CN215517068U - A multistage anaerobic system for tail dish thick liquid is handled - Google Patents
A multistage anaerobic system for tail dish thick liquid is handled Download PDFInfo
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- CN215517068U CN215517068U CN202120044789.6U CN202120044789U CN215517068U CN 215517068 U CN215517068 U CN 215517068U CN 202120044789 U CN202120044789 U CN 202120044789U CN 215517068 U CN215517068 U CN 215517068U
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Abstract
The utility model discloses a multi-stage anaerobic system for treating a tail vegetable slurry, which comprises a pretreatment unit, an ethanol fermentation type acid-producing phase reactor, an intermediate sedimentation tank, a sludge dewatering system, a stripping tank, a methane-producing phase reactor and an aerobic treatment unit, wherein the pretreatment unit is connected with the intermediate sedimentation tank; the pretreatment unit is connected with an ethanol fermentation type acid-producing phase reactor through a pipeline, and a pump body is arranged in the pipeline to provide power; the ethanol fermentation type acid-producing phase reactor is communicated with an intermediate sedimentation tank; the bottom of the intermediate sedimentation tank is communicated with a sludge dewatering system, the top of the intermediate sedimentation tank is communicated with a stripping tank, the stripping tank is communicated with a methanogenic phase reactor through a pipeline, a pump body is arranged in the pipeline to provide power, and a return pipe is arranged between the stripping tank and the methanogenic phase reactor; the methanogenic phase reactor is communicated with an aerobic treatment unit. Can remove pollutants in high-concentration organic wastewater under the condition of not adding metal coagulant, and has stable and high-efficiency treatment effect.
Description
Technical Field
The utility model relates to the field of wastewater treatment, in particular to a multistage anaerobic system for treating a rapeseed slurry.
Background
In the production process of food processing and the like, a certain amount of high-concentration organic wastewater, particularly waste pickle liquor, is discharged frequently, and the wastewater contains a large amount of organic substances such as carbohydrate, protein, grease, lignin and the like in a colloidal state or a dissolved state, and if the organic substances are directly discharged, the environment is seriously polluted.
The treatment of the organic wastewater of the high-concentration rape pulp liquid usually adopts a pretreatment and anaerobic-aerobic combined treatment process, and practices show that the process can effectively remove pollutants in the wastewater. However, for some waste water, because the content of carbohydrate in the waste water is high, a large amount of alkalinity is consumed in the anaerobic process, so that a large amount of alkaline substances are added, and the running cost is overhigh; the waste water containing more suspended substances or colloid substances is pretreated by a coagulating sedimentation or air floatation method, so a great amount of chemical sludge which is difficult to treat is generated, and secondary pollution is caused.
SUMMERY OF THE UTILITY MODEL
In order to overcome the problems in the prior art, the utility model provides a multistage anaerobic system for treating the waste vegetable pulp, which can remove pollutants in high-concentration organic wastewater without adding metal coagulants, has stable and efficient treatment effect, convenient sludge treatment and disposal, no secondary pollution, and can reduce the alkali amount required by pH value adjustment, and the operation cost is lower than that of the conventional process.
The technical scheme adopted by the utility model for solving the technical problems is as follows: a multi-stage anaerobic system for treating a pickle pulp comprises a pretreatment unit, an ethanol fermentation type acidogenic phase reactor, an intermediate sedimentation tank, a sludge dewatering system, a stripping tank, a methanogenic phase reactor and an aerobic treatment unit; the pretreatment unit is connected with an ethanol fermentation type acid-producing phase reactor through a pipeline, and a pump body is arranged in the pipeline to provide power; the ethanol fermentation type acid-producing phase reactor is communicated with an intermediate sedimentation tank; the bottom of the intermediate sedimentation tank is communicated with a sludge dewatering system, the top of the intermediate sedimentation tank is communicated with a stripping tank, the stripping tank is communicated with a methanogenic phase reactor through a pipeline, a pump body is arranged in the pipeline to provide power, and a return pipe is arranged between the stripping tank and the methanogenic phase reactor; the methanogenic phase reactor is communicated with an aerobic treatment unit.
The pretreatment unit can adopt conventional physical treatment methods such as grating, sedimentation, regulation and the like to remove large floating objects, silt and easily-precipitated organic matters in the wastewater, regulate water quantity and balance water quality, and create favorable conditions for subsequent biological treatment units.
The ethanol fermentation type acid-producing phase reactor is used for controlling the pH value in the reactor to be within the range of 4-4.5 by culturing ethanol-producing microorganisms and adjusting the hydraulic retention time, and performing acid-producing fermentation on the wastewater, wherein the fermentation product mainly comprises ethanol.
Because the pH value in the acidogenic phase reactor is low, the acidogenic phenomenon can occur, namely, some pollutants in the wastewater can be separated out from a dissolved state or a colloidal state under an acidic condition, converted into a suspended state and then removed by precipitation. Since this acidic condition is caused by microbial fermentation, it can be referred to as bio-acidification. The biological acid precipitation can fully utilize carbohydrate in the wastewater to produce acid, the acid precipitation condition can be achieved without adding inorganic acid, the coagulation of certain pollutants in a dissolved or colloidal state is promoted, and the microbial thallus has the coagulation promoting effect and can accelerate the precipitation separation speed of suspended matters, so that the secondary pollution caused by adding a coagulant can be avoided, and the wastewater treatment cost can be greatly reduced.
Meanwhile, the ethanol type fermentation product mainly contains ethanol, the final product of the ethanol which is continuously degraded in the subsequent methanogenic phase reactor is methane and carbon dioxide, the equivalent ratio is 3:1, while for other fermentation type acidogenic phase reactors, the fermentation product mainly contains acetic acid, propionic acid or butyric acid, the equivalent ratio of the methane to the carbon dioxide in the final degradation product of the acetic acid, the propionic acid or the butyric acid is 1:1, 11:9 and 5:3 respectively, and the carbon dioxide accounts for a ratio obviously higher than that of the ethanol. Because the carbon dioxide in the final product of the ethanol fermentation is least, the partial pressure of the carbon dioxide in the methane is low, the influence on the pH value is small, the pH control in a methanogenic phase reactor is facilitated, and the alkali amount required for adjusting the pH value can be reduced.
The intermediate sedimentation tank plays a role in removing suspended matters, as the acidification phenomenon occurs in the acidogenic phase reactor, some pollutants are converted into a suspended state from a dissolved or colloidal state, most pollutants are discharged along with water except for a small part of hydrolysis fermentation, and the pollutants need to be precipitated and removed in the intermediate sedimentation tank in order to reduce the load of a subsequent methanogenic phase reactor.
The pH value of the effluent of the intermediate sedimentation tank is 4-4.5, the alkalinity is low, and the pH value needs to be adjusted to improve the alkalinity in order to ensure the normal operation of the methanogenic phase reactor. Therefore, the measures of externally circulating and blowing off the effluent of the methanogenic phase reactor can be adopted, namely, part of the effluent of the methanogenic phase reactor is mixed with the effluent of the intermediate sedimentation tank and then enters a blowing-off tank, air is blown in for blowing off, and the mixture is returned to the methanogenic phase reactor after being deoxidized.
The effluent of the methanogenic phase reactor contains a large amount of alkalinity (as NaHCO)3Mainly), the effluent of the intermediate sedimentation tank contains organic acid, the organic acid sodium salt and carbon dioxide are generated after the organic acid sodium salt and the carbon dioxide are mixed, and the pH value of the wastewater can be increased after the carbon dioxide is blown off. The carbon dioxide generated after the organic acid sodium salt is degraded in the methanogenic phase reactor is combined with sodium ions and still uses NaHCO3Is present in the water, and is capable of replenishing the alkalinity in the reactor; if the mode of external reflux and stripping is still insufficient to maintain the proper pH value in the methanogenic phase reactor, a proper amount of liquid alkali can be added into the pH adjusting tank.
However, if an internal circulation mode is adopted, the effluent and the return water of the sedimentation tank are mixed in a closed pipeline, the generated carbon dioxide cannot be released, all the carbon dioxide enters a methanogenic phase reactor, the alkalinity cannot be supplemented, the alkalinity is consumed, and more liquid alkali needs to be added to maintain a proper pH value.
In order to improve the stripping effect and avoid the influence of oxygen brought into water by air blowing stripping on the strict anaerobic condition of a methane-producing phase, the stripping pool comprises a stripping area, a stripping area and a pH adjusting area, wherein the stripping area is positioned above the stripping area, the pH adjusting area is separated from the stripping area and the deoxidizing area, and the bottom of the deoxidizing area is communicated with the top of the pH adjusting area; the top of the stripping area is provided with overflow grooves distributed along the periphery, and the overflow grooves are communicated with a water outlet pipe of an intermediate sedimentation tank and a water return pipe of a methane-producing phase reactor; the bottom end of the pH adjusting area is communicated with a methane phase reactor through a pipeline provided with a pump body. The air for stripping enters from the lower part of the stripping area, the waste water enters the top of the stripping area, and the air and the water flow in the reverse direction, so that the maximum stripping effect can be obtained.
After the effluent of the intermediate sedimentation tank is mixed with the reflux water of the methanogenic phase reactor, the alkalinity in the water reacts with the organic acid to produce organic acid salt and carbon dioxide. The mixed wastewater firstly enters an overflow groove at the top of the blowing-off area and then overflows and falls to the top of the blowing-off area. In the falling process, part of carbon dioxide in the wastewater is volatilized to the atmosphere, then in the blowing-off area, the carbon dioxide in the wastewater is continuously transferred to the air through mass transfer, and the pH value of the wastewater is increased.
During stripping, some oxygen is also dissolved in the wastewater and, if it enters the methanogenic phase reactor, it may destroy its anaerobic environment. For this purpose, a deoxygenation zone is provided below the stripping zone, where the waste water suitably remains, consuming its dissolved oxygen.
After the waste water is blown off, alkali liquor can be added if the pH value still can not meet the water inlet requirement of the methane-producing phase reactor. In order to ensure the complete mixing of the alkali liquor and the waste water, a pH adjusting area is specially arranged, and the waste water after being blown off is mixed with the alkali liquor and then is lifted to a methane-producing phase reactor.
The stripping zone and the deoxidation zone run at constant water level, and wastewater after deoxidation enters the pH adjusting zone from the bottom of the deoxidation zone through a pipeline, so that the stripping and deoxidation time is ensured.
The utility model has the beneficial effects that:
(1) the method adopts multi-stage anaerobic reaction, wherein the first-stage anaerobic reaction mainly takes acidogenesis as an acidogenic phase reactor, and the second-stage or third-stage anaerobic reaction mainly takes methanogenesis as a methanogenic phase reactor. The first-order anaerobic reactor can effectively remove certain toxic substances, inhibitory substances or change the structures of certain refractory organic matters, reduce the adverse effects of the substances on methanogenic bacteria in a methanogenic phase reactor or improve the biodegradability of the methanogenic bacteria, is beneficial to the operation of a methanogenic phase, increases the stability of the whole system and also improves the treatment capacity of the whole system.
(2) The pH value in the acid-producing phase reactor is low, the acidification and demulsification effects can be realized, and some pollutants existing in a colloid state can be converted into a suspension state, so that the precipitation removal is facilitated; at this pH, some organics such as lignin can react with the acid and precipitate out of the water; the microbial cells also have a procoagulant effect. By the action, under the condition of not adding a metal coagulant, colloids, suspended matters and macromolecular organic matters in the wastewater can be effectively removed, and the load of a subsequent methanogenic phase reactor is reduced.
(3) The acidogenic phase reactor adopts ethanol fermentation, organic matters in effluent mainly comprise ethanol, final products of the ethanol in the methanogenic phase reactor mainly comprise methane, and the carbon dioxide accounts for a small amount, so that the alkalinity of the methane phase is favorably maintained, and the amount of liquid caustic soda required for adjusting the pH value is reduced.
(4) The methane-producing phase reactor adopts an external circulation operation mode, and is provided with a carbon dioxide stripping unit, so that the alkalinity of inlet water can be increased, and the carbon dioxide generated during reflux is prevented from entering the reactor again.
(5) The stripping pool is provided with a stripping area and a deoxidizing area, so that carbon dioxide can be stripped, and the destruction of dissolved oxygen to the methane-producing phase anaerobic environment can be avoided.
(6) The blowing-off area and the deoxidation area operate at constant water level, and water flows out from the lower part, so that the blowing-off and deoxidation time can be ensured.
(7) The system can remove pollutants in the high-concentration organic wastewater of the waste pickle pulp without adding a metal coagulant, has stable and efficient treatment effect, is convenient for sludge treatment and disposal, has no secondary pollution, can reduce the alkali amount required by pH value adjustment, and has lower operation cost than the conventional process.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the embodiments or the prior art will be briefly described below, it is obvious that the drawings in the following description are only some embodiments of the present invention, and for those skilled in the art, other drawings can be obtained according to the drawings without creative efforts.
FIG. 1 is a schematic diagram of the operation of the present invention;
FIG. 2 is a schematic diagram of the structure of a stripping cell.
Detailed Description
In order to make the objects, technical solutions and advantages of the present invention more apparent, the technical solutions of the present invention will be described in detail and completely with reference to the following embodiments and accompanying drawings. It is to be understood that the described embodiments are merely exemplary of the utility model, and not restrictive of the full scope of the utility model.
Referring to fig. 1-2, the present embodiment provides a multi-stage anaerobic system for processing a hull slurry, comprising a pretreatment unit, an ethanol fermentation type acidogenic phase reactor, an intermediate sedimentation tank, a sludge dewatering system, a stripping tank, a methanogenic phase reactor and an aerobic treatment unit; the pretreatment unit is connected with an ethanol fermentation type acid-producing phase reactor through a pipeline, and a pump body is arranged in the pipeline to provide power; the ethanol fermentation type acid-producing phase reactor is communicated with an intermediate sedimentation tank; the bottom of the intermediate sedimentation tank is communicated with a sludge dewatering system, the top of the intermediate sedimentation tank is communicated with a stripping tank, the stripping tank is communicated with a methanogenic phase reactor through a pipeline, a pump body is arranged in the pipeline to provide power, and a return pipe is arranged between the stripping tank and the methanogenic phase reactor; the methanogenic phase reactor is communicated with an aerobic treatment unit.
The pretreatment unit can adopt conventional physical treatment methods such as grating, sedimentation, regulation and the like to remove large floating objects, silt and easily-precipitated organic matters in the wastewater, regulate water quantity and balance water quality, and create favorable conditions for subsequent biological treatment units.
The ethanol fermentation type acid-producing phase reactor is used for controlling the pH value in the reactor to be within the range of 4-4.5 by culturing ethanol-producing microorganisms and adjusting the hydraulic retention time, and performing acid-producing fermentation on the wastewater, wherein the fermentation product mainly comprises ethanol.
Because the pH value in the acidogenic phase reactor is low, the acidogenic phenomenon can occur, namely, some pollutants in the wastewater can be separated out from a dissolved state or a colloidal state under an acidic condition, converted into a suspended state and then removed by precipitation. Since this acidic condition is caused by microbial fermentation, it can be referred to as bio-acidification. The biological acid precipitation can fully utilize carbohydrate in the wastewater to produce acid, the acid precipitation condition can be achieved without adding inorganic acid, the coagulation of certain pollutants in a dissolved or colloidal state is promoted, and the microbial thallus has the coagulation promoting effect and can accelerate the precipitation separation speed of suspended matters, so that the secondary pollution caused by adding a coagulant can be avoided, and the wastewater treatment cost can be greatly reduced.
Meanwhile, the ethanol type fermentation product mainly contains ethanol, the final product of the ethanol which is continuously degraded in the subsequent methanogenic phase reactor is methane and carbon dioxide, the equivalent ratio is 3:1, while for other fermentation type acidogenic phase reactors, the fermentation product mainly contains acetic acid, propionic acid or butyric acid, the equivalent ratio of the methane to the carbon dioxide in the final degradation product of the acetic acid, the propionic acid or the butyric acid is 1:1, 11:9 and 5:3 respectively, and the carbon dioxide accounts for a ratio obviously higher than that of the ethanol. Because the carbon dioxide in the final product of the ethanol fermentation is least, the partial pressure of the carbon dioxide in the methane is low, the influence on the pH value is small, the pH control in a methanogenic phase reactor is facilitated, and the alkali amount required for adjusting the pH value can be reduced.
The intermediate sedimentation tank plays a role in removing suspended matters, as the acidification phenomenon occurs in the acidogenic phase reactor, some pollutants are converted into a suspended state from a dissolved or colloidal state, most pollutants are discharged along with water except for a small part of hydrolysis fermentation, and the pollutants need to be precipitated and removed in the intermediate sedimentation tank in order to reduce the load of a subsequent methanogenic phase reactor.
The pH value of the effluent of the intermediate sedimentation tank is 4-4.5, the alkalinity is low, and the pH value needs to be adjusted to improve the alkalinity in order to ensure the normal operation of the methanogenic phase reactor. Therefore, the measures of externally circulating and blowing off the effluent of the methanogenic phase reactor can be adopted, namely, part of the effluent of the methanogenic phase reactor is mixed with the effluent of the intermediate sedimentation tank and then enters a blowing-off tank, air is blown in for blowing off, and the mixture is returned to the methanogenic phase reactor after being deoxidized.
The effluent of the methanogenic phase reactor contains a large amount of alkalinity (as NaHCO)3Mainly), the effluent of the intermediate sedimentation tank contains organic acid, the organic acid sodium salt and carbon dioxide are generated after the organic acid sodium salt and the carbon dioxide are mixed, and the pH value of the wastewater can be increased after the carbon dioxide is blown off. The carbon dioxide generated after the organic acid sodium salt is degraded in the methanogenic phase reactor is combined with sodium ions and still uses NaHCO3Is present in the water, and is capable of replenishing the alkalinity in the reactor; if the mode of external reflux and stripping is still insufficient to maintain the proper pH value in the methanogenic phase reactor, a proper amount of liquid alkali can be added into the pH adjusting tank.
However, if an internal circulation mode is adopted, the effluent and the return water of the sedimentation tank are mixed in a closed pipeline, the generated carbon dioxide cannot be released, all the carbon dioxide enters a methanogenic phase reactor, the alkalinity cannot be supplemented, the alkalinity is consumed, and more liquid alkali needs to be added to maintain a proper pH value.
In order to improve the stripping effect and avoid the influence of oxygen brought into water by air blowing stripping on the strict anaerobic condition of a methane-producing phase, the stripping pool comprises a stripping area, a stripping area and a pH adjusting area, wherein the stripping area is positioned above the stripping area, the pH adjusting area is separated from the stripping area and the deoxidizing area, and the bottom of the deoxidizing area is communicated with the top of the pH adjusting area; the top of the stripping area is provided with overflow grooves distributed along the periphery, and the overflow grooves are communicated with a water outlet pipe of an intermediate sedimentation tank and a water return pipe of a methane-producing phase reactor; the bottom end of the pH adjusting area is communicated with a methane phase reactor through a pipeline provided with a pump body. The air for stripping enters from the lower part of the stripping area, the waste water enters the top of the stripping area, and the air and the water flow in the reverse direction, so that the maximum stripping effect can be obtained.
After the effluent of the intermediate sedimentation tank is mixed with the reflux water of the methanogenic phase reactor, the alkalinity in the water reacts with the organic acid to produce organic acid salt and carbon dioxide. The mixed wastewater firstly enters an overflow groove at the top of the blowing-off area and then overflows and falls to the top of the blowing-off area. In the falling process, part of carbon dioxide in the wastewater is volatilized to the atmosphere, then in the blowing-off area, the carbon dioxide in the wastewater is continuously transferred to the air through mass transfer, and the pH value of the wastewater is increased.
During stripping, some oxygen is also dissolved in the wastewater and, if it enters the methanogenic phase reactor, it may destroy its anaerobic environment. For this purpose, a deoxygenation zone is provided below the stripping zone, where the waste water suitably remains, consuming its dissolved oxygen.
After the waste water is blown off, alkali liquor can be added if the pH value still can not meet the water inlet requirement of the methane-producing phase reactor. In order to ensure the complete mixing of the alkali liquor and the waste water, a pH adjusting area is specially arranged, and the waste water after being blown off is mixed with the alkali liquor and then is lifted to a methane-producing phase reactor.
The stripping zone and the deoxidation zone run at constant water level, and wastewater after deoxidation enters the pH adjusting zone from the bottom of the deoxidation zone through a pipeline, so that the stripping and deoxidation time is ensured.
The above description is only for the purpose of illustrating the preferred embodiments of the present invention and is not to be construed as limiting the utility model, and any modifications, equivalents and improvements made within the spirit and principle of the present invention are intended to be included within the scope of the present invention.
Claims (2)
1. A multi-stage anaerobic system for treating a pickle pulp is characterized by comprising a pretreatment unit, an ethanol fermentation type acidogenic phase reactor, an intermediate sedimentation tank, a sludge dewatering system, a stripping tank, a methanogenic phase reactor and an aerobic treatment unit; the pretreatment unit is connected with an ethanol fermentation type acid-producing phase reactor through a pipeline, and a pump body is arranged in the pipeline to provide power; the ethanol fermentation type acid-producing phase reactor is communicated with an intermediate sedimentation tank; the bottom of the intermediate sedimentation tank is communicated with a sludge dewatering system, the top of the intermediate sedimentation tank is communicated with a stripping tank, the stripping tank is communicated with a methanogenic phase reactor through a pipeline, a pump body is arranged in the pipeline to provide power, and a return pipe is arranged between the stripping tank and the methanogenic phase reactor; the methanogenic phase reactor is communicated with an aerobic treatment unit.
2. The multi-stage anaerobic system for canola slurry treatment of claim 1, wherein the blow tank includes a blow zone, a deoxygenation zone, and a pH adjustment zone; the stripping zone is positioned above the deoxygenation zone, the pH adjusting zone is separated from the stripping zone and the deoxygenation zone, and the bottom of the deoxygenation zone is communicated with the top of the pH adjusting zone; the top of the stripping area is provided with overflow grooves distributed along the periphery, and the overflow grooves are communicated with a water outlet pipe of an intermediate sedimentation tank and a water return pipe of a methane-producing phase reactor; the bottom end of the pH adjusting area is communicated with a methane phase reactor through a pipeline provided with a pump body.
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| CN202120044789.6U CN215517068U (en) | 2021-01-08 | 2021-01-08 | A multistage anaerobic system for tail dish thick liquid is handled |
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| CN202120044789.6U CN215517068U (en) | 2021-01-08 | 2021-01-08 | A multistage anaerobic system for tail dish thick liquid is handled |
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