CN113998856A - Excrement plug-flow anaerobic reaction system - Google Patents
Excrement plug-flow anaerobic reaction system Download PDFInfo
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- CN113998856A CN113998856A CN202111341537.0A CN202111341537A CN113998856A CN 113998856 A CN113998856 A CN 113998856A CN 202111341537 A CN202111341537 A CN 202111341537A CN 113998856 A CN113998856 A CN 113998856A
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- 238000006243 chemical reaction Methods 0.000 title claims abstract description 126
- 239000004576 sand Substances 0.000 claims abstract description 55
- 239000002002 slurry Substances 0.000 claims abstract description 32
- 239000010865 sewage Substances 0.000 claims abstract description 29
- 230000002550 fecal effect Effects 0.000 claims abstract description 22
- 230000009615 deamination Effects 0.000 claims abstract description 21
- 238000006481 deamination reaction Methods 0.000 claims abstract description 21
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 17
- 230000023556 desulfurization Effects 0.000 claims abstract description 17
- 239000002994 raw material Substances 0.000 claims abstract description 12
- 239000011550 stock solution Substances 0.000 claims abstract description 4
- 238000010992 reflux Methods 0.000 claims description 26
- 238000003756 stirring Methods 0.000 claims description 23
- 230000007062 hydrolysis Effects 0.000 claims description 17
- 238000006460 hydrolysis reaction Methods 0.000 claims description 17
- 238000007599 discharging Methods 0.000 claims description 13
- 238000010438 heat treatment Methods 0.000 claims description 11
- 238000005273 aeration Methods 0.000 claims description 9
- 238000005276 aerator Methods 0.000 claims description 3
- 238000007664 blowing Methods 0.000 claims description 3
- 239000011152 fibreglass Substances 0.000 claims description 3
- 238000004140 cleaning Methods 0.000 abstract description 3
- 238000012423 maintenance Methods 0.000 abstract description 3
- 239000007789 gas Substances 0.000 description 21
- 239000007788 liquid Substances 0.000 description 11
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 6
- 238000005265 energy consumption Methods 0.000 description 6
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 6
- 230000015556 catabolic process Effects 0.000 description 5
- 238000006731 degradation reaction Methods 0.000 description 5
- 210000003608 fece Anatomy 0.000 description 5
- 239000010871 livestock manure Substances 0.000 description 5
- 239000002245 particle Substances 0.000 description 4
- 230000036632 reaction speed Effects 0.000 description 4
- 239000000126 substance Substances 0.000 description 4
- 241000894006 Bacteria Species 0.000 description 3
- 229910021529 ammonia Inorganic materials 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 238000000855 fermentation Methods 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 2
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 2
- 230000007547 defect Effects 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 230000002349 favourable effect Effects 0.000 description 2
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 2
- 230000014759 maintenance of location Effects 0.000 description 2
- 239000002918 waste heat Substances 0.000 description 2
- 239000002028 Biomass Substances 0.000 description 1
- 102000004190 Enzymes Human genes 0.000 description 1
- 108090000790 Enzymes Proteins 0.000 description 1
- 241000287828 Gallus gallus Species 0.000 description 1
- 229920005830 Polyurethane Foam Polymers 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 239000012295 chemical reaction liquid Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000012851 eutrophication Methods 0.000 description 1
- 150000004676 glycans Chemical class 0.000 description 1
- 230000003301 hydrolyzing effect Effects 0.000 description 1
- 238000009413 insulation Methods 0.000 description 1
- 150000002632 lipids Chemical class 0.000 description 1
- 244000144972 livestock Species 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 150000002772 monosaccharides Chemical class 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 229920001184 polypeptide Polymers 0.000 description 1
- 229920001282 polysaccharide Polymers 0.000 description 1
- 239000005017 polysaccharide Substances 0.000 description 1
- 239000011496 polyurethane foam Substances 0.000 description 1
- 244000144977 poultry Species 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 102000004196 processed proteins & peptides Human genes 0.000 description 1
- 108090000765 processed proteins & peptides Proteins 0.000 description 1
- 230000001737 promoting effect Effects 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 239000002689 soil Substances 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 241001148471 unidentified anaerobic bacterium Species 0.000 description 1
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F11/00—Treatment of sludge; Devices therefor
- C02F11/02—Biological treatment
- C02F11/04—Anaerobic treatment; Production of methane by such processes
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/20—Nature of the water, waste water, sewage or sludge to be treated from animal husbandry
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/10—Temperature conditions for biological treatment
- C02F2301/106—Thermophilic treatment
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Life Sciences & Earth Sciences (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Health & Medical Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Molecular Biology (AREA)
- Hydrology & Water Resources (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Organic Chemistry (AREA)
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
Abstract
The invention relates to the technical field of fecal sewage treatment, in particular to a fecal sewage plug flow anaerobic reaction system, which comprises: the S-shaped reactor is provided with an S-shaped closed reaction channel and is provided with an inlet end and an outlet end; the sand removing device is arranged at the inlet end of the S-shaped reactor; and the heat exchange pipeline penetrates through the S-shaped reactor, the first end of the heat exchange pipeline is connected to the excrement collecting pool, the second end of the heat exchange pipeline is connected to the sand removing device, and the excrement stock solution and the biogas slurry in the S-shaped reactor are conducted into the sand removing device to remove sand after heat exchange. The anaerobic reaction system is designed in an S shape, and is designed in an integrated way from feeding to biogas generation, biogas desulfurization and deamination and biogas slurry deamination treatment, so that the occupied area and the building area are reduced, and heat supply is centralized; through the sand removal device, the sand grains in the excrement raw material are removed, the sand grains brought into the reactor are greatly reduced, the cleaning time interval is increased, the maintenance times are reduced, and the stability of system operation is kept.
Description
Technical Field
The invention relates to the technical field of fecal sewage treatment, in particular to a fecal sewage plug flow anaerobic reaction system.
Background
At present, the treatment technology and the comprehensive utilization mode of chicken manure aim at reduction, harmlessness and resource, livestock and poultry manure is used as a raw material in a manure energy utilization mode, biogas is generated in an anaerobic fermentation mode, and a pretreatment device, a gas stirring device, a temperature gradient control device, a strain reflux device, a sand removal component and a waste heat exchange device are used as auxiliary materials, so that the yield of the biogas is maximized.
The anaerobic reaction device is developed from 20 th century and 80 th century in China, technology is not available from Europe and America, but the defects of the anaerobic reactor are still many at present, such as low feeding concentration, insufficient retention time, insufficient strain quantity, frequent sand grain precipitation, insufficient heat of the anaerobic fermentation device, insufficient stirring or excessive stirring, and the like, so that the biomass biogas industry cannot be rapidly developed.
Disclosure of Invention
Aiming at the defects and shortcomings of the plug-flow anaerobic reactor in the prior art, the invention aims to improve the reaction speed and the degradation efficiency, reduce the floor area of equipment and reduce the reaction energy consumption.
The invention aims to provide a fecal sewage plug flow anaerobic reaction system, which comprises:
the S-shaped reactor is provided with an S-shaped closed reaction channel and is provided with an inlet end and an outlet end;
the sand removing device is arranged at the inlet end of the S-shaped reactor;
the heat exchange pipeline penetrates through the S-shaped reactor, a first end of the heat exchange pipeline is connected to the excrement collecting pool, a second end of the heat exchange pipeline is connected to the sand removing device, and excrement stock solution and biogas slurry in the S-shaped reactor are conducted into the sand removing device to remove sand after heat exchange;
the system comprises an S-shaped reactor, a hydrolysis zone, an anaerobic reaction front-stage zone, an anaerobic reaction rear-stage zone, an anoxic zone and an aerobic aeration zone, wherein the hydrolysis zone, the anaerobic reaction front-stage zone, the anaerobic reaction rear-stage zone, the anoxic zone and the aerobic aeration zone are sequentially arranged in the S-shaped reactor according to the flowing direction of biogas slurry, the hydrolysis zone and the anaerobic reaction front-stage zone are separated by a retaining wall, heating pipes are arranged in the anaerobic reaction front-stage zone and the anaerobic reaction rear-stage zone, the density of the heating pipes in the anaerobic reaction front-stage zone is greater than that of the heating pipes in the anaerobic reaction rear-stage zone, the S-shaped reactor is provided with an opening at the anoxic zone, and an aerator is arranged in the aerobic aeration zone;
and a backflow part is arranged between the tail end of the anaerobic reaction rear section area and the front end of the anaerobic reaction front section area and is used for refluxing biogas slurry at the tail end of the anaerobic reaction rear section area to the front end of the anaerobic reaction front section area.
Preferably, gas stirring parts are arranged in the anaerobic reaction front-stage area and the anaerobic reaction rear-stage area.
Preferably, the gas used by the gas stirring part is biogas, a desulfurization and deamination device is arranged on one side of the S-shaped reactor, a gas supply pipe of the gas stirring part is connected to the desulfurization and deamination device, and the gas supply pipe of the desulfurization and deamination device is connected to the tail end of the anaerobic reaction back section area, so that biogas generated at the tail end of the anaerobic reaction back section area is subjected to desulfurization and deamination treatment and then is subjected to gas stirring by the gas stirring part.
Preferably, the gas stirring member comprises a pulse blowing device, and the pulse frequency is 6 times/hour.
Preferably, the reflux component comprises a reflux pipe and a reflux pump, the reflux pump is connected to the reflux pipe in series, the first end of the reflux pipe is connected to the tail end of the anaerobic reaction rear-stage area for extracting biogas slurry, and the second end of the reflux pipe is connected to the front end of the anaerobic reaction front-stage area for discharging biogas slurry.
Preferably, the volume ratio of the returned biogas slurry to the fresh raw material is 1: 9.
preferably, the sand removing device comprises a container with a conical bottom surface, a sand discharging pipe is arranged in the container, the first end of the sand discharging pipe is located above the hammer-shaped bottom surface, and the second end of the sand discharging pipe is connected with a sewage pump and used for discharging gravel gathered on the conical bottom surface.
Preferably, the sand drain pipe comprises a transparent glass reinforced plastic pipe or a PV pipe.
Preferably, the front end of the anaerobic reaction front-stage zone is 28-30 ℃, the temperature of the tail end of the anaerobic reaction front-stage zone and the front end of the anaerobic reaction rear-stage zone is controlled at 37-38 ℃, and the temperature of the tail end of the anaerobic reaction rear-stage zone is controlled at 30 ℃.
Preferably, the S-shaped reactor is a concrete structure, has a height of 5 m and an aspect ratio of 20: 1, the raw materials stay in the S-shaped reactor for 21 to 25 days.
Compared with the prior art, the invention has the advantages that:
the anaerobic reaction system is designed in an S shape, and is designed in an integrated way from feeding to biogas generation, biogas desulfurization and deamination and biogas slurry deamination treatment, so that the occupied area and the building area are reduced, and heat supply is centralized;
sand particles in the fecal sewage raw material are removed through the sand removal device, and the sand particles brought into the reactor are greatly reduced, so that the cleaning time interval is greatly increased, the maintenance times are reduced, and the running stability of the system is kept;
through the arrangement of the heat exchange pipeline and the hydrolysis zone, the heat exchange pipeline penetrates through the tail end of the anaerobic reaction zone, heat exchange is carried out between biogas slurry and fresh excrement, the temperature and the hydrolysis speed of the excrement are rapidly improved, particularly in winter, the temperature of outdoor excrement is 3-4 ℃, the temperature difference between the outdoor excrement and the temperature in the reactor is too large, and the running stability of the anaerobic reactor is seriously influenced;
the temperature gradient is set in the anaerobic reaction zone through a hot water pipe, the temperature of the pretreatment zone is set at 30 ℃, the temperature of the anaerobic reaction zone is set at 37 ℃, the tail end of the anaerobic reaction zone is set at 30 ℃, and a smooth temperature gradient curve is formed at the front end, the middle end and the tail end, so that the energy consumption is reduced to the maximum extent;
and (3) strain backflow, wherein 10% biogas slurry flows back to the front end of the anaerobic reaction zone at the tail end of the anaerobic reaction zone, so that the concentration of the strain is increased, and the reaction speed and the degradation efficiency are improved.
It should be understood that all combinations of the foregoing concepts and additional concepts described in greater detail below can be considered as part of the inventive subject matter of this disclosure unless such concepts are mutually inconsistent. In addition, all combinations of claimed subject matter are considered a part of the presently disclosed subject matter.
The foregoing and other aspects, embodiments and features of the present teachings can be more fully understood from the following description taken in conjunction with the accompanying drawings. Additional aspects of the present invention, such as features and/or advantages of exemplary embodiments, will be apparent from the description which follows, or may be learned by practice of specific embodiments in accordance with the teachings of the present invention.
Drawings
The drawings are not intended to be drawn to scale. In the drawings, each identical or nearly identical component that is illustrated in various figures may be represented by a like numeral. For purposes of clarity, not every component may be labeled in every drawing. Embodiments of various aspects of the present invention will now be described, by way of example, with reference to the accompanying drawings, in which:
FIG. 1 is a schematic top view of a fecal sewage plug flow anaerobic reaction system according to the present invention;
FIG. 2 is a schematic structural diagram of a manure plug-flow anaerobic reaction system in a front view, which is shown in the invention;
fig. 3 is a schematic structural view of the sand removing device of the present invention.
Detailed Description
In order to better understand the technical content of the present invention, specific embodiments are described below with reference to the accompanying drawings.
In this disclosure, aspects of the present invention are described with reference to the accompanying drawings, in which a number of illustrative embodiments are shown. Embodiments of the present disclosure are not necessarily intended to include all aspects of the invention. It should be understood that the various concepts and embodiments described above, as well as those described in greater detail below, may be implemented in any of numerous ways in any fecal sewage plug anaerobic reaction system, as the disclosed concepts and embodiments are not limited to any embodiment. In addition, some aspects of the present disclosure may be used alone, or in any suitable combination with other aspects of the present disclosure.
The system provided by the invention can be suitable for enterprises and industries with high-concentration COD (chemical oxygen demand) such as farms, sewage plants, chemical plants and the like.
Referring to fig. 1-2, the invention provides a fecal sewage plug flow anaerobic reaction system, which mainly comprises a sand removal device 1, an S-shaped reactor 2, a heating pipe 5 and a heat exchange pipeline 12. The heat exchange pipeline 12 pumps the excrement raw liquid in the excrement collecting pool 11 into the sand removing device 1 for sand removal, and then the excrement raw liquid enters the S-shaped reactor 2 for anaerobic reaction after sand removal to generate biogas slurry and biogas.
Heat exchange pipe
Because the temperature of the excrement raw liquid pumped from the excrement collecting pool 11 is low, good reaction effect cannot be formed after the excrement raw liquid directly enters the S-shaped reactor 2, and because the temperature of the input excrement raw liquid is unstable, the operation stability of the S-shaped reactor 2 is affected, therefore, the heat exchange pipeline 12 penetrates through the S-shaped reactor 2 and exchanges heat at the tail end of the S-shaped reactor 2, the temperature of the biogas slurry is reduced, and the temperature of the excrement raw liquid is increased. Thus, the temperature stability of the input fecal sewage stock solution is maintained.
In an alternative embodiment, the heat exchange pipe 12 is arranged on the inner wall of the S-shaped reactor 2 in a disc shape to improve the heat exchange time and fully exchange heat between the fecal sewage and the biogas slurry.
Preferably, the outer wall of the heat exchange pipe 12 extending out of the S-shaped reactor is provided with an insulation layer, such as a polyurethane foam layer, to reduce temperature re-variation.
Sand removing device
The ideal concentration of the excrement TS (the content proportion of dry substances in the excrement mixed liquid) is 8-10%, the concentration is lower than 8%, the biogas yield is low, and the utilization efficiency of the anaerobic reactor is poor; the concentration is higher than 10%, and the gas stirring effect is poor. In order to reduce the content of solid matters in the manure raw liquid, a sand removal device 1 is arranged at the inlet end of the S-shaped reactor 2.
In an alternative embodiment, shown in connection with fig. 3, the sand removing device 1 comprises a container with a conical bottom surface, a sand discharge pipe 13 is arranged in the container, a first end of the sand discharge pipe 13 is positioned above the hammer-shaped bottom surface, and a second end of the sand discharge pipe is connected with a sewage pump 14 for discharging gravel accumulated on the conical bottom surface.
In an optional embodiment, the sand removing component 1 is a cuboid concrete structure, the concrete bottom plate is designed to be an inverted cone structure with a low middle part, a transparent sand discharging pipe 13 is installed above the inverted cone structure, one end of the sand discharging pipe is inserted into the bottom of the inverted cone, one end of the sand discharging pipe is connected with a sewage pump 14, and after sand enters the sand removing component 1, the sand naturally settles and is discharged through the sewage pump 14.
Preferably, the sand discharge pipe 13 comprises a transparent glass reinforced plastic pipe or a PV pipe, the transparent pipe is favorable for observation, and whether sand in the pipe is discharged completely can be judged by naked eyes, wherein the sewage pump 14 is selected according to the feeding amount, the power is 1.5-3kw, the lift is 10m, and the discharged sand can enter the sand washer for recycling.
S-shaped reactor
Referring to FIGS. 1-2, the S-shaped reactor 2 is provided with an S-shaped closed reaction channel having an inlet end and an outlet end; a hydrolysis zone 201, an anaerobic reaction front section zone 202, an anaerobic reaction rear section zone 203, an anoxic zone 6 and an aerobic aeration zone 7 are sequentially arranged in the S-shaped reactor 2 according to the flowing direction of biogas slurry.
Through the mode of integrating hydrolysis area 201, anaerobic reaction front end district 202, anaerobic reaction back end district 203, anoxic zone 6 and aerobic aeration district 7, can reduce the area of building, and thermal supply is concentrated relatively, hydrolysis area and anaerobic reaction district heat can be transferred, heat between anaerobic zone and the heat exchange pipeline 12 can be transferred, stoste between anaerobic reaction back end district 203 and the anaerobic reaction front end district 202 is easily exchanged, and the difference in temperature is little, therefore, be favorable to promoting whole reaction system's high reaction rate and degradation efficiency, reduce whole power consumption.
In an alternative embodiment, the anaerobic reactor 2 is an S-shaped concrete structure, 5 meters in height, with an aspect ratio of 20: 1, the retention time of the raw materials is 21 days to 25 days. Can meet the use requirement of large-scale farms.
Further, as shown in FIG. 1, the hydrolysis zone 201 and the anaerobic reaction front-stage zone 202 are separated by a retaining wall 3. A gap is reserved between the retaining wall 3 and the anaerobic reactor 2, part of the excrement passes through the gap and stays in the hydrolysis area 201, optionally, the staying time of the excrement raw material in the hydrolysis area 201 is 24 hours on average, the excrement raw material is hydrolyzed in the hydrolysis area 201, extracellular enzymes secreted by hydrolytic bacteria are utilized to decompose organic matters in the excrement into soluble substances such as monosaccharide, polysaccharide, polypeptide, lipid and the like, and the hydrolyzed organic matters enter an anaerobic reaction front-stage area 202 through the retaining wall 3.
As shown in figure 1, since the optimum action temperature of anaerobic bacteria is 30-35 ℃, heating pipes 8 are arranged in the anaerobic reaction front-stage area 202 and the anaerobic reaction rear-stage area 203 to heat the liquid in the anaerobic reaction front-stage area and the anaerobic reaction rear-stage area 203.
Optionally, the density of the heating pipes 8 in the anaerobic reaction front section 202 is greater than that of the heating pipes 8 in the anaerobic reaction rear section 203. And the heating pipe 8 in the anaerobic reaction front section 202.
Thus, the temperature of the front end of the anaerobic reaction front-stage area 201 can be controlled to be 28-30 ℃, the temperature of the tail end of the anaerobic reaction front-stage area and the temperature of the front end of the anaerobic reaction rear-stage area are controlled to be 37-38 ℃, and the temperature of the tail end of the anaerobic reaction rear-stage area is controlled to be 30 ℃. The front end, the middle end and the tail end of the anaerobic reaction form a smooth temperature gradient curve, and the energy consumption is reduced to the maximum extent.
In order to increase the anaerobic reaction efficiency, gas stirring components 4 are arranged in the anaerobic reaction front-stage area 202 and the anaerobic reaction rear-stage area 203, and the action effect between the reaction liquid and the flora is improved in a pneumatic stirring mode.
Preferably, the gas used by the gas stirring part 4 is biogas, and one side of the S-shaped reactor 2 is provided with a desulfurization and deamination device 9, the gas supply pipe of the gas stirring part 4 is connected to the desulfurization and deamination device 9, and the gas supply pipe of the desulfurization and deamination device is connected to the tail end of the anaerobic reaction back-stage area 203.
Thus, biogas generated at the tail end of the anaerobic reaction rear section area 203 is subjected to desulfurization and deamination treatment and then is subjected to gas stirring by the gas stirring component.
Optionally, desulfurization deamination device 9 contains desulfurization deamination tower, utilizes vulcanized bacterium and deamination bacterium, gets rid of hydrogen sulfide and ammonia in the marsh gas, makes discharged marsh gas purer, also prevents during hydrogen sulfide and ammonia reentrant the natural pond liquid, makes the ammonia content of natural pond liquid increase.
Preferably, the gas stirring means 4 comprises a pulse blowing device with a pulse frequency of 6 times/hour.
Further, as the tail end of the anaerobic reaction rear-stage area 203 contains methanogens with high concentration, a reflux component 8 is arranged between the tail end of the anaerobic reaction rear-stage area 203 and the front end of the anaerobic reaction front-stage area 202 and is used for refluxing biogas slurry at the tail end of the anaerobic reaction rear-stage area to the front end of the anaerobic reaction front-stage area. Therefore, the biological reaction at the front end of the anaerobic reaction zone is accelerated, and the degradation rate of the organic matters is improved.
Optionally, the reflux unit 8 includes a reflux pipe and a reflux pump, the reflux pump is connected in series to the reflux pipe, a first end of the reflux pipe is connected to the end of the anaerobic reaction back-stage region 203 to extract the biogas slurry, and a second end of the reflux pipe is connected to the front end of the anaerobic reaction front-stage region 202 to discharge the biogas slurry.
Preferably, the volume ratio of the returned biogas slurry to the fresh raw material is 1: 9.
further, the biogas slurry after anaerobic fermentation has high ammonia nitrogen content, and the direct discharge can cause secondary pollution caused by eutrophication of soil and water body. Therefore, an opening is arranged at the anoxic zone 6 of the S-shaped reactor 2 to form an anoxic zone, the deammoniation treatment is carried out by contacting with air, the energy consumption is saved by utilizing the temperature of the biogas slurry at the tail end of the reactor, and further, an aerator is arranged in the aerobic aeration zone 7 to improve the contact area and the reaction efficiency with the air. The ammonia nitrogen removal efficiency is improved through the residual temperature of the biogas slurry and the larger air inflow.
Therefore, energy consumption is reduced through a gas stirring and waste heat exchange mode; the reaction speed is accelerated by a strain backflow mode, so that the methane yield is maximized.
With the above embodiments, the present invention has the advantages that:
the anaerobic reaction system is designed in an S shape, and is designed in an integrated way from feeding to biogas generation, biogas desulfurization and deamination and biogas slurry deamination treatment, so that the occupied area and the building area are reduced, and heat supply is centralized;
sand particles in the fecal sewage raw material are removed through the sand removal device, and the sand particles brought into the reactor are greatly reduced, so that the cleaning time interval is greatly increased, the maintenance times are reduced, and the running stability of the system is kept;
through the arrangement of the heat exchange pipeline and the hydrolysis zone, the heat exchange pipeline penetrates through the tail end of the anaerobic reaction zone, heat exchange is carried out between biogas slurry and fresh excrement, the temperature and the hydrolysis speed of the excrement are rapidly improved, particularly in winter, the temperature of outdoor excrement is 3-4 ℃, the temperature difference between the outdoor excrement and the temperature in the reactor is too large, and the running stability of the anaerobic reactor is seriously influenced;
the temperature gradient is set in the anaerobic reaction zone through a hot water pipe, the temperature of the pretreatment zone is set at 30 ℃, the temperature of the anaerobic reaction zone is set at 37 ℃, the tail end of the anaerobic reaction zone is set at 30 ℃, and a smooth temperature gradient curve is formed at the front end, the middle end and the tail end, so that the energy consumption is reduced to the maximum extent;
and (3) strain backflow, wherein 10% biogas slurry flows back to the front end of the anaerobic reaction zone at the tail end of the anaerobic reaction zone, so that the concentration of the strain is increased, and the reaction speed and the degradation efficiency are improved.
Although the present invention has been described with reference to the preferred embodiments, it is not intended to be limited thereto. Those skilled in the art can make various changes and modifications without departing from the spirit and scope of the invention. Therefore, the protection scope of the present invention should be determined by the appended claims.
Claims (10)
1. A fecal sewage plug flow anaerobic reaction system is characterized by comprising:
the S-shaped reactor is provided with an S-shaped closed reaction channel and is provided with an inlet end and an outlet end;
the sand removing device is arranged at the inlet end of the S-shaped reactor;
the heat exchange pipeline penetrates through the S-shaped reactor, a first end of the heat exchange pipeline is connected to the excrement collecting pool, a second end of the heat exchange pipeline is connected to the sand removing device, and excrement stock solution and biogas slurry in the S-shaped reactor are conducted into the sand removing device to remove sand after heat exchange;
the system comprises an S-shaped reactor, a hydrolysis zone, an anaerobic reaction front-stage zone, an anaerobic reaction rear-stage zone, an anoxic zone and an aerobic aeration zone, wherein the hydrolysis zone, the anaerobic reaction front-stage zone, the anaerobic reaction rear-stage zone, the anoxic zone and the aerobic aeration zone are sequentially arranged in the S-shaped reactor according to the flowing direction of biogas slurry, the hydrolysis zone and the anaerobic reaction front-stage zone are separated by a retaining wall, heating pipes are arranged in the anaerobic reaction front-stage zone and the anaerobic reaction rear-stage zone, the density of the heating pipes in the anaerobic reaction front-stage zone is greater than that of the heating pipes in the anaerobic reaction rear-stage zone, the S-shaped reactor is provided with an opening at the anoxic zone, and an aerator is arranged in the aerobic aeration zone;
and a backflow part is arranged between the tail end of the anaerobic reaction rear section area and the front end of the anaerobic reaction front section area and is used for refluxing biogas slurry at the tail end of the anaerobic reaction rear section area to the front end of the anaerobic reaction front section area.
2. The fecal sewage push flow anaerobic reaction system of claim 1, wherein gas stirring components are arranged in the anaerobic reaction front stage zone and the anaerobic reaction rear stage zone.
3. The fecal sewage plug flow anaerobic reaction system of claim 2, wherein the gas used by the gas stirring part is biogas, a desulfurization and deamination device is arranged at one side of the S-shaped reactor, a gas supply pipe of the gas stirring part is connected to the desulfurization and deamination device, and the gas supply pipe of the desulfurization and deamination device is connected to the tail end of the anaerobic reaction back-stage area, so that the biogas generated at the tail end of the anaerobic reaction back-stage area is subjected to desulfurization and deamination treatment and then is stirred by the gas stirring part to gas the biogas slurry.
4. A fecal sewage push anaerobic reaction system according to claim 3 characterized in that the gas stirring means comprises a pulse blowing device with a pulse frequency of 6 times per hour.
5. The fecal sewage push flow anaerobic reaction system according to claim 1, wherein the reflux component comprises a reflux pipe and a reflux pump, the reflux pump is connected to the reflux pipe in series, the first end of the reflux pipe is connected to the tail end of the anaerobic reaction rear section zone to draw biogas slurry, and the second end of the reflux pipe is connected to the front end of the anaerobic reaction front section zone to discharge biogas slurry.
6. The fecal sewage push flow anaerobic reaction system of claim 5, wherein the volume ratio of the returned biogas slurry to the fresh raw material is 1: 9.
7. the fecal sewage plug flow anaerobic reaction system according to claim 1, wherein the sand removing device comprises a container with a conical bottom surface, a sand discharging pipe is arranged in the container, the first end of the sand discharging pipe is positioned above the hammer-shaped bottom surface, and the second end of the sand discharging pipe is connected with a sewage pump for discharging gravel gathered on the conical bottom surface.
8. The fecal sewage push anaerobic reaction system of claim 7, wherein the sand drain tube comprises a transparent glass reinforced plastic or PV tube.
9. A fecal sewage push flow anaerobic reaction system according to any of the claims 1-8, characterized in that the front end of the anaerobic reaction front section is 28-30 ℃, the temperature of the end of the anaerobic reaction front section and the front end of the anaerobic reaction rear section is controlled at 37-38 ℃, and the temperature of the end of the anaerobic reaction rear section is controlled at 30 ℃.
10. A fecal sewage push flow anaerobic reaction system according to any of the claims 1-8 characterized in that the S-shaped reactor is a concrete structure with a height of 5 meters and an aspect ratio of 20: 1, the raw materials stay in the S-shaped reactor for 21 to 25 days.
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Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN201952322U (en) * | 2010-10-26 | 2011-08-31 | 北京市环境保护科学研究院 | Anaerobic micropore aeration oxidation ditch reactor |
| CN102910730A (en) * | 2012-09-28 | 2013-02-06 | 方明环保科技(漳州)有限公司 | Thermophilic anaerobic digestion biological reaction system |
| CN203530020U (en) * | 2013-08-16 | 2014-04-09 | 苏州工业园区清源华衍水务有限公司 | Synchronous nitrification and denitrification wastewater treatment device |
| CN210974351U (en) * | 2019-06-06 | 2020-07-10 | 南京工大环境科技南通有限公司 | Sludge anaerobic digestion, desulfurization and energy recovery device |
| CN113430101A (en) * | 2021-07-15 | 2021-09-24 | 中钢集团天澄环保科技股份有限公司 | Efficient cooperative resource utilization method for livestock and poultry manure and silage straws |
-
2021
- 2021-11-12 CN CN202111341537.0A patent/CN113998856A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN201952322U (en) * | 2010-10-26 | 2011-08-31 | 北京市环境保护科学研究院 | Anaerobic micropore aeration oxidation ditch reactor |
| CN102910730A (en) * | 2012-09-28 | 2013-02-06 | 方明环保科技(漳州)有限公司 | Thermophilic anaerobic digestion biological reaction system |
| CN203530020U (en) * | 2013-08-16 | 2014-04-09 | 苏州工业园区清源华衍水务有限公司 | Synchronous nitrification and denitrification wastewater treatment device |
| CN210974351U (en) * | 2019-06-06 | 2020-07-10 | 南京工大环境科技南通有限公司 | Sludge anaerobic digestion, desulfurization and energy recovery device |
| CN113430101A (en) * | 2021-07-15 | 2021-09-24 | 中钢集团天澄环保科技股份有限公司 | Efficient cooperative resource utilization method for livestock and poultry manure and silage straws |
Non-Patent Citations (4)
| Title |
|---|
| 李永峰等: "环境生物技术 典型厌氧环境微生物过程", 31 August 2014, 哈尔滨工业大学出版社 * |
| 武深树: "畜禽粪便污染治理的环境成本控制和区域适宜性分析", 31 October 2013, 湖南科学技术出版社 * |
| 王岁楼等: "生化工程", 31 August 2002, 中国医药科技出版社 * |
| 赵智勇等: "十二五普通高等教育本科国家级规划教材 制浆造纸污染控制 第2版", 31 March 2020, 西北农林科技大学出版社 * |
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