset water content, the biogas residue is used as the hydrothermal carbon raw material.
As a further preferred embodiment of the present invention, the hydrothermal carbonization process in step 3) includes the following steps:
3.1 Constructing a hydrothermal carbonization process parameter response model;
3.2 Determining a hydrothermal carbonization process parameter threshold range;
3.3 Determining an optimal hydrothermal carbonization reaction path;
3.4 Correcting the optimal hydrothermal carbonization reaction path through equipment optimization and numerical simulation;
3.5 Establishing a performance index system suitable for the hydrothermal carbon product obtained by the hydrothermal carbonization process;
3.6 Determining corresponding parameters of the hydrothermal carbon product for replacing the solid waste coal slurry coal.
As a further preferred embodiment of the present invention, the step 4) comprises the steps of:
4.1 Pretreating the hydrothermal carbon and the industrial organic solid waste, feeding the pretreated hydrothermal carbon, the first byproduct water and the second byproduct water into a coal mill for mixing, and continuously introducing coal and water in the mixing process to form solid waste coal slurry;
4.2 Placing the solid waste coal slurry in a temporary storage tank for temporary storage;
4.3 Solid waste coal slurry is pumped into the gasification furnace through a nozzle by a coal slurry pump, and oxygen is introduced into the gasification furnace at the same time;
4.4 The mixed gas discharged from the gasification furnace enters a cyclone separator through a mixer, and slag at the bottom in the gasification furnace is conveyed out through a hopper;
4.5 The cyclone separator carries out gas-liquid separation on the mixed gas, the separated top gas is sent into a water washing tower, and the separated bottom liquid and the bottom liquid of the gasification furnace are sent into an evaporation hot water tower together;
4.6 Gray water is introduced into the hot evaporation water tower, high-temperature water vapor evaporated by the hot evaporation water tower is discharged from the top and introduced into the water washing tower, acid gas discharged by the hot evaporation water tower is discharged from the top after reaching the standard through detection, and redundant liquid at the bottom is discharged from the bottom after reaching the standard through detection;
4.7 Introducing the condensate into the water washing tower, discharging the gas entering the water washing tower from the top after water washing to form synthesis gas, and sending one part of the liquid in the water washing tower into the gasification furnace and sending the other part of the liquid back to the evaporation hot water tower for recycling.
As a further preferred embodiment of the present invention, the step 4.3) further comprises the following steps:
4.3.1 Determining the influence direction and influence degree of slurry factors, pump gas factors and nozzle factors on the atomized particle size distribution and the atomized angle according to the primary fracture and secondary fracture characteristics of the solid waste coal slurry;
4.3.2 Sequencing the slurry factor, the pumping factor and the nozzle factor according to the influence degree;
4.3.3 Determine the adjustment priority of the slurry factor, the pumping factor, and the nozzle factor according to the sorting result.
As a further preferred embodiment of the present invention, the step 4.3.1) further comprises the following steps:
4.3.1.1 Adopting a laser particle sizer to determine the influence direction and the influence degree of solid content, viscosity and rheological property on the atomization particle size distribution and the atomization angle in pump body factors;
4.3.1.2 According to the influence degree, the solid content, the viscosity and the rheological property in the pump body factors are sequenced in sequence;
4.3.1.3 The adjustment priority of solid content, viscosity and rheological property is determined according to the sequencing result.
As a further preferred embodiment of the present invention, the step 4.3.1) further comprises the following steps:
4.3.1.4 Adopting a laser particle size analyzer to determine the influence direction and influence degree of the output pressure, the output gas speed and the output liquid-gas mass ratio of the coal slurry pump to the atomization particle size distribution and the atomization angle in the pumping factors;
4.3.1.5 Sorting the output pressure, the output gas speed and the output liquid-gas mass ratio in sequence according to the influence degree;
4.3.1.6 According to the sorting result, determining the regulation priority of output pressure, output gas speed and output liquid-gas mass ratio.
As a further preferred embodiment of the present invention, the step 4.3.1) further comprises the following steps:
4.3.1.7 Determining the influence direction and influence degree of the nozzle aperture, the nozzle flow velocity and the nozzle angle on the atomization particle size distribution and the atomization angle in the nozzle factors by using a high-speed camera;
4.3.1.8 Sorting the aperture, flow rate and angle of the nozzle according to the degree of influence;
4.3.1.9 Determine the adjustment priority of the nozzle aperture, nozzle flow rate, and nozzle angle based on the sequencing results.
As a further preferred embodiment of the present invention, the direction and degree of influence of the slurry factor, the pump gas factor and the nozzle factor on the atomized particle size distribution and the atomization angle are determined sequentially or simultaneously.
Compared with the prior art, the invention has the following beneficial effects:
1) The invention provides a multi-source waste resource utilization method, which realizes multi-source solid waste cooperative resource utilization, realizes cooperative anaerobic digestion of kitchen solid waste and sludge, cooperative hydrothermal carbonization of biogas residues and garden waste, and cooperative high-temperature gasification of hydrothermal carbon and byproduct wastewater, effectively improves solid waste pretreatment efficiency, reduces carbon emission in a recovery process, improves energy and resource recovery efficiency, reduces waste discharge, and finally realizes higher economic benefit and full life cycle negative carbon emission.
2) The invention provides a resource utilization method of multisource wastes, which is based on different characteristics of multisource solid wastes, combines an anaerobic fermentation process with high energy recovery efficiency, an advanced biomass hydrothermal carbonization process and a relatively mature and advanced coal water slurry gasification process in China, innovatively provides a resource utilization method of multisource wastes with multi-technology integration, realizes the recovery and utilization of biodiesel, industrial and civil gas, building material, chemical products and carbon dioxide with high added value, and really realizes the high-efficiency and cooperative resource utilization and negative carbon emission of multisource solid wastes.
3) The invention provides a multisource waste resource utilization method, which comprises the steps of constructing a hydrothermal carbonization process parameter response model, sequentially determining a hydrothermal carbonization process parameter threshold range, a reaction path, continuously correcting and optimizing the reaction path, establishing a performance index system suitable for a hydrothermal carbonization process obtained hydrothermal carbon product, and determining corresponding parameters of the hydrothermal carbon product for replacing solid waste coal slurry coal, so that continuous correction and optimization of an optimal path of the hydrothermal carbonization process suitable for the multisource waste resource utilization method are realized, the working efficiency of the hydrothermal carbonization process is further improved, and template reference is provided for the hydrothermal carbonization process in the multisource waste resource utilization method.
4) The invention provides a resource utilization method of multi-source wastes, which is characterized in that according to the characteristics of primary fracture and secondary fracture of solid waste coal slurry, the influence direction and the influence degree of slurry factors, pump factors and nozzle factors on the distribution of atomized particle size and atomized angle are determined; sequencing the slurry factor, the pumping factor and the nozzle factor according to the influence degree; and determining the adjustment priorities of the slurry factors, the pump gas factors and the nozzle factors according to the sequencing result, thereby improving the adjustment efficiency of correcting and optimizing the high-temperature gasification process, saving the debugging time of parameter optimization of the process and equipment correction, and further improving the working efficiency and reliability of the high-temperature gasification process.
Drawings
FIG. 1 is a flow chart of the steps of the present invention.
FIG. 2 is a flow diagram of the steps of the anaerobic digestion process of the present invention.
FIG. 3 is a flow chart of the steps of the hydrothermal carbonization process of the present invention.
FIG. 4 is a flow chart of the steps of the high temperature gasification process of the present invention.
Detailed Description
The technical solution in the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings in the embodiments of the present invention.
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be obtained by a person skilled in the art without making any creative effort based on the embodiments in the present invention, belong to the protection scope of the present invention.
In the description of the present invention, it should be noted that the terms "upper", "lower", "inner", "outer", "front", "rear", "both ends", "one end", "the other end", and the like indicate orientations or positional relationships based on those shown in the drawings, and are only for convenience of description and simplicity of description, but do not indicate or imply that the referred device or element must have a specific orientation, be constructed in a specific orientation, and be operated, and thus, should not be construed as limiting the present invention. Furthermore, the terms "first" and "second" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance.
In the description of the present invention, it is to be noted that, unless otherwise explicitly specified or limited, the terms "mounted," "disposed," "connected," and the like are to be construed broadly, such as "connected," which may be fixedly connected, detachably connected, or integrally connected; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meanings of the above terms in the present invention can be understood in specific cases to those skilled in the art.
Fig. 1 shows a method for recycling multi-source waste provided by this embodiment, which includes the following steps:
1) Obtaining kitchen liquid waste and kitchen solid waste through kitchen waste; in the embodiment, kitchen waste is pretreated to obtain kitchen liquid waste and kitchen solid waste; the pretreatment step comprises the steps of sorting, cutting, crushing and filtering in sequence; thereby effectively realizing the solid-liquid separation of the kitchen liquid waste and the kitchen solid waste in the kitchen waste; wherein the kitchen liquid waste comprises grease which can be used as a raw material of biodiesel;
2) Mixing the kitchen solid waste obtained in the step 1) with municipal sludge, and then obtaining methane, carbon dioxide, biogas residue and a first byproduct water through an anaerobic digestion process; wherein, methane can be used as industrial and civil fuel gas, carbon dioxide can be used for capturing resources and utilizing, liquid carbon dioxide or dry ice can be prepared, biogas residues can be used in the hydrothermal carbonization process with garden wastes, and the first byproduct water can participate in the high-temperature gasification process;
3) Mixing the biogas residues obtained in the step 2) with garden wastes, and then carrying out a hydrothermal carbonization process to obtain hydrothermal carbon and a second byproduct water; the hydrothermal char and the second by-product water obtained in this step may be used in a high temperature gasification process;
4) Mixing the hydrothermal carbon and the second byproduct water obtained in the step 3) and the first byproduct water obtained in the step 2) with industrial organic solid waste and coal to form solid waste coal slurry, and then gasifying the solid waste coal slurry at high temperature to obtain slag and synthesis gas; wherein the industrial organic solid waste contains oil-containing sludge, dregs of a decoction, active carbon and other components, the obtained slag can be used as a building material raw material, and the obtained synthesis gas can be used as a raw material for manufacturing chemical products.
According to the multisource waste resource utilization method provided by the invention, the multi-source solid waste is utilized in a coordinated resource manner, the kitchen solid waste and the sludge are subjected to coordinated anaerobic digestion, the biogas residue and the garden waste are subjected to coordinated hydrothermal carbonization, and the hydrothermal carbon and the byproduct wastewater are subjected to coordinated high-temperature gasification, so that the solid waste pretreatment efficiency is effectively improved, the carbon emission in the recovery process is reduced, the energy and resource recovery efficiency is improved, the waste discharge is reduced, and the higher economic benefit and the full life cycle negative carbon emission are finally realized; based on different characteristics of multi-source solid wastes, an anaerobic fermentation process with high energy recovery efficiency, an advanced biomass hydrothermal carbonization process and a domestic relatively mature and advanced coal water slurry gasification process are combined, a multi-technology integrated multi-source waste resource utilization method is innovatively provided, the recovery and utilization of biodiesel, industrial and civil gas, building material raw materials, chemical products and carbon dioxide with high added values are realized, and the high-efficiency and synergistic resource utilization and negative carbon emission of the multi-source solid wastes are really realized
As shown in fig. 2, the anaerobic digestion process of step 2) of the method provided in this embodiment includes the following steps:
2.1 Feeding the sludge into a slurrying tank for mixing, and introducing reclaimed water and steam into the slurrying tank; in the embodiment, the water content of the sludge is adjusted by adding reclaimed water and forming mixed slurry through accelerated stirring, and meanwhile, the consumption of clean water resources in the stirring process is reduced; the function of adding steam is to realize temperature rise so as to form mixed slurry through rapid mixing;
2.2 Feeding the sludge discharged from the pulping tank and the kitchen solid waste into a mixing tank, and detecting the water content of the mixed slurry in the mixing tank in real time;
2.3 When the water content of the mixed slurry in the mixing tank is greater than or equal to a first preset water content, feeding the mixed slurry in the mixing tank into an anaerobic digestion tank for anaerobic digestion to respectively obtain biogas and biogas slurry; in this embodiment, the first preset water content is set to 90% to ensure that the anaerobic digestion reaction process is smoothly performed so as to smoothly obtain biogas and biogas slurry;
2.4 Delivering the marsh gas obtained in the step 2.3) into a marsh gas cabinet, and purifying the marsh gas to obtain methane and liquid carbon dioxide; wherein methane can be used as industrial and civil gas, and carbon dioxide can be used for capturing resource utilization
2.5 Feeding the biogas slurry obtained in the step 2.3) into a biogas slurry storage tank, and detecting the water content of the biogas slurry in the biogas slurry storage tank in real time;
2.6 When the water content of the biogas slurry in the biogas slurry storage tank is greater than or equal to a second preset water content, in this embodiment, the second preset water content is set to 93.5%, liquid inside the biogas slurry storage tank is filtered to obtain biogas residues and biogas slurry, a medicament is added into the biogas residues to perform dehydration treatment and detect the water content of the biogas residues in real time, and filtrate generated in the biogas residue dehydration step is used as a water coal raw material; in the embodiment, the agent can be selected from Polyacrylamide (PAM) to carry out water quality treatment on the biogas residues so as to realize the cleaning of the hydrothermal carbon raw material;
2.7 When the water content of the biogas residue is larger than or equal to the third preset water content, the biogas residue is used as the hydrothermal carbon raw material, and the water content of the biogas residue meets the preset water content requirement, so that the smooth operation of a subsequent high-temperature gasification process involving the hydrothermal carbon as the raw material can be ensured.
The hydrothermal carbonization process takes biomass (including biogas residues and garden wastes in the embodiment) as a raw material, takes water as a liquid phase reaction medium, and converts the biomass into a series of high value-added products mainly comprising biochar at a certain temperature (150-250 ℃) and under a certain pressure (2-10 MPa).
As shown in fig. 3, the method provided in this embodiment, in step 3), the hydrothermal carbonization process includes the following steps:
3.1 Constructing a hydrothermal carbonization process parameter response model; the established model is used for carrying out process parameter threshold value range demarcation, optimal reaction path determination and correction, performance index system establishment, corresponding parameters for replacing solid waste coal slurry coal and the like;
3.2 Determining the threshold range of the parameters of the hydrothermal carbonization process; the optimal reaction path can be determined within a reliable and effective threshold range by determining the threshold range of the process parameter, and the correction efficiency of the optimal reaction path is influenced by determining the threshold range of the process parameter, so that the determination of the threshold range of the process parameter generally needs to be determined by combining empirical parameters and the actual working environment on site;
3.3 Determining an optimal hydrothermal carbonization reaction path; the optimal hydrothermal carbonization reaction path is a preliminary path, and the preliminary path needs to be further corrected and optimized in the modes of equipment optimization, numerical simulation and the like in the follow-up process;
3.4 Correcting the optimal hydrothermal carbonization reaction path through equipment optimization and numerical simulation; the skilled in the art knows that the modification of the optimal hydrothermal carbonization reaction path can also be realized in the aspects of artificial efficiency, raw material quality and the like, and in this embodiment, only an economic and feasible equipment optimization and numerical simulation mode is selected to realize the modification, and in this embodiment, in order to ensure the effectiveness and reliability of the modification, the priority of the numerical simulation is higher than the priority of the equipment optimization;
3.5 Establishing a performance index system suitable for the hydrothermal carbon product obtained by the hydrothermal carbonization process; thereby providing template reference for the hydrothermal carbonization process in the multi-source waste resource utilization method;
3.6 Determining corresponding parameters of the hydrothermal carbon product for replacing solid waste coal slurry coal so as to further realize the actual operation of multi-source waste resource utilization.
As shown in fig. 4, in step 4) of the method provided in this embodiment, the following steps are included:
4.1 Pretreating the hydrothermal carbon and the industrial organic solid waste, feeding the pretreated hydrothermal carbon, the first byproduct water and the second byproduct water into a coal mill for mixing, and continuously introducing coal and water in the mixing process to form solid waste coal slurry; the multisource waste replaces partial raw materials to be mixed with coal and water to form solid waste coal slurry, so that the solid waste is utilized, and meanwhile, the actual conversion efficiency of the multisource waste relative to the raw materials can be determined compared with the original pure raw materials, and data basis is provided for continuous optimization and correction of technological process parameters in the later period;
4.2 Placing the solid waste coal slurry in a temporary storage tank for temporary storage;
4.3 Solid waste coal slurry is pumped into the gasification furnace through a nozzle by a coal slurry pump, and oxygen is introduced into the gasification furnace at the same time; so as to supplement oxygen required by the high-temperature gasification process in the gasification furnace; as known to those skilled in the art, a gasifier generally comprises a gasification chamber and a combustion chamber (also referred to as a reduction chamber). After the gasification chamber utilizes fuel combustion to generate a temperature field of about 800 ℃, the fuel is gradually fed into the gasification chamber, and the fuel is cracked and gasified in a proper temperature field. The combustible gas generated at the moment enters the combustion chamber along with the flame generated by the complete combustion of part of the fuel, and the combustion chamber is a heat insulation combustion chamber, so that the heat insulation performance is sufficient, and the heat dissipation loss is reduced. When high-temperature flame generated by full combustion of part of fuel enters the combustion chamber along with combustible gas, the combustible gas is mixed and combusted in the combustion chamber by virtue of the high-temperature flame, the temperature is gradually increased to 900-1100 ℃, and then high-temperature gasification staged combustion begins to occur. The continuous operation of gasification combustion is ensured through the continuous input of oxygen, and heat energy is output to do work. The combustible gas is combusted in the combustion chamber, the temperature field is 900-1100 ℃, when the temperature field is more than or equal to 800 ℃, the ignition point of the combustible gas is greatly exceeded, as long as oxygen is met, violent chemical reaction can occur, and the ignition and combustion stability is excellent. When the temperature field is more than or equal to 900 ℃, even if the oxygen content is 5 percent, stable combustion flame can be obtained. At this time, since the combustion reaction activation energy of the combustible gas with oxygen is much lower than the reaction activation energy of oxygen atoms with nitrogen, the combustible gas first undergoes a combustion reaction with oxygen, and only when oxygen remains, the combustible gas reacts with nitrogen atoms to generate NOx. Sufficient temperature and combustion space expand the flame combustion area, the combustion chamber (reduction chamber) does not generate hot spots, and the temperature distribution is uniform, so that the generation of NOx is greatly reduced, and low nitrogen emission is realized.
4.4 The mixed gas discharged from the gasification furnace enters a cyclone separator through a mixer, and slag at the bottom of the gasification furnace is conveyed out through a hopper; the transported slag can be used as a building material raw material;
4.5 The cyclone separator carries out gas-liquid separation on the mixed gas, the separated top gas is sent into a water washing tower for cleaning, and the separated bottom liquid and the bottom liquid of the gasification furnace are sent into an evaporation hot water tower together to serve as a supplementary raw material of the evaporation hot water tower;
4.6 Gray water is introduced into the hot evaporation water tower, high-temperature water vapor evaporated by the hot evaporation water tower is discharged from the top and introduced into the water washing tower, acid gas discharged by the hot evaporation water tower is discharged from the top after reaching the standard through detection, and redundant liquid at the bottom is discharged from the bottom after reaching the standard through detection; in this embodiment, the greywater is water coming out of washbasins and floor drains, as opposed to black water, and the effect of the greywater is to reduce the amount of clean water consumed in the evaporating water heater.
4.7 Introducing a condensate into the water washing tower, discharging the gas entering the water washing tower from the top after washing to form synthesis gas, and sending one part of the liquid in the water washing tower into the gasification furnace and sending the other part of the liquid back to the evaporation hot water tower for recycling.
As a further preferred embodiment of the present invention, the step 4.3) further comprises the following steps:
4.3.1 According to the primary fracture and secondary fracture characteristics of the solid waste coal slurry, determining the influence direction and influence degree of slurry factors, pump gas factors and nozzle factors on the atomized particle size distribution and the atomized angle; therefore, the influence directions and the influence degrees of the slurry factors, the pump gas factors and the nozzle factors on the atomization particle size distribution and the atomization angle are respectively determined, so that the influence degrees and the adjustment priorities are determined in the correction and optimization processes of the corresponding slag and the synthesis gas obtained through the high-temperature gasification process, and therefore, on one hand, the efficiency of optimization and correction is improved, and on the other hand, the adjustment efficiency during later-stage adaptive adjustment (for example, adaptive adjustment aiming at equipment optimization and replacement, product raw material replacement and the like) can also be improved.
4.3.2 Sequencing the slurry factor, the pumping factor and the nozzle factor according to the influence degree; since there may be an influence factor having a large unit adjustment amount and a small overall influence range, in this embodiment, the influence degree refers to the overall influence range of each factor; for example, the adjustment of the unit content of a certain component in the slurry factor has a large influence on the atomized particle size distribution, while the adjustment of the content of the whole component of the slurry factor has the smallest influence on the whole range of the atomized particle size distribution, and therefore the influence of the slurry factor is considered to be the lowest in this embodiment.
4.3.3 The adjustment priorities of the slurry factors, the pumping factors and the nozzle factors are determined according to the sequencing results, so that the efficiency of optimizing and correcting the process is improved on one hand, and the adjustment efficiency during later-period adaptive adjustment (such as adaptive adjustment for equipment optimization and replacement, product raw material replacement and the like) is also improved on the other hand.
As a further preferable implementation manner of this embodiment, the step 4.3.1) further includes the following steps:
4.3.1.1 Adopting a laser particle sizer to determine the influence direction and the influence degree of solid content, viscosity and rheological property on the atomization particle size distribution and the atomization angle in pump body factors; therefore, the influence directions and the influence degrees of the solid content, the viscosity and the rheological property in the slurry factors on the atomization particle size distribution and the atomization angle are respectively determined, so that the influence degrees and the adjustment priorities are determined in the correction and optimization processes of the corresponding slag and the synthesis gas obtained through the high-temperature gasification process, and therefore, on one hand, the efficiency of optimization and correction is improved, and on the other hand, the adjustment efficiency during later-stage adaptive adjustment (for example, adaptive adjustment aiming at equipment optimization and replacement, product raw material replacement and the like) can also be improved.
4.3.1.2 Sorting the solid holdup, viscosity and rheological property of the pump body factors according to the influence degree;
4.3.1.3 The adjustment priorities of the solid content rate, the viscosity and the rheological property are determined according to the sequencing result, so that when the slurry factor is corrected and optimized, the adjustment priorities in the correction optimization process of the solid content rate, the viscosity and the rheological property and the adjustment priorities in the later adaptive adjustment process are determined.
As a further preferable implementation manner of this embodiment, the step 4.3.1) further includes the following steps:
4.3.1.4 Adopting a laser particle size analyzer to determine the influence direction and influence degree of the output pressure, the output gas speed and the output liquid-gas mass ratio of the coal slurry pump to the atomization particle size distribution and the atomization angle in the pumping factors; therefore, the influence direction and the influence degree of the output pressure, the output gas speed and the output liquid-gas mass ratio of the coal slurry pump in the pump gas factors on the atomizing particle size distribution and the atomizing angle are respectively determined, and the influence degree and the regulation priority are determined in the correction and optimization process of obtaining the corresponding slag and the synthesis gas through the high-temperature gasification process, so that the optimization correction efficiency is improved on one hand, and the regulation efficiency in the later-stage adaptability regulation (such as the adaptability regulation aiming at equipment optimization and replacement, product raw material replacement and the like) can also be improved on the other hand.
4.3.1.5 Sorting the output pressure, the output gas speed and the output liquid-gas mass ratio in sequence according to the influence degree;
4.3.1.6 Output pressure, output gas speed and output liquid-gas mass ratio according to the sequencing result, so that when the pumping factor is corrected and optimized, the adjustment priority in the correction optimization process of the output pressure, the output gas speed and the output liquid-gas mass ratio and the adjustment priority in the later adaptive adjustment process are determined.
As a further preferable implementation manner of this embodiment, in step 4.3.1), the method further includes the following steps:
4.3.1.7 Determining the influence direction and influence degree of the nozzle aperture, the nozzle flow velocity and the nozzle angle on the atomization particle size distribution and the atomization angle in the nozzle factors by using a high-speed camera; therefore, the influence directions and the influence degrees of the nozzle aperture, the nozzle flow velocity and the nozzle angle on the atomization particle size distribution and the atomization angle in the nozzle factors are respectively determined, so that the influence degrees and the adjustment priorities are determined in the correction and optimization processes of obtaining the corresponding slag and the synthesis gas through the high-temperature gasification process, and therefore, on one hand, the efficiency of optimization and correction is improved, and on the other hand, the adjustment efficiency during later-stage adaptive adjustment (for example, adaptive adjustment aiming at equipment optimization and replacement, product raw material replacement and the like) can also be improved.
4.3.1.8 Sequencing the aperture, the flow speed and the angle of the nozzle according to the influence degree;
4.3.1.9 Determining the adjustment priorities of the nozzle aperture, the nozzle flow rate and the nozzle angle according to the sequencing result, so as to determine the adjustment priorities in the correction optimization process and the later adaptive adjustment process of the nozzle aperture, the nozzle flow rate and the nozzle angle when correcting and optimizing the nozzle factors.
In addition, as further optimization, the influence direction and the influence degree of the slurry factor, the pump gas factor and the nozzle factor on the atomization particle size distribution and the atomization angle are determined sequentially or synchronously, and when the influence direction and the influence degree of the slurry factor, the pump gas factor and the nozzle factor on the atomization particle size distribution and the atomization angle are determined sequentially, the influence direction and the influence degree of single factor change on the atomization particle size distribution and the atomization angle are convenient to know, and the result is visual and reliable; the influence direction and the influence degree of slurry factors, pump gas factors and nozzle factors on the atomized particle size distribution and the atomized angle can be determined simultaneously, and the coordination influence of a plurality of factors can be determined; those skilled in the art will appreciate that the sequential and synchronous combinations may be used to meet practical application requirements.
Although the present invention has been described in detail with reference to the foregoing embodiments, it will be apparent to those skilled in the art that various changes in the embodiments and/or modifications of the invention can be made, and equivalents and modifications of some features of the invention can be made without departing from the spirit and scope of the invention.
Claims (4)
1. A resource utilization method of multi-source wastes is characterized in that: the method comprises the following steps:
1) Obtaining kitchen liquid waste and kitchen solid waste through kitchen waste;
2) Mixing the kitchen solid waste obtained in the step 1) with municipal sludge, and then obtaining methane, carbon dioxide, biogas residue and a first byproduct water through an anaerobic digestion process;
3) Mixing the biogas residues obtained in the step 2) with garden wastes, and then carrying out a hydrothermal carbonization process to obtain hydrothermal carbon and a second byproduct water;
4) Mixing the hydrothermal carbon and the second byproduct water obtained in the step 3) and the first byproduct water obtained in the step 2) with industrial organic solid waste and coal to form solid waste coal slurry, and then gasifying the solid waste coal slurry at high temperature to obtain slag and synthesis gas;
the step 4) comprises the following steps:
4.1 Pretreating the hydrothermal carbon and the industrial organic solid waste, feeding the pretreated hydrothermal carbon, the first byproduct water and the second byproduct water into a coal mill for mixing, and continuously introducing coal and water in the mixing process to form solid waste coal slurry;
4.2 Placing the solid waste coal slurry in a temporary storage tank for temporary storage;
4.3 Solid waste coal slurry is pumped into the gasification furnace through a nozzle by a coal slurry pump, and oxygen is introduced into the gasification furnace at the same time;
4.4 The mixed gas discharged from the gasification furnace enters a cyclone separator through a mixer, and slag at the bottom in the gasification furnace is conveyed out through a hopper;
4.5 The cyclone separator carries out gas-liquid separation on the mixed gas, the separated top gas is sent into a water washing tower, and the separated bottom liquid and the bottom liquid of the gasification furnace are sent into an evaporation hot water tower together;
4.6 Gray water is introduced into the hot evaporation water tower, high-temperature water vapor evaporated by the hot evaporation water tower is discharged from the top and introduced into the water washing tower, acid gas discharged by the hot evaporation water tower is discharged from the top after reaching the standard through detection, and redundant liquid at the bottom is discharged from the bottom after reaching the standard through detection;
4.7 Introducing condensate into the water washing tower, discharging the gas entering the water washing tower from the top after water washing to form synthesis gas, and sending one part of liquid in the water washing tower into the gasification furnace and sending the other part of liquid back to the evaporation hot water tower for recycling;
in the step 4.3), the method further comprises the following steps:
4.3.1 Determining the influence direction and influence degree of slurry factors, pump gas factors and nozzle factors on the atomized particle size distribution and the atomized angle according to the primary fracture and secondary fracture characteristics of the solid waste coal slurry;
4.3.2 Sorting the slurry factors, the pumping factors and the nozzle factors according to the influence degree;
4.3.3 Determining the adjustment priority of the slurry factor, the pumping factor and the nozzle factor according to the sequencing result;
in the step 4.3.1), the method further comprises the following steps:
4.3.1.1 Adopting a laser particle sizer to determine the influence direction and the influence degree of solid content, viscosity and rheological property on atomization particle size distribution and atomization angle in slurry factors;
4.3.1.2 Sorting the solid content, viscosity and rheological property of the slurry factors according to the influence degree;
4.3.1.3 Determining the adjustment priority of solid content rate, viscosity and rheological property according to the sequencing result;
in the step 4.3.1), the method further comprises the following steps:
4.3.1.4 Adopting a laser particle size analyzer to determine the influence direction and the influence degree of the output pressure, the output gas speed and the output liquid-gas quality ratio of the coal slurry pump to the atomized particle size distribution and the atomized angle in the pumping factors;
4.3.1.5 Sequencing output pressure, output gas speed and output liquid-gas mass ratio according to the influence degree;
4.3.1.6 Determining the adjustment priority of output pressure, output gas speed and output liquid-gas mass ratio according to the sequencing result;
in the step 4.3.1), the method further comprises the following steps:
4.3.1.7 Determining the influence direction and influence degree of the nozzle aperture, the nozzle flow velocity and the nozzle angle on the atomization particle size distribution and the atomization angle in the nozzle factors by using a high-speed camera;
4.3.1.8 Sequencing the aperture, the flow speed and the angle of the nozzle according to the influence degree;
4.3.1.9 Determining the adjustment priority of the aperture, the flow speed and the angle of the nozzle according to the sequencing result;
and determining the influence direction and the influence degree of slurry factors, pump gas factors and nozzle factors on the atomized particle size distribution and the atomized angle in sequence or synchronously.
2. The resource utilization method of the multi-source waste according to claim 1, characterized in that: in the step 1), kitchen waste is pretreated to obtain kitchen liquid waste and kitchen solid waste; the pretreatment step comprises the steps of sorting, cutting, crushing and filtering which are sequentially carried out.
3. The resource utilization method of the multi-source waste according to claim 1, characterized in that: the anaerobic digestion process in the step 2) comprises the following steps:
2.1 Feeding the sludge into a slurrying tank for mixing, and introducing reclaimed water and steam into the slurrying tank;
2.2 Feeding the sludge discharged from the slurrying tank and the kitchen solid waste into a mixing tank, and detecting the water content of the mixed slurry in the mixing tank in real time;
2.3 When the water content of the mixed slurry in the mixing tank is greater than or equal to a first preset water content, feeding the mixed slurry in the mixing tank into an anaerobic digestion tank for anaerobic digestion to respectively obtain biogas and biogas slurry;
2.4 Delivering the biogas obtained in the step 2.3) into a biogas gas holder, and purifying the biogas to obtain methane and liquid carbon dioxide;
2.5 Feeding the biogas slurry obtained in the step 2.3) into a biogas slurry storage tank, and detecting the water content of the biogas slurry in the biogas slurry storage tank in real time;
2.6 When the water content of the biogas slurry in the biogas slurry storage tank is greater than or equal to a second preset water content, filtering liquid in the biogas slurry storage tank to obtain biogas residues and biogas slurry, adding a medicament into the biogas residues for dehydration treatment and detecting the water content of the biogas residues in real time, wherein filtrate generated in the biogas residue dehydration step is used as a coal water source material;
2.7 When the water content of the biogas residue is larger than or equal to the third preset water content, the biogas residue is used as the hydrothermal carbon raw material.
4. The resource utilization method of the multi-source waste according to claim 1, characterized in that: the hydrothermal carbonization process in the step 3) comprises the following steps:
3.1 Constructing a hydrothermal carbonization process parameter response model;
3.2 Determining the threshold range of the parameters of the hydrothermal carbonization process;
3.3 Determining an optimal hydrothermal carbonization reaction path;
3.4 Correcting the optimal hydrothermal carbonization reaction path through equipment optimization and numerical simulation;
3.5 Establishing a performance index system suitable for the hydrothermal carbon product obtained by the hydrothermal carbonization process;
3.6 Determining corresponding parameters of the hydrothermal carbon product for replacing the solid waste coal slurry coal.
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