CN117700059A - Cooperative treatment system and method for sludge and organic waste - Google Patents
Cooperative treatment system and method for sludge and organic waste Download PDFInfo
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Classifications
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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
Abstract
The invention discloses a system and a method for cooperatively treating sludge and organic waste. The treatment system comprises a cooperative anaerobic pretreatment unit, an anaerobic digestion unit and a drying treatment unit which are sequentially connected; the cooperative anaerobic pretreatment unit comprises a cooperative anaerobic pretreatment tank and a mechanical circulation pretreatment device; the anaerobic digestion unit comprises a first anaerobic digestion tank and a second anaerobic digestion tank; the drying treatment unit comprises sludge drying equipment, a sludge dewatering device and a dewatered sludge bin. The system and the method realize the serosity of materials, provide uniform, good rheological property and high reaction efficiency liquefied slurry for anaerobic digestion, further improve biogas productivity, reduce stirring energy consumption, avoid scum generation at the upper layer of an anaerobic digestion tank, obtain higher gas yield in a shorter anaerobic reaction time, realize self-sufficiency of heat energy, realize further energy utilization in a biogas purification production natural gas or biogas power generation mode, and realize efficient treatment and balance of heat energy.
Description
Technical Field
The invention relates to a system and a method for cooperatively treating sludge and organic waste.
Background
Municipal sewage treatment has been fully popularized in China, but the municipal sludge treatment rate is still not high. The sludge treatment has various problems of high investment cost, high technical difficulty, insufficient guide and the like, wherein the treatment cost is one of the most critical problems.
The sludge treatment comprises the main means of land utilization, drying incineration, building material utilization and the like; wherein, the sludge is treated to realize land utilization or drying incineration, which is a mainstream technology in the world and in the domestic world. The sludge treatment process before treatment is divided into two main types, namely anaerobic stabilization and anaerobic stabilization. Whether anaerobic stabilization is adopted mainly depends on the state of the art and the advanced degree of the technology, developed countries such as the United states, germany and Japan, nordic and the like commonly adopt technical routes such as land utilization or incineration after anaerobic stabilization, and the method is also a technical direction of important development in the double-carbon era of China.
In addition, in China, new towns are developed in the future, and the new towns have the problems that single waste objects are small in quantity and difficult to be treated in a dispersing way, such as agricultural straws, livestock manure and industrial organic garbage.
In this regard, the prior art has been to combine the above-mentioned organic waste with municipal sludge after sorting and crushing, and to perform anaerobic digestion under electrically heated conditions in a manner similar to a dry anaerobic digestion reaction. However, the method has the advantages of lower gas production rate of unit fed organic matters, higher energy consumption, limited product outlet and lower overall efficiency.
How to treat sludge and organic waste with high efficiency and realize stabilization and recycling on the basis of low carbon and technical popularization is a difficult problem to be solved at present.
Disclosure of Invention
The invention provides a cooperative treatment system and a cooperative treatment method for sludge and organic waste, which aim to solve the defects of high investment cost, poor operation stability, unsmooth tail end outlet, high energy consumption and the like in the decentralized treatment of the sludge and the organic waste. On the premise of realizing the stabilization of sludge with high standard, the invention integrally realizes self-heating balance, and utilizes the generated biogas as the energy source of the system to realize self-heating balance of digestion and drying; the system and the method can improve the capacity of methane, obtain higher gas yield in shorter anaerobic reaction time, realize the efficient treatment of sludge and organic waste, and solve the difficult problem of treatment of multi-source sludge and organic waste; and the heat energy balance in the system can be realized, and the heat consumption of the system is reduced.
The present invention solves the above-described problems by the following technical means.
The invention provides a cooperative treatment system for sludge and organic waste, which comprises a cooperative anaerobic pretreatment unit, an anaerobic digestion unit and a drying treatment unit which are sequentially connected;
The cooperative anaerobic pretreatment unit comprises a cooperative anaerobic pretreatment tank and a mechanical circulation pretreatment device for liquefying raw material slurry; the collaborative anaerobic pre-reaction tank comprises a raw material inlet, wherein the raw material inlet is used for introducing sludge and organic waste into the collaborative anaerobic pre-reaction tank; the outlet of the cooperative anaerobic pre-reaction tank is connected with the inlet of the mechanical circulation pre-treatment device through a heat exchange pipeline, and the outlet of the mechanical circulation pre-treatment device is connected with the inlet of the cooperative anaerobic pre-reaction tank to form a circulation pre-treatment loop of raw materials; a first heat exchanger and a second heat exchanger are sequentially arranged on the heat exchange pipeline along the flow direction of the materials;
the anaerobic digestion unit comprises a first anaerobic digestion tank and a second anaerobic digestion tank; the first anaerobic digestion tank is connected with the cooperative anaerobic pre-reaction tank; the gas phase outlet of the first anaerobic digestion tank and the gas phase outlet of the second anaerobic digestion tank are connected with the fuel gas inlet of the steam boiler and are used for providing fuel for the steam boiler; the steam outlet of the steam boiler is respectively connected with the collaborative anaerobic pre-reaction tank and the drying treatment unit through a first steam pipeline and a second steam pipeline;
The drying treatment unit comprises sludge drying equipment, and a feed inlet of the sludge drying equipment is connected with a discharge outlet of the second anaerobic digestion tank; the hot fluid outlet of the sludge drying device is connected with the first heat exchanger through a first heat exchange medium pipeline, and the steam condensate outlet of the sludge drying device is connected with the second heat exchanger through a second heat exchange medium pipeline.
In the invention, the hot fluid is from tail gas obtained by heating sludge in the sludge drying equipment, and the tail gas contains a small amount of granular sludge and steam.
In the invention, the first heat exchange medium pipeline provides heat from the tail gas for the heat exchange pipeline.
In the invention, the steam condensate is obtained by heat exchange of the superheated steam of the second steam pipeline.
In the invention, the second heat exchange medium pipeline provides heat of the steam condensate water subjected to heat exchange for the heat exchange pipeline.
In the invention, the temperature of steam condensate water in the second heat exchange medium pipeline is higher than that of tail steam in the first heat exchange medium pipeline; the first heat exchange medium pipeline and the second heat exchange medium pipeline respectively provide progressively rising heat for materials in the heat exchange pipeline through the first heat exchanger and the second heat exchanger.
In some embodiments, the synergistic anaerobic pre-reaction tank further comprises an industrial water inlet and/or a complex agent inlet.
In the invention, the first anaerobic digestion tank is used for anaerobic digestion reaction, and the second anaerobic digestion tank is used for anaerobic digestion reaction and also used for providing buffering function.
In the invention, the anaerobic digestion unit can improve the yield of methane to the greatest extent; after the rheological property of the raw materials is improved through the cooperative anaerobic pretreatment unit, all the generated biogas can be collected and efficiently treated in the anaerobic digestion unit to the greatest extent.
In the invention, the first steam pipeline and the second steam pipeline respectively supply heat of superheated steam from the steam boiler to the cooperative anaerobic pre-reaction tank and the drying treatment unit.
In some embodiments, the drying treatment unit further comprises a sludge dewatering device and a dewatered sludge bin, and the second anaerobic digester is connected in sequence with the sludge dewatering device, the dewatered sludge bin, and the sludge drying apparatus.
In some embodiments, the sludge and organic waste co-treatment system further comprises a biogas storage and purification unit, wherein the inlet of the biogas storage and purification unit is respectively connected with the gas phase outlet of the first anaerobic digestion tank and the gas phase outlet of the second anaerobic digestion tank, and is used for storing and purifying biogas generated after anaerobic digestion; and a fuel gas outlet of the biogas storage and purification unit is connected with the steam boiler.
In a specific embodiment, a water outlet is arranged at the liquid phase outlet of the sludge dewatering device.
In a specific embodiment, the waste gas outlet of the biogas storage and purification unit is also connected with a residual gas combustion tower, and the residual gas combustion tower is provided with an exhaust port.
In the invention, the sludge drying equipment is generally arranged in a sludge drying workshop; those skilled in the art will appreciate that other sludge drying kits are also included in the sludge drying plant.
The invention also provides a cooperative treatment method of the sludge and the organic waste, which adopts the cooperative treatment system of the sludge and the organic waste and comprises the following steps:
s1, mixing raw materials with superheated steam in the first steam pipeline in the cooperative anaerobic pre-reaction tank, wherein the raw materials comprise sludge and organic wastes; starting the mechanical circulation pretreatment device to carry out circulation pretreatment to obtain a slurry-liquefied material;
s2, introducing the pulped materials into an anaerobic digestion unit, and sequentially carrying out secondary anaerobic digestion reaction in the first anaerobic digestion tank and the second anaerobic digestion tank to obtain methane and digestive juice;
s3, introducing the biogas into the steam boiler for combustion to obtain superheated steam, and introducing the superheated steam into the cooperative anaerobic pre-reaction tank and a heat medium inlet of the sludge drying device through the first steam pipeline and the second steam pipeline respectively;
S4, introducing the digestive juice into the sludge drying equipment, and heating and drying by using the superheated steam in the second steam pipeline to obtain dried sludge, tail steam and steam condensate water;
s5, enabling the tail gas to enter the first heat exchanger through the first heat exchange medium pipeline; the steam condensate water enters the second heat exchanger through the second heat exchange medium pipeline.
In the art, anaerobic digestion of sludge generally comprises anaerobic hydrolysis, acidification, methanation, etc., wherein anaerobic hydrolysis breaks the organic macromolecules to produce medium molecular weight organics, which is the rate limiting reaction affecting the overall anaerobic digestion reaction time.
In the invention, the serous material is ground by adopting a mechanical and thermal circulation mode, preferably by matching with a chemical method, which is equivalent to the fact that the crushing and partial hydrolysis of a part of agglomerated zoogloea and organic mass substances are finished in advance, thereby shortening the residence time of the subsequent anaerobic digestion reaction.
In the step S1 of the invention, the waste consisting of the sludge and the organic waste comprises water and solid suspended matters; specifically comprises the following components: inorganic minerals, organic matter, heavy metals, pathogens and pathogenic microorganisms, protozoa and metazoan, ova and adults, and the like.
In the invention, the addition amount of the organic waste is generally more than 10% of the total mass of the sludge so as to improve the organic matter content in the sludge.
In step S1 of the present invention, preferably, before introducing the raw material containing sludge and organic waste into the synergistic anaerobic pre-reaction tank, the bulk inorganic impurities in the raw material are removed; more preferably, the bulk inorganic impurities include one or more of wood, metal, ceramic, and glass.
In some embodiments, in step S1, the organic content of the feedstock is 60% or more.
In some embodiments, in step S1, the feedstock has a solids content (TS) of 5-15%.
In some embodiments, in step S1, the sludge comprises municipal sludge; the municipal sludge is conventional in the art, and refers to solid precipitate substances generated in the sewage treatment process of a sewage treatment plant, and has the main characteristic of dehydrated sludge with the water content reaching about 80%.
In some embodiments, in step S1, the organic waste comprises one or more of kitchen waste, industrial organic waste, agricultural organic waste, aquatic plant waste, and livestock manure.
In some embodiments, in step S1, the superheated steam directly heats the feedstock in a spray.
In some embodiments, in step S1, the cyclic pretreatment includes one or more of grinding treatment, microwave treatment, and ultrasonic treatment; the device is used for carrying out physical processing methods such as grinding, microwave or ultrasonic and the like on the materials, so that the serosity of the materials is realized, the viscosity of the materials is promoted to be reduced, the anaerobic digestion stirring energy consumption is controlled in a reasonable range, and the energy-saving operation is realized.
In the invention, through the cooperative anaerobic pretreatment of the sludge and the organic waste, the pH value or the pH value of the material is not required to be regulated by adding an alkaline agent during digestion.
In some embodiments, in step S1, the feedstock further comprises industrial water and/or a pharmaceutical agent for enhancing hydrolysis tempering; preferably, the agent comprises an oxidizing agent and/or a basic agent; more preferably, the agent comprises one or more of iron salt, hydrogen peroxide and aqueous ozone; by adding the auxiliary agent, specific organic wastes such as agricultural straws, river water plants and other high-fiber organic wastes can be purposefully solved, and the hydrolysis tempering is enhanced to improve the biogas productivity.
In some embodiments, in step S1, the superheated steam in the first steam line has a temperature of 160-200 ℃.
In the step S1 of the invention, the raw materials are subjected to tempering pretreatment and slurrying in the cooperative anaerobic pre-reaction tank.
In some embodiments, in step S1, the residence time of the feedstock in the synergistic anaerobic pre-reaction tank is from 12 to 24 hours.
In some embodiments, in step S1, the ratio of the feedstock subjected to the cyclic pretreatment is 10-100wt%, the percentage being the ratio of the mass of the feedstock subjected to the cyclic pretreatment to the total mass of the feedstock.
In the step S1, steam is added into the cooperative anaerobic pre-reaction tank, and a mechanical circulation pre-treatment device is started to perform circulation pre-treatment on the raw materials, so that tempering pre-treatment and slurry liquefaction of the raw materials are realized; after the whole co-processing system is started, tail steam and steam condensate water in the step S5 are used for providing heat for the circulating raw materials.
In the invention, mechanical and thermal means, preferably means including medicament and industrial water, are utilized to carry out quenching and tempering treatment on the fed mixed material to realize serosity of the material, and uniform, rheological property-good and high-reaction-efficiency liquefied slurry is provided for anaerobic digestion.
According to the material property and the system design working condition, the pretreatment system and the secondary anaerobic digestion can be operated in a high-temperature anaerobic mode or a medium-temperature anaerobic mode.
In some embodiments, in step S1, the temperature of the synergistic anaerobic pre-reaction tank is 40-90 ℃.
In a specific embodiment, when the secondary anaerobic digestion reaction is carried out at moderate temperatures, the temperature of the synergistic anaerobic pre-reaction tank is 42-60 ℃.
In a specific embodiment, when the secondary anaerobic digestion reaction is carried out at elevated temperature, the temperature of the synergistic anaerobic pre-reaction tank is from 58 to 90 ℃.
In the invention, after anaerobic digestion reaction, the volatile organic compounds undergo anaerobic hydrolysis, acidification and methanation reaction; wherein, the main products of macromolecular organic matters comprise methane and carbon dioxide, and the byproducts comprise organic matters with medium molecular weight and small molecules, such as humic acid, small molecular volatile acid and the like.
In some embodiments, in step S2, the temperature of the first anaerobic digester is in the range of 30-60 ℃.
In a specific embodiment, when the secondary anaerobic digestion reaction is carried out at moderate temperature, the temperature of the first anaerobic digestion tank is 32-38 ℃.
In a specific embodiment, when the secondary anaerobic digestion reaction is carried out at an elevated temperature, the temperature of the first anaerobic digestion tank is 52-58 ℃.
In some embodiments, in step S2, the temperature of the second anaerobic digester is 30-60 ℃.
In a specific embodiment, when the secondary anaerobic digestion reaction is carried out at moderate temperature, the temperature of the second anaerobic digestion tank is 32-38 ℃.
In a specific embodiment, when the secondary anaerobic digestion reaction is carried out at an elevated temperature, the temperature of the second anaerobic digestion tank is 52-58 ℃.
In some embodiments, in step S2, the temperature of the first anaerobic digester and the second anaerobic digester are the same.
In a specific embodiment, the slurried material is digested for 20 days or more when the temperature of the first anaerobic digester and the second anaerobic digester ranges from 32 to 38 ℃.
In a specific embodiment, the digestion time of the slurried material is 15 days or more when the temperature of the first anaerobic digester and the second anaerobic digester is in the range of 52-58 ℃.
In step S2 of the present invention, preferably, the volatile solid load of the sludge and organic waste co-treatment system is 2-3kg VS/(m) 3 D) a step of; in this case, the biogas production per organic matter is 0.4-0.6Nm 3 Each kg of volatile solids is fed. The volatile solid load refers to the amount of volatile solids added to the digester daily divided by the digester working volume.
In the present invention, the slurry is fed to an anaerobic digestion unit using a pump delivery method conventional in the art.
In some embodiments, in step S2, the solids content of the slurried material is no more than 12%, preferably 10-12%.
In some embodiments, in step S2, the pH of the first anaerobic digester is between 6.5 and 7.5.
In some embodiments, in step S2, the pH of the second anaerobic digester is between 6.5 and 7.5.
In some embodiments, in step S2, the energy consumption per mechanical agitation in the first anaerobic digester or the second anaerobic digester is from 4 to 8W/m 3 。
In some embodiments, in step S2, the temperature difference within the first anaerobic digester is no more than 3 ℃.
In some embodiments, in step S2, the temperature difference within the second anaerobic digester is no more than 5 ℃.
In some embodiments, in step S2, the biogas is purified and stored in a biogas storage and purification unit, and the generated residual gas enters a residual gas combustion tower.
In a specific embodiment, in step S2, the biogas may be a crude biogas as is common in the art, having a methane content of 55-95%.
In a specific embodiment, in step S2, after the purification treatment, the methane content in the biogas is 75% or more; the methane content in the biogas is improved by feeding the organic waste.
In a specific embodiment, in step S2, after the purification treatment, the content of hydrogen sulfide in the biogas is lower than 20mg/Nm 3 。
In the invention, the superheated steam supplies heat to a heat user through a first steam pipeline and a second steam pipeline respectively.
In some embodiments, in step S3, the superheated steam of the second steam line has a temperature of 160-200 ℃.
In the invention, the biogas is used for generating steam by the combustion of a boiler, so that the impurity content in the biogas needs to be controlled.
In some embodiments, in step S3, the biogas is passed from the biogas storage and purification unit to the steam boiler for combustion; after passing through the biogas storage and purification unit, the biogas is purified, so that the impurity contents of water, hydrogen sulfide, carbon dioxide and the like in the biogas are reduced, dehydration, desulfurization and decarbonization are realized, the methane content in the purified product is ensured, and the atmospheric pollutants of the boiler meet the emission requirement.
In some embodiments, in step S3, when the feeding organic matters exceed more than 60%, the system design of the biogas storage and purification unit can increase the natural gas purification production or the biogas power generation self-use to balance the surplus energy.
In the invention, after the digestion liquid is dehydrated and dried, no more than 50% of materials undergo further decomposition reaction.
In the invention, the heat for heating and drying is provided by the superheated steam of the second steam pipeline, and the superheated steam of the second steam pipeline forms steam condensate water after heat exchange; the dewatered sludge is subjected to heat drying treatment to generate tail gas containing a small amount of granular sludge and steam.
In the present invention, in step S4, the sludge drying apparatus may include a single-stage dryer, and the heating drying may be performed in the single-stage dryer.
In the present invention, in step S4, the sludge drying may adopt an indirect heat exchange manner, and the steam provides heat for the sludge through a jacket or a heat exchanger.
In some embodiments, in step S4, the temperature of the tail gas is 92-98 ℃.
In some embodiments, in step S4, the tail gas is in a negative pressure state of-4 to-6 kPa.
In some embodiments, in step S4, the temperature of the steam condensate is 100-140 ℃.
In some embodiments, in step S4, the digestion solution is dehydrated to obtain digested sludge before the heating and drying; preferably, the digested sludge has a water content of 80% or less, with the addition of a Polyacrylamide (PAM) conditioner. After the dehydration treatment, the materials entering the drying treatment unit are further stabilized, reduced and reach the dry biogas residue products of the hygiene standard, and can be used as the materials for land utilization.
In the invention, because the sludge and the organic waste contain toxic pollutants such as PCB, PCDD, PFAS, heavy metals, pathogens, disease-related organisms and the like, the sludge and the organic waste are directly discharged or land is utilized to cause diseases or epidemic outbreaks easily, and the food chain is polluted. National standard CJ/T510-2017 'sludge treatment stability Standard of urban wastewater treatment plant' prescribes that the sludge stability Standard is that the treatment product meets the sanitary requirements of difficult rotting odor, pathogen control and the like; the united states specifies the requirements for a class a sludge product by EPA503 clause.
In some embodiments, in step S4, the water content of the dried sludge is less than 25%, which meets the above-mentioned requirements of sanitation in national standards and international industries; and the solid content of the dried sludge is 75% or more, so that the dried sludge has stability and meets the control index of fecal coliform in the sludge stability standard.
In the invention, the tail gas and the steam condensate serve as recoverable heat energy for conditioning of the cyclic pretreatment.
In the invention, the sludge and organic waste cooperative treatment system balances redundant energy and can realize the form of a residual gas combustion tower and the discharge of condensate water by utilizing residual heat.
In the invention, the waste heat of the superheated steam of the second steam pipeline of the sludge drying equipment can be recycled by recovering the tail steam and the steam condensate water and is introduced into the waste heat, wherein the waste heat accounts for 50-60% of the total heat energy input by the superheated steam of the second steam pipeline; the available net heat energy of the cooperative anaerobic pre-reaction tank accounts for 25-35% of the total heat energy input by the superheated steam of the second steam pipeline in the heating and drying process, so that the heat energy balance of the whole system can be realized, and the system can be designed for realizing automatic operation by self-learning feedback control.
In the invention, the treatment process of the dried sludge is conventional disinfection and sterilization in the field, and finally a mixture of organic solid and inorganic solid and water are formed.
On the basis of conforming to the common knowledge in the field, the above preferred conditions can be arbitrarily combined to obtain the preferred examples of the invention.
The reagents and materials used in the present invention are commercially available.
The invention has the positive progress effects that:
(1) the invention can realize volume reduction and weight reduction by removing the water in the sludge, thereby achieving the reduction, and finally the obtained dried sludge meets the sanitary requirements of national standards and international industries, realizes the stabilization and simultaneously realizes the harmless and recycling treatment targets.
(2) The system and the method of the invention utilize machinery and heat to carry out quenching and tempering on the fed mixed materials to realize the serosity of the materials, provide uniform, rheological property good and high-efficiency liquefied slurry for anaerobic digestion, further improve biogas productivity, reduce stirring energy consumption, avoid scum generation on the upper layer of an anaerobic digestion tank, and obtain higher gas yield in shorter anaerobic reaction time.
(3) The sludge is subjected to anaerobic treatment and then dried independently, so that the balance of heat energy is difficult to realize, and the anaerobic digestion of the organic waste is easy to acidify and the long-term stable operation is difficult to realize; the invention realizes stable production and self-sufficiency of heat energy by utilizing a low-carbon cooperative treatment mode of sludge and organic waste, has a rich biogas productivity under the condition of sufficient and stable supply of organic waste, and can realize further energy utilization and high-efficiency treatment and heat energy balance by utilizing a power generation mode of producing natural gas or biogas through biogas purification.
(4) In the system and the method, the difficult problem of multi-source sludge or organic waste treatment can be effectively and intensively solved by the heat drying treatment technology performed after the cooperative anaerobic treatment of the sludge and the organic matters; the treated hygiene standard product can be used as raw material for land utilization or blending burning treatment and building material utilization, and compared with single treatment, the comprehensive treatment has greatly reduced investment and cost.
Drawings
Fig. 1 is a schematic diagram of the co-treatment system for sludge and organic waste in example 1.
Reference numerals illustrate:
synergistic anaerobic pretreatment unit 1
Synergistic anaerobic pre-reaction tank 101
Raw material inlet 1011
Mechanical circulation pretreatment device 102
First heat exchanger 103
Second heat exchanger 104
Anaerobic digestion unit 2
First anaerobic digester 201
Second anaerobic digester 202
Drying treatment unit 3
Sludge drying equipment 301
Sludge dewatering device 302
Dewatered sludge silo 303
Steam boiler 401
Biogas storage and purification unit 501
Residual gas combustion tower 601
Heat exchange pipeline 1000
First steam pipe 1001
Second steam pipe 1002
First heat exchange medium pipeline 1003
A second heat exchange medium line 1004.
The technical solutions 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.
Detailed Description
The invention is further illustrated by means of the following examples, which are not intended to limit the scope of the invention. The experimental methods, in which specific conditions are not noted in the following examples, were selected according to conventional methods and conditions, or according to the commercial specifications.
In all embodiments 1-4 of the present application, a co-processing system for sludge and organic waste as shown in fig. 1 is adopted, and fig. 1 is a schematic structural diagram of the processing system.
The cooperative treatment system for the sludge and the organic waste comprises a cooperative anaerobic pretreatment unit 1, an anaerobic digestion unit 2 and a drying treatment unit 3 which are sequentially connected;
the cooperative anaerobic pretreatment unit 1 comprises a cooperative anaerobic pretreatment tank 101 and a mechanical circulation pretreatment device 102 for liquefying raw material slurry; the cooperative anaerobic pre-reaction tank 101 includes a raw material inlet 1011, the raw material inlet 1011 for introducing sludge and organic waste into the cooperative anaerobic pre-reaction tank 101; the outlet of the cooperative anaerobic pre-reaction tank 101 is connected with the inlet of the mechanical circulation pre-treatment device 102 through a heat exchange pipeline 1000, and the outlet of the mechanical circulation pre-treatment device 102 is connected with the inlet of the cooperative anaerobic pre-reaction tank 101 to form a circulation pre-treatment loop of raw materials; a first heat exchanger 103 and a second heat exchanger 104 are sequentially arranged on the heat exchange pipeline 1000 along the flow direction of the materials;
the anaerobic digestion unit 2 includes a first anaerobic digestion tank 201 and a second anaerobic digestion tank 202; the first anaerobic digestion tank 201 is connected with the cooperative anaerobic pre-reaction tank 101; the gas phase outlet of the first anaerobic digestion tank 201 and the gas phase outlet of the second anaerobic digestion tank 202 are connected with the fuel gas inlet of the steam boiler 401, and are used for providing fuel for the steam boiler 401; the steam outlet of the steam boiler 401 is respectively connected with the cooperative anaerobic pre-reaction tank 101 and the drying treatment unit 3 through a first steam pipeline 1001 and a second steam pipeline 1002 for providing heat;
The drying treatment unit 3 comprises a sludge drying device 301, and a feed inlet of the sludge drying device 301 is connected with a discharge outlet of the second anaerobic digestion tank 202; the hot fluid outlet of the sludge drying device 301 is connected with the first heat exchanger 103 through a first heat exchange medium pipeline 1003, and the steam condensate outlet of the sludge drying device 301 is connected with the second heat exchanger 104 through a second heat exchange medium pipeline 1004 for supplying heat to the materials in the heat exchange pipeline 1000.
Wherein the co-anaerobic pre-reactor 101 further comprises an industrial water inlet and/or a complex agent inlet.
The drying treatment unit 3 further comprises a sludge dewatering device 302 and a dewatered sludge storage bin 303, and the second anaerobic digestion tank 202 is sequentially connected with the sludge dewatering device 302, the dewatered sludge storage bin 303 and the sludge drying device 301.
The sludge and organic waste cooperative treatment system further comprises a biogas storage and purification unit 501, wherein the inlet of the biogas storage and purification unit 501 is respectively connected with the gas phase outlet of the first anaerobic digestion tank 201 and the gas phase outlet of the second anaerobic digestion tank 202 and is used for storing and purifying biogas generated after anaerobic digestion; the fuel gas outlet of the biogas storage and purification unit 501 is connected to the steam boiler 401.
Wherein, a water outlet is arranged at the liquid phase outlet of the sludge dewatering device 302.
The waste gas outlet of the biogas storage and purification unit 501 is also connected with a waste gas combustion tower 601, and the waste gas combustion tower 601 is provided with an exhaust port.
Example 1
The embodiment is a cooperative treatment method for sludge and organic waste, which adopts the cooperative treatment system for sludge and organic waste, and comprises the following steps:
s1, municipal sludge, kitchen waste or organic industrial waste, agricultural waste or livestock manure are mixed to be used as a material for preparing a synergistic anaerobic system after inorganic impurities are removed, and at least more than 1 organic waste except the municipal sludge is used as a raw material; the pretreatment method of this example includes mechanical milling and thermal conditioning: in a cooperative anaerobic pre-reaction tank 101, mixing raw materials with superheated steam in a first steam pipeline 1001, wherein the raw materials comprise sludge and organic waste, and starting a mechanical circulation pre-treatment device 102 to perform mechanical grinding and circulation pre-treatment to obtain a slurry-liquefied material;
s2, introducing the pulped materials into an anaerobic digestion unit 2, and sequentially performing secondary anaerobic digestion reaction in a first anaerobic digestion tank 201 and a second anaerobic digestion tank 202 to obtain biogas and digestive juice;
S3, introducing methane into the steam boiler 401 for combustion to obtain superheated steam, and introducing the superheated steam into the heat medium inlets of the cooperative anaerobic pre-reaction tank 101 and the sludge drying equipment 301 through the first steam pipeline 1001 and the second steam pipeline 1002 respectively;
s4, introducing the digestive juice into the sludge drying equipment 301, and performing heating drying through superheated steam in the second steam pipeline 1002 to obtain dried sludge, tail steam and steam condensate water;
s5, enabling tail gas to enter the first heat exchanger 103 through the first heat exchange medium pipeline 1003; the steam condensate enters the second heat exchanger 104 through the second heat exchange medium pipeline 1004 to supply heat to the materials in the heat exchange pipeline 1000.
In the step S1, controlling the organic matter content of the raw materials to be more than or equal to 60%, controlling the solid content of the raw materials to be 5-15%, heating the raw materials by steam in a starting stage in a jet mode, and performing cyclic pretreatment including grinding treatment; the temperature of the superheated steam in the first steam line 1001 is 180 ℃; in the cooperative anaerobic pre-reaction tank 101, the residence time of the raw materials is 12 hours; the ratio of the material subjected to the cyclic pretreatment is 25wt%, and the percentage is the ratio of the mass of the material subjected to the cyclic pretreatment to the total mass of the material.
In step S1, the temperature range in the cooperative anaerobic pre-reaction tank 101 is 45 ℃.
In the embodiment, the pretreatment tempering medium-temperature anaerobic digestion mode is adopted for operation, the temperature range of the first anaerobic digestion tank 201 and the second anaerobic digestion tank 202 is 35+/-3 ℃, and the digestion time of the pulp liquefied material is 20 days;
in the step S2, the volatile solid load of the sludge and organic waste cooperative treatment system is 2-3kg VS/(m) 3 D) a step of; the unit organic biogas yield is 0.4-0.6Nm 3 Feeding each kg of volatile solid; the solid content of the pulped materials is not more than 10-12%; the pH value of the first anaerobic digestion tank 201 and the second anaerobic digestion tank 202 is controlled to be 6.5-7.2; the energy consumption per mechanical stirring in the first anaerobic digestion tank 201 or the second anaerobic digestion tank 202 is 4-8W/m 3 The method comprises the steps of carrying out a first treatment on the surface of the The temperature difference in the first anaerobic digestion tank 201 and the temperature difference in the second anaerobic digestion tank 202 are not more than 3 ℃; after being purified, the biogas is stored in a biogas storage and purification unit 501, and the generated residual gas enters a residual gas combustion tower 601; the methane is common crude methane, and the methane content is 55-95%; after purification treatments such as dehydration, desulfurization, decarbonization and the like, the content of methane in the biogas is 75 percent or more, and the content of hydrogen sulfide in the biogas is lower than 20mg/Nm 3 。
In step S3, the temperature of superheated steam generated by the boiler is 180 ℃; the biogas is introduced into the steam boiler 401 from the biogas storage and purification unit 501 for combustion; after passing through the biogas storage and purification unit 501, the biogas realizes dehydration, desulfurization and decarbonization; when the feeding organic matters exceed more than 60%, the system design of the biogas storage and purification unit 501 can increase the natural gas purification production or the biogas power generation self-use to balance the surplus energy.
In step S4, the sludge drying apparatus 301 may include a single-stage dryer, and the heating drying may be performed in the single-stage dryer; the temperature of the tail gas is 92-98 ℃ and is in a negative pressure state of-4 to-6 kPa; the temperature of the steam condensate water is 100-140 ℃; dehydrating the digestive juice before heating and drying to obtain digested sludge; the water content of the dehydrated digested sludge is 80% or less on the premise of adding a PAM conditioner.
If the mode of mesophilic anaerobic digestion is adjusted to be operated in a thermophilic anaerobic digestion mode, when the temperature range of the first anaerobic digestion tank 201 and the second anaerobic digestion tank 202 is 55-58 ℃, the temperature range in the cooperative anaerobic pre-reaction tank 101 is 65 ℃, and the digestion time of the slurry-liquefied material is 15 days; the effect of the subsequent processing is the same as in the present embodiment.
Example 2
The embodiment is a cooperative treatment method of sludge and organic waste; unlike example 1, in step S1 of this example, during pretreatment,based on mechanical grinding and thermal conditioning, ferric salt is used as a composite medicament and raw material MixingThe procedure used to control the anaerobic reaction to produce hydrogen sulfide was the same as in example 1.
Example 3
The embodiment is a cooperative treatment method of sludge and organic waste; unlike example 1, in step S1 of this example, during pretreatment,taking hydrogen peroxide or ozone water solution as a base of mechanical grinding and thermal conditioning Composite medicament and raw materials are mixedThe method is used for conditioning the raw materials and pertinently solving specific organic matters difficult to hydrolyze in the feed, and other steps are the same as those of the example 1.
Example 4
The embodiment is a cooperative treatment method of sludge and organic waste; unlike example 1, in step S1 of this example, microwave or ultrasonic equipment is used instead of the mechanical crushing and grinding method of example 1, i.e.The cyclic pretreatment is realized by adopting a microwave or ultrasonic crushing and heating power conditioning modeOther steps and examples1 are all the same.
Effect examples 1 to 4
The method for cooperatively treating the sludge and the organic waste in the embodiments 1-4 is adopted, wherein the organic matter content in the raw materials is more than or equal to 60%, the solid content in the raw materials is less than or equal to 15%, the equipment size under the working condition a, b, c, d is respectively used, the value of the organic matter content under the working condition is 60%, the solid content in the raw materials is 15%, the average treatment capacity of the system on the raw materials under different equipment sizes is calculated, and the biogas yield under each working condition is estimated, and the results are shown in the table 1:
TABLE 1
Table 1 shows the results of sludge and waste treatment using any of the methods of examples 1-4, using different conditions, which can cover most of the application scenarios.
With the system and method of the present invention, biogas yields can be at 960Nm when the average throughput is 4tTS/d, 8tTS/d, 12tTS/d, 16tTS/d, respectively (where tTS/d refers to tonnage per day of solid waste processed) 3 、1920Nm 3 、2880Nm 3 、3840Nm 3 The above. In addition, in the step S4, the water content of the formed dried sludge is less than 25%, the solid content is 75% or more, and the requirements of the sanitation of national standards and international industries are met.
In addition, the drying tail steam and the steam condensate water are recovered, and waste heat after heat exchange of the superheated steam of the second steam pipeline of the sludge drying equipment is introduced, wherein the waste heat accounts for 50-60% of total heat energy input by the superheated steam of the second steam pipeline; the available net heat energy of the cooperative anaerobic pre-reaction tank accounts for 25-35% of the total heat energy input by the superheated steam of the second steam pipeline in the heating and drying process, so that the heat energy balance of the whole system can be realized, and the system can be designed for self-learning feedback control to realize automatic operation.
Comparative example 1
The treatment object of this comparative example was sludge and kitchen waste, and its composition and implementation In the same manner as in example 1, the treatment object is simply mixed and subjected to anaerobic digestion by adopting a dry anaerobic digestion reaction (solid content of raw material is 20% -40%) which is conventional in the art, the residence time in the medium-temperature anaerobic digestion anaerobic tank is generally designed to be 25-35 days, and the gas production rate is about 0.3Nm after the actual production exceeds 35 days 3 /kgVS。
Comparative example 2
The treatment object of the comparative example was municipal sludge, and the treatment object was simply mixed and subjected to anaerobic digestion by wet medium-temperature anaerobic digestion (raw material solid content: 10% to 15%) conventional in the art to achieve a gas production rate of 0.3Nm 3 The residence time required for/kgVS takes 22 days.
In contrast, after the sludge is liquefied, the organic gas production rate can reach 0.4-0.6Nm when the retention time of the sludge is 22 days after the sludge is subjected to the medium-temperature anaerobic digestion 3 /kgVS, or, to 0.3Nm 3 The gas production rate per kgVS and residence time were only about 15 days.
The above embodiments are merely illustrative embodiments of the present invention, but the scope of the present invention is not limited thereto, and any changes, substitutions or combinations thereof, which are within the technical scope of the present invention, are intended to be included in the scope of the present invention. Therefore, the protection scope of the present invention should be subject to the protection scope of the claims.
Claims (10)
1. The cooperative treatment system for the sludge and the organic waste is characterized by comprising a cooperative anaerobic pretreatment unit, an anaerobic digestion unit and a drying treatment unit which are sequentially connected;
the cooperative anaerobic pretreatment unit comprises a cooperative anaerobic pretreatment tank and a mechanical circulation pretreatment device for liquefying raw material slurry; the collaborative anaerobic pre-reaction tank comprises a raw material inlet, wherein the raw material inlet is used for introducing sludge and organic waste into the collaborative anaerobic pre-reaction tank; the outlet of the cooperative anaerobic pre-reaction tank is connected with the inlet of the mechanical circulation pre-treatment device through a heat exchange pipeline, and the outlet of the mechanical circulation pre-treatment device is connected with the inlet of the cooperative anaerobic pre-reaction tank to form a circulation pre-treatment loop of raw materials; a first heat exchanger and a second heat exchanger are sequentially arranged on the heat exchange pipeline along the flow direction of the materials;
the anaerobic digestion unit comprises a first anaerobic digestion tank and a second anaerobic digestion tank; the first anaerobic digestion tank is connected with the cooperative anaerobic pre-reaction tank; the gas phase outlet of the first anaerobic digestion tank and the gas phase outlet of the second anaerobic digestion tank are connected with the fuel gas inlet of the steam boiler and are used for providing fuel for the steam boiler; the steam outlet of the steam boiler is respectively connected with the collaborative anaerobic pre-reaction tank and the drying treatment unit through a first steam pipeline and a second steam pipeline;
The drying treatment unit comprises sludge drying equipment, and a feed inlet of the sludge drying equipment is connected with a discharge outlet of the second anaerobic digestion tank; the hot fluid outlet of the sludge drying device is connected with the first heat exchanger through a first heat exchange medium pipeline, and the steam condensate outlet of the sludge drying device is connected with the second heat exchanger through a second heat exchange medium pipeline.
2. The co-processing system of sludge and organic waste of claim 1, wherein the co-anaerobic pre-reactor further comprises an industrial water inlet and/or a complex chemical inlet;
and/or the drying treatment unit further comprises a sludge dewatering device and a dewatered sludge bin, and the second anaerobic digestion tank is sequentially connected with the sludge dewatering device, the dewatered sludge bin and the sludge drying equipment;
and/or the sludge and organic waste cooperative treatment system further comprises a biogas storage and purification unit, wherein the inlet of the biogas storage and purification unit is respectively connected with the gas phase outlet of the first anaerobic digestion tank and the gas phase outlet of the second anaerobic digestion tank and is used for storing and purifying biogas generated after anaerobic digestion; and a fuel gas outlet of the biogas storage and purification unit is connected with the steam boiler.
3. The co-processing system for sludge and organic waste according to claim 2, wherein a water outlet is provided at a liquid phase outlet of the sludge dewatering device;
and/or the waste gas outlet of the biogas storage and purification unit is also connected with a residual gas combustion tower, and the residual gas combustion tower is provided with an exhaust port.
4. A method for the co-treatment of sludge and organic waste, characterized in that it employs a sludge and organic waste co-treatment system as claimed in any one of claims 1 to 3, and comprises the steps of:
s1, mixing raw materials with superheated steam in the first steam pipeline in the cooperative anaerobic pre-reaction tank, wherein the raw materials comprise sludge and organic wastes; starting the mechanical circulation pretreatment device to carry out circulation pretreatment to obtain a slurry-liquefied material;
s2, introducing the pulped materials into an anaerobic digestion unit, and sequentially carrying out secondary anaerobic digestion reaction in the first anaerobic digestion tank and the second anaerobic digestion tank to obtain methane and digestive juice;
s3, introducing the biogas into the steam boiler for combustion to obtain superheated steam, and introducing the superheated steam into the cooperative anaerobic pre-reaction tank and a heat medium inlet of the sludge drying device through the first steam pipeline and the second steam pipeline respectively;
S4, introducing the digestive juice into the sludge drying equipment, and heating and drying by using the superheated steam in the second steam pipeline to obtain dried sludge, tail steam and steam condensate water;
s5, enabling the tail gas to enter the first heat exchanger through the first heat exchange medium pipeline; the steam condensate water enters the second heat exchanger through the second heat exchange medium pipeline.
5. The method according to claim 4, wherein in the step S1, the superheated steam in the first steam pipe has a temperature of 160-200 ℃;
and/or, in the step S1, the temperature of the cooperative anaerobic pre-reaction tank is 40-90 ℃; preferably, the temperature of the synergistic anaerobic pre-reaction tank is 42-60 ℃; preferably, the temperature of the synergistic anaerobic pre-reaction tank is 58-90 ℃;
and/or the temperature of the cooperative anaerobic pre-reaction tank is greater than the temperature of the first anaerobic digestion tank; preferably, the temperature of the cooperative anaerobic pre-reaction tank is 3 ℃ greater than the temperature of the first anaerobic digestion tank;
and/or, in step S2, the temperature of the first anaerobic digestion tank is 30-60 ℃, preferably, the temperature of the first anaerobic digestion tank is 32-38 ℃; preferably, the temperature of the first anaerobic digestion tank is 52-58 ℃;
And/or, in step S2, the temperature of the second anaerobic digestion tank is 30-60 ℃, preferably, the temperature of the second anaerobic digestion tank is 32-38 ℃; preferably, the temperature of the second anaerobic digestion tank is 52-58 ℃;
and/or, in step S2, the temperatures of the first anaerobic digestion tank and the second anaerobic digestion tank are the same;
and/or, in step S3, the temperature of the superheated steam in the second steam pipeline is 160-200 ℃;
and/or, in the step S4, the temperature of the heating and drying is less than or equal to 110 ℃;
and/or, in the step S4, the heating and drying mode is indirect heat exchange;
and/or, in the step S4, the temperature of the tail gas is 92-98 ℃;
and/or, in the step S4, the temperature of the steam condensate water is 100-140 ℃.
6. The method according to claim 5, wherein when the temperature ranges of the first anaerobic digestion tank and the second anaerobic digestion tank are 52 to 58 ℃, the digestion time of the slurried material is 15 days or more;
or, when the temperature of the first anaerobic digestion tank and the second anaerobic digestion tank is in the range of 32-38 ℃, the digestion time of the serous material is 20 days or more.
7. The method for co-processing sludge and organic waste as claimed in claim 4, wherein in step S1, the organic matter content of said raw material is 60% or more;
and/or the solid content of the raw materials is 5-15%;
and/or, the sludge comprises municipal sludge;
and/or the organic waste comprises one or more of kitchen waste, industrial organic waste, agricultural organic waste, aquatic plants and livestock and poultry manure;
and/or the cyclic pretreatment includes one or more of grinding treatment, microwave treatment, and ultrasonic treatment.
8. The method according to claim 4, wherein in step S1, the raw materials further include industrial water and/or chemicals; preferably, the agent comprises an oxidizing agent and/or a basic agent; more preferably, the agent comprises one or more of iron salt, hydrogen peroxide and aqueous ozone;
and/or, in the synergistic anaerobic pre-reaction tank, the residence time of the raw materials is 12-24h;
and/or the ratio of the material subjected to the cyclic pretreatment is 10-100wt%, and the percentage is the ratio of the mass of the material subjected to the cyclic pretreatment to the total mass of the material.
9. The method according to claim 4, wherein in step S2, the solid content of the slurried material is not more than 12%, preferably 10-12%;
and/or in the step S2, the pH value of the first anaerobic digestion tank is 6.5-7.5;
and/or in the step S2, the pH value of the second anaerobic digestion tank is 6.5-7.5;
and/or, in step S2, the temperature difference in the first anaerobic digestion tank is not more than 3 ℃;
and/or, in step S2, the temperature difference in the second anaerobic digestion tank is not more than 5 ℃;
and/or, in the step S2, the biogas is stored after being purified in a biogas storage and purification unit, and the generated residual gas enters a residual gas combustion tower;
and/or, in the step S3, the biogas is introduced into the steam boiler from the biogas storage and purification unit for combustion;
and/or, in the step S4, before the heating and drying, dehydrating the digestive juice to obtain digested sludge; preferably, the digested sludge has a water content of 80% or less;
and/or, in the step S4, the water content of the dried sludge is less than 25%, and the solid content is 75% or more.
10. The method according to claim 9, wherein in step S2, the methane content in the biogas after the purification treatment is 75% or more;
And/or, in the step S2, after the purification treatment, the content of hydrogen sulfide in the biogas is lower than 20mg/Nm 3 。
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