CN111282962B - Method for co-processing organic solid waste and kitchen waste - Google Patents
Method for co-processing organic solid waste and kitchen waste Download PDFInfo
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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
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
- B09B—DISPOSAL OF SOLID WASTE NOT OTHERWISE PROVIDED FOR
- B09B5/00—Operations not covered by a single other subclass or by a single other group in this subclass
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
- B09B—DISPOSAL OF SOLID WASTE NOT OTHERWISE PROVIDED FOR
- B09B2101/00—Type of solid waste
- B09B2101/02—Gases or liquids enclosed in discarded articles, e.g. aerosol cans or cooling systems of refrigerators
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- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Processing Of Solid Wastes (AREA)
- Treatment Of Sludge (AREA)
Abstract
The invention discloses a method for cooperatively treating organic solid waste and kitchen waste, which comprises the following steps: a1, receiving organic solid waste; a2, mixing the organic solid waste, the biogas residue and the backflow biogas slurry uniformly; a3, carrying out wet oxidation on the mixed materials; a4, mechanically dehydrating the oxidized material; B. pretreating the kitchen waste to obtain a solid-liquid mixed phase; b7, hydrolyzing and acidifying the solid-liquid mixed phase; c1, mixing the filtrate obtained from A4 and the acidified material obtained from B7 uniformly, performing anaerobic biogas generation of C2, performing C3 on the obtained digestive juice, and performing D1 on the obtained biogas; c3, mechanically dehydrating the digestive juice to obtain biogas residues and biogas slurry; d1, purifying the obtained biogas; d2, generating power by the purified methane, and enabling the generated high-temperature flue gas to enter D3 and generate electric energy; d3, exchanging heat of the high-temperature flue gas, introducing the obtained high-temperature steam into A3 for supplying power, and introducing circulating hot water into B7 and C2 respectively for supplying heat.
Description
Technical Field
The invention relates to the technical field of solid waste treatment, in particular to a method for cooperatively treating organic solid waste and kitchen waste.
Background
The sewage treatment technology based on the activated sludge method is the mainstream technology adopted by municipal sewage treatment in China at present, and the output of municipal sludge (hereinafter referred to as sludge) is rapidly increased along with the increase of the total sewage treatment amount and the treatment depth. Traditionally, sludge in China is treated in a sanitary landfill mode, but the mode occupies land resources, and the sludge contains a certain amount of organic matters, pathogenic microorganisms, parasitic ova and other toxic and harmful substances, so that the risk of polluting underground water and causing secondary pollution to the environment exists, and the sludge treatment becomes a bottleneck problem of synergy and capacity expansion of sewage plants particularly in large and medium-sized cities with large population density and short land supply, and limits the improvement of the city management level. Therefore, the technology of "harmless treatment, reduction and recycling" is becoming the development direction of sludge treatment at present. Among them, anaerobic digestion is commonly used for sludge treatment, because it not only degrades pollutants but also recovers energy. However, due to the characteristics of low organic matter content, high proportion of refractory parts, low C/N ratio, unbalanced nutrition and the like of the sludge, the sludge has low gas production of single anaerobic digestion, low organic matter conversion rate, long treatment period (more than 30 days) and large occupied area of facilities.
With the improvement of the living standard of urban people and the promotion of the classification work of garbage in China, the yield of the kitchen garbage also tends to rise year by year, the kitchen garbage has complex components and the characteristics of high water content and high organic matter content, is easy to rot and stink without treatment, pollutes the environment, and has great energy-recycling potential including the recycling of grease and methane. At present, anaerobic digestion is the mainstream technology of kitchen waste treatment in China, and according to statistics, over 70% of kitchen waste treatment plants adopt the anaerobic digestion technology. However, the technology also has the problems of easy acidification and unstable operation. Under the condition of high load, the acid production rate of kitchen waste fermentation is high, organic acid is easily accumulated in a system, the pH value of the system is reduced, the methane process is finally inhibited, the system is in failure risk, and the improvement of the treatment efficiency is limited.
The digestion effect can be improved to a certain extent by co-digestion of sludge and kitchen waste or by utilizing a two-phase anaerobic technology. The carbon-nitrogen ratio of the materials can be adjusted through co-digestion, so that the balance of nutrition is ensured, and the gas production efficiency is improved; the two-phase anaerobic phase-splitting of the acidogenesis and the methanogenesis avoids the influence of the acidogenesis on the methanogenesis to a certain extent, and improves the treatment load and the system operation stability. Patent CN 103508643B provides a sewage sludge and kitchen waste treatment device and a method thereof, the patent integrates co-digestion and two-phase anaerobic technology, sludge and kitchen waste are mixed according to a certain proportion and then are subjected to anaerobic fermentation to produce acid and methane, the problems of sludge and kitchen waste in separate treatment are effectively solved, but the method cannot solve the problem that organic matters which are difficult to degrade in sludge interfere the methane production process, the biogas slurry dehydration performance is poor, a large amount of dehydrated mud cakes (biogas residues) are generated, harmlessness is not thorough, secondary pollution is easy to generate, and subsequent treatment is difficult.
By using wet oxidation or catalytic wet oxidation technology, a large amount of refractory organic matters in the sludge can be oxidized and decomposed into carbon dioxide and water, so that harmful organisms such as viruses, germs, parasites and the like in the sludge are effectively inactivated, the volume reduction and decrement of the sludge and the mineralization of sludge cakes are realized, and the dehydration performance of the sludge is greatly improved. Patent CN 104355514B provides a wet oxidation-based sludge treatment method, in which wet sludge with a water content of 90% is subjected to oxidation reaction at a temperature of 240 to 260 ℃ and a pressure of 4.0 to 5.5MPa using oxygen as an oxidizing agent, but this method only treats sludge alone, requires external energy supply, and is expensive in investment and operation. Also, patent CN 104556597B provides a method for catalytic wet oxidation treatment of industrial sludge using powdered activated carbon/Fe3+The composite catalyst is used as a catalyst, oxygen is used as an oxidant, the reaction temperature and the reaction pressure are respectively reduced to 100 ℃ and 2.0MPa, but the treatment object of the method is industrial sludge, external energy supply is still needed, the anaerobic digestion biogas production technology is not integrated, the advantage of synergistic treatment with kitchen waste is not exerted, the energy consumption problem is solved, the treatment cost is reduced, and the thorough harmless treatment of anaerobic digestion biogas residues is realized.
In summary, the existing separate treatment of sludge and kitchen waste has respective technical limitations, the traditional co-digestion does not realize the complete decomposition and conversion of refractory organic matters, the harmless degree of sludge cakes after digestion is insufficient, secondary pollution is easily caused, the wet oxidation or catalysis wet technology of sludge has high operation cost, and the development of a new synergistic treatment technology of sludge and kitchen waste is urgently needed to solve the problems.
Disclosure of Invention
In order to make up for the defects of the prior art, the invention provides a method for cooperatively treating organic solid waste and kitchen waste.
The technical problem of the invention is solved by the following technical scheme:
a method for the cooperative treatment of organic solid waste and kitchen waste comprises the following steps:
a1, receiving: receiving organic solid waste, and conveying the organic solid waste into a homogenizing reactor, wherein the organic solid waste is municipal sludge and/or livestock manure;
a2, homogenizing and mixing: uniformly mixing the organic solid waste conveyed in the step A1, the biogas residues generated in the step C3 and the backflow biogas slurry in the homogenizing reactor;
a3, wet oxidation: under the air or oxygen, carrying out wet oxidation on the material mixed in the step A2 in a reactor;
a4, mechanical dehydration: mechanically dehydrating the material oxidized in the step A3, carrying out the obtained solid phase out, and conveying the obtained filtrate into a homogenizing pool;
B. pretreatment: pretreating the kitchen waste to obtain a solid-liquid mixed phase and an oil phase;
b7, hydrolysis acidification: b, carrying out hydrolysis acidification on the solid-liquid mixed phase obtained in the step B to obtain an acidified material, and conveying the acidified material into the homogenizing pool;
c1, homogenizing and mixing: uniformly mixing the filtrate conveyed in the step A4 and the acidizing material conveyed in the step B7 in the homogenizing pool;
c2, anaerobic biogas production: c3 is carried out on the digestion liquid obtained by anaerobic biogas production of the material treated by C1, and D1 is carried out on the obtained biogas;
c3, mechanical dehydration: mechanically dehydrating the digestive juice, conveying the obtained biogas residues to step A2, allowing a part of the obtained biogas slurry to enter a sewage treatment system, and allowing a part of the biogas slurry to flow back to step A2;
d1, biogas purification: purifying the biogas obtained in the step C2;
d2, biogas power generation: d3 is carried out on the biogas purified in the step D1 to generate electricity, part of the generated electric energy is used for the electricity consumption of the steps in the method, and the rest electric energy is transmitted to a power grid system;
d3, heat exchange treatment: exchanging heat of the high-temperature flue gas generated in the step D2 to obtain high-temperature steam and circulating hot water, introducing the high-temperature steam into the step A3 for energy supply, and introducing the circulating hot water into the step B7 and the step C2 respectively to provide heat.
Preferably, the method further comprises the following steps: b8, mechanical dehydration: and C, mechanically dehydrating the acidified materials obtained in the step B7 to obtain filtrate and a solid phase, conveying the obtained filtrate into the homogenizing pool to carry out the step C1, and conveying the obtained solid phase into the step A2 to mix.
Preferably, in the step A2, the solid content is 5-12 wt%.
Preferably, the conditions of step a3 are: the temperature is 50-250 ℃, the pressure in the reactor is 0.1-3.0 MPa, and the reaction time is 30-240 min.
Preferably, in the step a3, a catalyst is further added for reaction, and the catalyst is a transition metal salt or a transition metal oxide.
Preferably, the conditions of step B7 are: the temperature is 30-70 ℃, the retention time is 2-10 d, and the feed solid content is 5-15 wt%.
Preferably, in the step C2, the conditions are: the temperature is 35-37 ℃, or 50-60 ℃, and the retention time is 15-22 d.
Preferably, the step B includes:
b1, receiving materials: receiving the kitchen waste;
b3, sorting and removing impurities: sorting the kitchen waste received in the step B1 to remove impurities, carrying out outward transportation treatment on the removed impurities, and feeding the kitchen waste subjected to impurity removal into the step B4;
b4, crushing and pulping: b3, crushing the kitchen waste subjected to impurity removal into slurry of which the size is less than 5 mm;
b5, hydrothermal treatment: subjecting the slurry obtained in the step B4 to hydrothermal treatment, wherein the heat of the hydrothermal treatment is derived from the circulating hot water generated in the step D3, and the conditions of the hydrothermal treatment are as follows: the temperature is 60-100 ℃, and the treatment time is 10-240 min;
b6, three-phase separation: and C, carrying out three-phase separation on the slurry subjected to the hydrothermal treatment in the step B5 to obtain an oil phase and a solid-liquid mixed phase, and carrying out the step B7 on the solid-liquid mixed phase.
Preferably, when the material is received in the step B1, the method further includes leaching the kitchen waste, the obtained leachate is subjected to the step B2, and the kitchen waste after leachate is subjected to the step B3; the step B further comprises the following steps: b2, leachate collection: and (4) collecting the leachate generated in the step B1, and conveying the leachate to a step B6 to perform three-phase separation together with the slurry subjected to the hydrothermal treatment of the step B5.
Compared with the prior art, the invention has the advantages that:
in the method, aiming at the problems of low organic matter content, high proportion of refractory parts, poor direct anaerobic digestion performance, low organic matter conversion rate and the like of organic solid wastes (municipal sludge and/or livestock manure), a wet oxidation technology is adopted to strengthen the dissolution of organic matters in a solid phase and the oxidative decomposition of the refractory organic matters, and then the quality division of the organic solid wastes is realized by a mechanical dehydration mode of the step A4, namely the obtained solid phase is basically mineralized (more than 80 percent of the organic matters are transferred into a filtrate); aiming at the problem that the kitchen waste is singly anaerobic and easy to acidify, a two-phase anaerobic technology is adopted to realize the physical phase splitting of an acid production stage (step B7) and a methane production stage (step C2), and the adverse effect of the acid production process on methane production is avoided. After the kitchen waste is fermented to produce acid in the step B7, the kitchen waste and the filtrate obtained in the step A4 are combined and enter a methane-producing phase for co-digestion, the nutrition structure required by a methane-producing system is balanced, the digestion efficiency is improved, the biogas generated by anaerobic digestion is combined in a heat and power cogeneration mode, the generated electric energy meets the self-electricity demand of the system and then is merged into a power grid system, and the generated waste heat can meet the heat demand in each step needing heat.
In a traditional co-digestion system, only 30-40% of the biogas generated is converted into electric energy and 60-70% is converted into heat energy, the heat demand of the methane generation system is only about 20%, and the residual 40-50% of heat is lost. The invention adds wet oxidation technology into the traditional co-digestion system, can fully utilize the original lost heat, not only improves the energy recycling efficiency of the system, but also effectively controls the operation cost. In addition, the wet oxidation technology can be used as a treatment way of the co-digested biogas residues, the problems of difficult treatment and easy generation of secondary pollution of the biogas residues in the prior art are solved, and the basic harmlessness, volume reduction and decrement of the net outflow solid phase of the system are realized. In a word, compared with the traditional technology, the problems of difficult sludge innocent treatment, low organic matter conversion rate and poor volume reduction and decrement effects are solved through an organic coupling wet oxidation technology, a two-phase anaerobic digestion technology and a co-digestion technology, the stability of anaerobic digestion of the kitchen waste is improved, the organic matter conversion rate of the system can reach more than 90%, the treatment period is shortened to 15-22 d, the overall energy recycling efficiency of the system can be improved through a synergistic treatment scheme, the comprehensive energy utilization rate is improved to more than 80% from the traditional 50-60%, and finally the generated solid phase is basically inorganic and convenient to dispose or utilize.
Drawings
FIG. 1 is a schematic flow chart of the method in example 1 of the present invention;
FIG. 2 is a schematic flow chart of a method in embodiment 3 of the present invention.
Detailed Description
The invention will be further described with reference to the accompanying drawings and preferred embodiments. It should be noted that the embodiments and features of the embodiments in the present application may be combined with each other without conflict.
A method for the cooperative treatment of organic solid waste and kitchen waste comprises the following steps:
a1, receiving: receiving and conveying organic solid waste into a homogenizing reactor, wherein the organic solid waste is municipal sludge (such as from a municipal sewage plant) and/or livestock manure;
a2, homogenizing and mixing: uniformly mixing the organic solid waste conveyed in the step A1, the biogas residues generated in the step C3 and the backflow biogas slurry in the homogenizing reactor;
a3, wet oxidation: under the air or oxygen, carrying out wet oxidation on the material mixed in the step A2 in a reactor;
a4, mechanical dehydration: mechanically dehydrating the material oxidized in the step A3, carrying out the obtained solid phase out, and conveying the obtained filtrate into a homogenizing pool;
B. pretreatment: pretreating the kitchen waste to obtain a solid-liquid mixed phase and an oil phase;
b7, hydrolysis acidification: b, carrying out hydrolysis acidification on the solid-liquid mixed phase obtained in the step B to obtain an acidified material, and conveying the acidified material into the homogenizing pool;
c1, homogenizing and mixing: uniformly mixing the filtrate conveyed in the step A4 and the acidizing material conveyed in the step B7 in the homogenizing pool;
c2, anaerobic biogas production: c3 is carried out on the digestion liquid obtained by anaerobic biogas production of the material treated by C1, and D1 is carried out on the obtained biogas;
c3, mechanical dehydration: mechanically dehydrating the digestive juice, conveying the obtained biogas residues to step A2, allowing a part of the obtained biogas slurry to enter a sewage treatment system, and allowing a part of the biogas slurry to flow back to step A2;
d1, biogas purification: purifying the biogas obtained in the step C2;
d2, biogas power generation: d3 is performed on the biogas purified in the step D1, the generated high-temperature flue gas (450-650 ℃), part of the generated electric energy is used for the power consumption of each step in the method, and the rest electric energy is transmitted to a power grid system;
d3, heat exchange treatment: and D, performing heat exchange on the high-temperature flue gas generated in the step D2 to obtain high-temperature steam (100-300 ℃) and circulating hot water (50-100 ℃), and introducing the high-temperature steam into the step A3 for supplying power, wherein the circulating hot water is introduced into the step B7 and the step C2 respectively for supplying heat.
In some preferred embodiments, the method further comprises the steps of: b8, mechanical dehydration: and C, mechanically dehydrating the acidified materials obtained in the step B7 to obtain filtrate and a solid phase, conveying the obtained filtrate into the homogenizing pool to carry out the step C1, and conveying the obtained solid phase into the step A2 to mix.
In some preferred embodiments, the solid content of the mixture in the homogenizing reactor of step A2 is 5-12 wt%.
In some preferred embodiments, the conditions of step a3 are: the temperature is 50-250 ℃, the pressure in the reactor is 0.1-3.0 MPa, and the reaction time is 30-240 min.
In some preferred embodiments, in the step A3, a catalyst is further added for reaction, and the catalyst is a transition metal salt or a transition metal oxide, such as an iron-based catalyst, TiZrO4Ru catalysts (heterogeneous catalysts in which ruthenium is supported on zirconium oxide titanium), and the like.
In some preferred embodiments, in step a3, oxygen is supplied with a purity of 80% or more.
In some preferred embodiments, the conditions of step B7 are: and (C) the temperature is 30-70 ℃, the retention time is 2-10 d, and the solid content of the feed (namely the solid-liquid mixed phase obtained in the step (B)) is 5-15 wt%.
In some preferred embodiments, in the step C2, the conditions are: the temperature is 35-37 ℃, or 50-60 ℃, and the retention time is 15-22 d.
In some preferred embodiments, the step B specifically includes:
b1, receiving materials: receiving the kitchen waste;
b3, sorting and removing impurities: sorting the kitchen waste received in the step B1 to remove impurities, carrying out outward transportation treatment on the removed impurities, and feeding the kitchen waste subjected to impurity removal into the step B4;
b4, crushing and pulping: b3, crushing the kitchen waste subjected to impurity removal into slurry of less than 5 mm;
b5, hydrothermal treatment: subjecting the slurry obtained in the step B4 to hydrothermal treatment, wherein the heat of the hydrothermal treatment is derived from the circulating hot water generated in the step D3, and the conditions of the hydrothermal treatment are as follows: the temperature is 60-100 ℃, and the treatment time is 10-240 min;
b6, three-phase separation: and C, carrying out three-phase separation on the slurry subjected to the hydrothermal treatment in the step B5 to obtain an oil phase and a solid-liquid mixed phase, and carrying out the step B7 on the solid-liquid mixed phase.
In some preferred embodiments, when the step B1 is performed with material receiving, the kitchen waste is subjected to leachate treatment, the obtained leachate is subjected to step B2, and the leachate is subjected to step B3; the step B further comprises the following steps: b2, leachate collection: and (4) collecting the leachate generated in the step B1, and conveying the leachate to a step B6 to perform three-phase separation together with the slurry subjected to the hydrothermal treatment of the step B5.
The following organic solid waste will describe the method of the present invention in detail by taking municipal sludge (hereinafter referred to as "sludge") from a municipal sewage plant as an example.
Example 1
Referring to fig. 1, a method for the cooperative treatment of municipal sludge and kitchen waste comprises the following steps:
a1, receiving: receiving the sludge, and conveying the sludge into a homogenizing reactor to carry out the step A2;
a2, homogenizing and mixing: and C, uniformly mixing the sludge conveyed in the step A1, the biogas residues generated in the step C3 and the backflow biogas slurry in a homogenizing reactor, wherein the solid content of the mixture in the homogenizing reactor is 5-12 wt%, and in the embodiment, the solid content is controlled to be 10 wt%.
A3, wet oxidation: wet oxidizing the material mixed in step a2 in a reactor under air or oxygen, wherein air or oxygen (in this case, oxygen with a purity of 90%) is supplied to the reactor, and oxidizing under the following conditions: the temperature is 50-250 ℃ (220 ℃ in the embodiment), the pressure in the reactor is 0.1-3.0 MPa (3.0 MPa in the embodiment), the reaction time is 30-240 min (60 min in the embodiment), and TiZrO is added4A Ru catalyst.
A4, mechanical dehydration: mechanically dehydrating the material oxidized in the step A3, transporting the obtained solid phase (namely the basically inorganic mud cake) out, and conveying the obtained filtrate into a homogenizing pool to perform the step C1;
b1, receiving materials: receiving the kitchen waste, performing liquid leaching treatment on the kitchen waste, performing step B2 on the obtained leaching liquid, and performing step B3 on the kitchen waste after liquid leaching;
b2, leachate collection: collecting leachate generated in the step B1, and conveying the leachate to a step B6 to be combined with the slurry subjected to the hydrothermal treatment of the step B5 for three-phase separation;
b3, sorting and removing impurities: sorting the kitchen waste received in the step B1 to remove impurities, carrying out outward transportation treatment on the removed impurities, and feeding the kitchen waste subjected to impurity removal into the step B4;
b4, crushing and pulping: b3, crushing the kitchen waste subjected to impurity removal into slurry of less than 5 mm;
b5, hydrothermal treatment: subjecting the slurry obtained in step B4 to hydrothermal treatment to promote the dissolution of fats and oils in the solid phase by hydrothermal reaction, the heat of the hydrothermal treatment being derived from the circulating hot water produced in step D3 below, the conditions of the hydrothermal treatment being: the temperature is 60-100 ℃ (70 ℃ in the embodiment), and the treatment time is 10-240 min (30 min in the embodiment);
b6, three-phase separation: carrying out three-phase separation on the slurry subjected to the hydro-thermal treatment in the step B5 to obtain an oil phase and a solid-liquid mixed phase, wherein the solid-liquid mixed phase is subjected to the step B7, and the oil phase can be used for preparing biodiesel;
b7, hydrolysis acidification: and C, hydrolyzing and acidifying the solid-liquid mixed phase obtained in the step B6 to obtain an acidified material, and conveying the acidified material into a homogenizing pool to perform the step C1, wherein the conditions of the step B7 are as follows: the temperature is 30-70 ℃ (35 ℃ in the embodiment), the retention time is 2-10 d (4 d in the embodiment), and the solid content of the feeding material is 5-15 wt% (10 wt% in the embodiment);
c1, homogenizing and mixing: uniformly mixing the filtrate conveyed in the step A4 and the acidizing material conveyed in the step B7 in a homogenizing pool;
c2, anaerobic biogas production: anaerobic biogas production is carried out on the material treated by the C1, the obtained digestion solution is carried out in the step C3, the obtained biogas is carried out in the step D1, and in the step C2, the conditions are as follows: the temperature is 35-37 ℃ or 50-60 ℃ (35 ℃ in the embodiment), and the retention time is 15-22 d (20 d in the embodiment);
c3, mechanical dehydration: mechanically dehydrating the digestive juice, conveying the obtained biogas residues to step A2, allowing part of the obtained biogas slurry to enter a sewage treatment system for subsequent treatment, and allowing part of the biogas slurry to flow back to step A2;
d1, biogas purification: purifying the biogas obtained in the step C2;
d2, biogas power generation: generating power by using the biogas purified in the step D1, feeding the generated high-temperature flue gas into the step D3, supplying part of the generated electric energy to the power consumption of each step in the method, and transmitting the rest electric energy to a power grid system;
d3, heat exchange treatment: and D, exchanging heat of the high-temperature flue gas generated in the step D2 to obtain high-temperature steam and circulating hot water, introducing the high-temperature steam into the step A3 for energy supply, and introducing the circulating hot water into the step B7, the step C2 and the step B5 respectively to provide heat.
The mechanical dehydration in each step adopts a plate-and-frame filtration mode.
The anaerobic methane generation in the step C2 can adopt reactors with the configurations of UASB, IC, EGSB and the like to realize rapid methane conversion. The liquid phase part is directly anaerobic, so that the mass transfer efficiency of the system is improved, and the anaerobic digestion period can be shortened to 2-7 days.
The method can realize the high-efficiency synergistic anaerobic digestion of municipal sludge and kitchen waste in a quality-divided and phase-splitting manner, the total COD of the sludge before and after the reaction is 93.2g/L and 45.1g/L respectively, the soluble COD after the reaction is 35.7g/L, the organic matter dissolution rate of the sludge is 84.5 percent, the mineralization rate is 51.6 percent, and the unit organic matter biogas yield is 790m3And d, the organic matter conversion rate of the system is 90.8%, the comprehensive energy utilization rate is 85.6%, 100% self-supply of energy is realized, meanwhile, electric energy is output outwards, and finally, the generated sludge is basically inorganic and convenient to dispose or utilize.
Example 2
This example differs from example 1 in that:
the solid content in step A2 was controlled to 5 wt%. In step a 3: the temperature is 180 ℃, the pressure in the reactor is 1.5MPa, the reaction time is 30min, no catalyst is used, and the purity of the supplied oxygen is 80%. In step B5: the hydrothermal treatment temperature is 80 ℃ and the treatment time is 45 min. In step B7: the temperature was 55 ℃, the residence time was 3d, and the feed solids content was 5 wt%. In step C2: the temperature was 55 ℃ and the residence time 15 d.
The method of the embodiment can realize the high-efficiency synergistic anaerobic digestion of municipal sludge and kitchen waste in a quality-divided and phase-splitting manner, the total COD of the sludge before and after the reaction is respectively 46.6g/L and 30.7g/L, the soluble COD after the reaction is 23.6g/L, and the dissolution rate of organic matters in the sludge is 84.8%, compared with the method in example 1The mineralization rate of the organic matter is lower and is 34.1 percent, more organic matters are converted into methane in the anaerobic methane production stage, and the unit organic matter methane yield is 812m3And d, the organic matter conversion rate of the system is 93.3%, the comprehensive energy utilization rate is 86.9%, 100% self-supply of energy is realized, meanwhile, electric energy is output outwards, and finally, the generated sludge is basically inorganic and convenient to dispose or utilize.
Example 3
As shown in fig. 2, it differs from embodiment 1 in that: further comprising the following step B8:
b8, mechanical dehydration: and C, mechanically dehydrating the acidified material obtained in the step B7 in the step B8 to obtain filtrate and a solid phase, conveying the obtained filtrate into a homogenizing pool to perform the step C1, and conveying the obtained solid phase into the step A2 to be mixed with the sludge, the biogas residues and the backflow biogas slurry.
The embodiment of the invention aims at the characteristics of low organic matter content, high proportion of refractory substances and poor direct anaerobic digestion performance of the sludge, adopts a wet oxidation technology to strengthen the decomposition and conversion of the refractory organic matters and the transfer of the refractory organic matters into a liquid phase, then realizes the quality separation of the sludge in a mechanical dehydration mode, the obtained mud cake is basically inorganic, more than 80 percent of organic matters are transferred into the filtrate, the physical phase separation of acid production and methane production stages is realized by adopting a two-phase anaerobic technology aiming at the problem that the kitchen waste is singly anaerobic and easy to acidify, after the kitchen waste is fermented by acid production, the filter liquor which is combined with the wet oxidation of the sludge enters a methane-producing phase for co-digestion, the generated methane can be subjected to cogeneration, the energy requirement of the wet oxidation is met, the generated biogas residue is subjected to the wet oxidation again, and the thorough harmless treatment of the system outflow sludge is realized, namely: the embodiment of the invention integrates wet oxidation, two-phase anaerobic digestion and co-digestion technologies, can cooperatively treat municipal sludge and kitchen waste, realizes the dissolution and mineralization of more than 80% of organic matters in the municipal sludge and co-digested biogas residue by the wet oxidation technology, improves the dehydration performance of the sludge, performs solid-liquid separation by a mechanical dehydration mode, transfers more than 80% of the organic matters into a liquid phase, and basically mineralizes a solid phase. The physical phase splitting of acid production and methane production by kitchen waste fermentation is realized through a two-phase anaerobic digestion technology, the influence of the acid production on the methane production is avoided, and the stability and the treatment load of a system are improved; by combining the sludge catalytic wet oxidation filtrate and the kitchen waste acidification liquid, the nutrition structure required by a methane production system is balanced, and then co-digestion is carried out, so that the digestion efficiency of the system is improved; the generated biogas is subjected to cogeneration, 100% of self-sufficiency of energy is realized, and the residual electric energy can be also merged into a power grid system.
The above examples are given in terms of municipal sludge, and in other examples, other organic solid wastes with poor anaerobic digestion, such as livestock manure, may be treated.
The foregoing is a more detailed description of the invention in connection with specific preferred embodiments and it is not intended that the invention be limited to these specific details. For those skilled in the art to which the invention pertains, several equivalent substitutions or obvious modifications can be made without departing from the spirit of the invention, and all the properties or uses are considered to be within the scope of the invention.
Claims (8)
1. A method for the cooperative treatment of organic solid waste and kitchen waste is characterized by comprising the following steps:
a1, receiving: receiving organic solid waste, and conveying the organic solid waste into a homogenizing reactor, wherein the organic solid waste is municipal sludge and/or livestock manure;
a2, homogenizing and mixing: uniformly mixing the organic solid waste conveyed in the step A1, the biogas residues generated in the step C3 and the backflow biogas slurry in the homogenizing reactor;
a3, wet oxidation: and (2) carrying out wet oxidation on the material mixed in the step A2 in a reactor under the air or oxygen to strengthen the dissolution of organic matters in a solid phase and the oxidative decomposition of organic matters difficult to degrade, wherein the conditions of the step A3 are as follows: the temperature is 50-250 ℃, the pressure in the reactor is 0.1-3.0 MPa, and the reaction time is 30-240 min;
a4, mechanical dehydration: mechanically dehydrating the material oxidized in the step A3, carrying out the obtained solid phase outward, conveying the obtained filtrate into a homogenizing pool, transferring more than 80% of organic matters into the filtrate, and basically mineralizing the solid phase;
B. pretreatment: pretreating the kitchen waste to obtain a solid-liquid mixed phase and an oil phase;
b7, hydrolysis acidification: b, carrying out hydrolysis acidification on the solid-liquid mixed phase obtained in the step B to obtain an acidified material, and conveying the acidified material into the homogenizing pool;
c1, homogenizing and mixing: uniformly mixing the filtrate conveyed in the step A4 and the acidizing material conveyed in the step B7 in the homogenizing pool;
c2, anaerobic biogas production: c3 is carried out on the digestion liquid obtained by anaerobic biogas production of the material treated by C1, and D1 is carried out on the obtained biogas;
c3, mechanical dehydration: mechanically dehydrating the digestive juice, conveying the obtained biogas residues to step A2, allowing a part of the obtained biogas slurry to enter a sewage treatment system, and allowing a part of the biogas slurry to flow back to step A2;
d1, biogas purification: purifying the biogas obtained in the step C2;
d2, biogas power generation: d3 is carried out on the biogas purified in the step D1 to generate electricity, part of the generated electric energy is used for the electricity consumption of the steps in the method, and the rest electric energy is transmitted to a power grid system;
d3, heat exchange treatment: exchanging heat of the high-temperature flue gas generated in the step D2 to obtain high-temperature steam and circulating hot water, introducing the high-temperature steam into the step A3 for energy supply, and introducing the circulating hot water into the step B7 and the step C2 respectively to provide heat.
2. The method for the co-treatment of organic solid waste and kitchen waste according to claim 1, further comprising the steps of:
b8, mechanical dehydration: and C, mechanically dehydrating the acidified materials obtained in the step B7 to obtain filtrate and a solid phase, conveying the obtained filtrate into the homogenizing pool to carry out the step C1, and conveying the obtained solid phase into the step A2 to mix.
3. The method for co-processing the organic solid waste and the kitchen waste according to claim 1 or 2, wherein in the step A2, the solid content is 5-12 wt%.
4. The method for co-processing organic solid waste and kitchen waste according to claim 1 or 2, wherein in step a3, a catalyst is further added for reaction, wherein the catalyst is a transition metal salt or a transition metal oxide.
5. The method for the co-treatment of the organic solid waste and the kitchen waste according to claim 1 or 2, wherein the conditions of the step B7 are as follows: the temperature is 30-70 ℃, the retention time is 2-10 d, and the feed solid content is 5-15 wt%.
6. The method for the co-treatment of the organic solid waste and the kitchen waste according to claim 1 or 2, wherein in the step C2, the conditions are as follows: the temperature is 35-37 ℃, or 50-60 ℃, and the retention time is 15-22 d.
7. The method for the co-treatment of the organic solid waste and the kitchen waste according to claim 1 or 2, wherein the step B comprises:
b1, receiving materials: receiving the kitchen waste;
b3, sorting and removing impurities: sorting the kitchen waste received in the step B1 to remove impurities, carrying out outward transportation treatment on the removed impurities, and feeding the kitchen waste subjected to impurity removal into the step B4;
b4, crushing and pulping: b3, crushing the kitchen waste subjected to impurity removal into slurry of which the size is less than 5 mm;
b5, hydrothermal treatment: subjecting the slurry obtained in the step B4 to hydrothermal treatment, wherein the heat of the hydrothermal treatment is derived from the circulating hot water generated in the step D3, and the conditions of the hydrothermal treatment are as follows: the temperature is 60-100 ℃, and the treatment time is 10-240 min;
b6, three-phase separation: and C, carrying out three-phase separation on the slurry subjected to the hydrothermal treatment in the step B5 to obtain an oil phase and a solid-liquid mixed phase, and carrying out the step B7 on the solid-liquid mixed phase.
8. The method for co-processing organic solid waste and kitchen waste according to claim 7, wherein the step B1 further comprises leaching the kitchen waste when receiving materials, the obtained leachate is subjected to step B2, and the leached kitchen waste is subjected to step B3;
the step B further comprises the following steps:
b2, leachate collection: and (4) collecting the leachate generated in the step B1, and conveying the leachate to a step B6 to perform three-phase separation together with the slurry subjected to the hydrothermal treatment of the step B5.
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| CN112495982A (en) * | 2020-10-22 | 2021-03-16 | 湖北君集水处理有限公司 | Method for converting kitchen waste into wastewater denitrification carbon source through catalytic wet oxidation |
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Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO1995025698A1 (en) * | 1994-03-21 | 1995-09-28 | Otv Omnium De Traitements Et De Valorisation | Method and facility for treating effluents loaded with organic material, particularly by wet oxidation and with internal solid residue recycling, and purification facility therefor |
| CN1405103A (en) * | 2001-09-20 | 2003-03-26 | 中国石化集团齐鲁石油化工公司 | Sludge treatment method |
| CN102092914A (en) * | 2010-12-03 | 2011-06-15 | 东莞市可迪环保科技有限公司 | Sludge treatment device and method |
| CN102950137A (en) * | 2011-08-19 | 2013-03-06 | 光大环保科技发展（北京）有限公司 | Kitchen waste collaborative processing method |
| CN110116126A (en) * | 2019-05-22 | 2019-08-13 | 安徽省通源环境节能股份有限公司 | A kind of kitchen garbage, sludge cooperative disposal method |
| CN110307536A (en) * | 2019-06-13 | 2019-10-08 | 上海电力学院 | It is suitble to the integrated energy system of intensive agricultural production |
-
2020
- 2020-03-02 CN CN202010137737.3A patent/CN111282962B/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO1995025698A1 (en) * | 1994-03-21 | 1995-09-28 | Otv Omnium De Traitements Et De Valorisation | Method and facility for treating effluents loaded with organic material, particularly by wet oxidation and with internal solid residue recycling, and purification facility therefor |
| CN1405103A (en) * | 2001-09-20 | 2003-03-26 | 中国石化集团齐鲁石油化工公司 | Sludge treatment method |
| CN102092914A (en) * | 2010-12-03 | 2011-06-15 | 东莞市可迪环保科技有限公司 | Sludge treatment device and method |
| CN102950137A (en) * | 2011-08-19 | 2013-03-06 | 光大环保科技发展（北京）有限公司 | Kitchen waste collaborative processing method |
| CN110116126A (en) * | 2019-05-22 | 2019-08-13 | 安徽省通源环境节能股份有限公司 | A kind of kitchen garbage, sludge cooperative disposal method |
| CN110307536A (en) * | 2019-06-13 | 2019-10-08 | 上海电力学院 | It is suitble to the integrated energy system of intensive agricultural production |
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