CN107459207B - Integrated device for treating aquaculture wastewater and application thereof - Google Patents

Integrated device for treating aquaculture wastewater and application thereof Download PDF

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CN107459207B
CN107459207B CN201710728674.7A CN201710728674A CN107459207B CN 107459207 B CN107459207 B CN 107459207B CN 201710728674 A CN201710728674 A CN 201710728674A CN 107459207 B CN107459207 B CN 107459207B
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tank
aeration
anaerobic
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folded plate
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CN107459207A (en
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张涛
方慈
江荣风
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China Agricultural University
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China Agricultural University
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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
    • C02F9/00—Multistage treatment of water, waste water or sewage
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/02—Treatment of water, waste water, or sewage by heating
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
    • C02F1/442—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by nanofiltration
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
    • C02F1/444—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by ultrafiltration or microfiltration
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
    • C02F1/5263—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using natural chemical compounds
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/58—Treatment of water, waste water, or sewage by removing specified dissolved compounds
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F2001/007—Processes including a sedimentation step
    • 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
    • C02F2303/00—Specific treatment goals
    • C02F2303/04—Disinfection
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/28—Anaerobic digestion processes
    • C02F3/284—Anaerobic digestion processes using anaerobic baffled reactors
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/30—Aerobic and anaerobic processes
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F7/00—Aeration of stretches of water
    • 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 an integrated device for treating aquaculture wastewater and application thereof. The device comprises a culture wastewater storage tank, a U-shaped tubular hydrothermal reactor, a folded plate anaerobic bioflocculation plug flow tank, an inclined plate aeration crystallization tank, a dynamic ultrafiltration membrane reaction tank, an aeration-nanofiltration bifunctional membrane reaction tank and a water collection sedimentation tank; the sample inlet of the U-shaped tubular hydrothermal reactor is connected with the sample outlet of the culture wastewater reservoir; a sample outlet of the U-shaped tubular hydrothermal reactor is connected with a sample inlet of the folded plate anaerobic biological flocculation plug flow pool; the sample outlet of the folded plate anaerobic biological flocculation plug flow tank is connected with the sample inlet of the inclined plate aeration crystallization tank; the sample outlet of the inclined plate aeration crystallization tank is connected with the sample inlet of the dynamic ultrafiltration membrane reaction tank; the sample outlet of the dynamic ultrafiltration membrane reaction tank is connected with the sample inlet of the aeration-nanofiltration dual-function membrane reaction tank; the sample outlet of the aeration-nanofiltration dual-function membrane reaction tank is connected with the water-collecting sedimentation tank. The invention can realize the safe, resource and energy treatment of the culture wastewater at the same time.

Description

Integrated device for treating aquaculture wastewater and application thereof
Technical Field
The invention relates to an integrated device for treating aquaculture wastewater and application thereof, belonging to the technical field of agricultural resources and environment.
Background
In recent years, the change of the breeding mode of China from a scattered breeding mode to an intensive breeding mode accelerates the development of animal husbandry, and simultaneously, various environmental problems are generated, particularly the problems of non-point source pollution and water eutrophication pollution caused by the contradictory problem that breeding wastewater is excessively discharged and cannot be absorbed by limited land. On the other hand, the aquaculture wastewater is rich in a large amount of energy elements and nutrient elements such as carbon, oxygen, nitrogen, phosphorus and the like, and is a renewable resource. Therefore, a treatment mode of recycling and replacing the culture wastewater by energy has become one of the modes of environmental sustainable development.
However, the breeding wastewater belongs to high-concentration organic wastewater, the water quality characteristics of the breeding wastewater are different from that of common domestic wastewater, the Chemical Oxygen Demand (COD), the total suspended solid (TS) content, ammonia nitrogen and total phosphorus content of the breeding wastewater are far higher than that of the domestic wastewater, and abundant organic matters bring difficulty to the treatment of the breeding wastewater.
At present, the conventional cultivation wastewater treatment process mainly adopts a biogas fermentation process, can effectively reduce COD and generate biogas to realize energy utilization. The patent 'integrated livestock and poultry breeding wastewater treatment method (CN 201210201431.5)' discloses a high-concentration organic wastewater treatment method, which realizes the utilization of biogas energy and the standard discharge of water quality of breeding wastewater through flocculation, solid-liquid separation, UASB anaerobic fermentation, ultrasonic ozone oxidation, filter material filtration and other methods. However, the method cannot realize thorough sterilization and does not realize the recovery of resources such as nitrogen, phosphorus and the like. The patent 'a method for treating aquaculture wastewater (CN 201210454362.9)' discloses a method for treating aquaculture wastewater, which is characterized in that liquid fertilizer is prepared by the modes of wastewater powder, collection, concentration and anaerobic fermentation, and wastewater is discharged after reaching the standard. However, the method still does not realize complete sterilization, and chemical reagents are still needed to be supplemented to enhance the fermentation effect and improve the concentration of the effective components of the liquid fertilizer.
Disclosure of Invention
The invention aims to provide an integrated device for treating aquaculture wastewater and application thereof, which can reasonably treat the aquaculture wastewater to ensure that the aquaculture wastewater reaches the standard and is discharged, reduce the environmental sanitation risk and recycle the aquaculture wastewater to realize the reutilization of resources and energy; can realize the safe, resource and energy treatment of the culture wastewater at the same time.
The invention provides an integrated device for treating aquaculture wastewater, which is characterized in that: the device comprises a culture wastewater storage tank, a U-shaped tubular hydrothermal reactor, a folded plate anaerobic bioflocculation plug flow tank, an inclined plate aeration crystallization tank, a dynamic ultrafiltration membrane reaction tank, an aeration-nanofiltration bifunctional membrane reaction tank and a water collection sedimentation tank;
the sample inlet of the U-shaped tubular hydrothermal reactor is connected with the sample outlet of the culture wastewater reservoir;
the sample outlet of the U-shaped tubular hydrothermal reactor is connected with the sample inlet of the folded plate anaerobic biological flocculation plug flow pool;
the sample outlet of the folded plate anaerobic biological flocculation plug flow tank is connected with the sample inlet of the inclined plate aeration crystallization tank;
the sample outlet of the inclined plate aeration crystallization tank is connected with the sample inlet of the dynamic ultrafiltration membrane reaction tank;
the sample outlet of the dynamic ultrafiltration membrane reaction tank is connected with the sample inlet of the aeration-nanofiltration dual-function membrane reaction tank;
and a sample outlet of the aeration-nanofiltration bifunctional membrane reaction tank is connected with the water collection sedimentation tank.
In the integrated device, the integrated device for treating the aquaculture wastewater is designed in a container type, and the specific size of each part of the integrated device for treating the aquaculture wastewater can be scaled according to the size of the container in an equal proportion;
one side of the U-shaped tubular hydrothermal reactor is provided with a sample inlet and a closed heating inner container, and the other side of the U-shaped tubular hydrothermal reactor is provided with a sample outlet and a normal-pressure cooling inner container;
pressure valves are respectively arranged between the sample inlet of the U-shaped tubular hydrothermal reactor and the closed heating inner container and between the closed heating inner container and the normal-pressure cooling inner container;
the closed heating inner container and the normal pressure cooling inner container are respectively provided with a sampling port, a pressure gauge and a temperature sensor; the normal pressure cooling liner is also provided with an air outlet pipe for collecting the ammonia gas volatilized by heating, and the air outlet pipe is communicated with the inclined plate aeration crystallization tank;
the U-shaped tubular hydrothermal reactor is cast by steel materials, the length ratio of the outer diameter of the tube to the inner diameter of the tube of the U-shaped tubular hydrothermal reactor is 1.5-2: 1, and the length ratio of the inner diameter of the tube to the length of the tube is 1: 3-5.
In the integrated device, a sample outlet of the U-shaped tubular hydrothermal reactor is communicated with a sample inlet of the folded plate anaerobic biological flocculation plug flow pool by adopting a high-temperature resistant tube;
the high-temperature resistant pipe is arranged at the bottom of the folded plate anaerobic biological flocculation plug flow tank, and the temperature of the folded plate anaerobic biological flocculation plug flow tank is ensured to be 30-50 ℃ by utilizing the residual temperature of the water discharged by the U-shaped tubular hydrothermal reactor;
the high-temperature resistant pipe is made of tripropylene polyethylene (PPR for short), and the ratio of the outer diameter to the inner diameter can be 1.25: 1.
In the integrated device, the integrated device further comprises a gas collecting device and a sludge dewatering device;
the folded plate anaerobic biological flocculation plug flow tank comprises 3-5 anaerobic chambers which are communicated, each anaerobic chamber comprises a downstream chamber and an upstream chamber, and the downstream chamber and the upstream chamber are divided by folded plate semi-closed; the top end of the folded plate is vertically connected with the inner wall of the top end of the folded plate anaerobic bioflocculation plug flow tank; the inclination angle of the lower end of the folded plate can be 30-60 degrees, specifically 30 degrees, 45 degrees and 60 degrees, and the direction is inclined from the upper flow chamber to the lower flow chamber; the height from the lower end of the folded plate to the bottom of the folded plate anaerobic bioflocculation plug flow pool is 10-30% of the height of the bottom of the folded plate anaerobic bioflocculation plug flow pool;
the volume ratio of the downstream chamber to the upstream chamber may be 1: 4;
the volume of the anaerobic chamber arranged from the sample inlet of the folded plate anaerobic biological flocculation plug flow pool to the sample outlet thereof is sequentially increased, and the vertical height of the water inlet level of the anaerobic chamber is in a decreasing state; the top of each anaerobic chamber is provided with an air outlet, and the air outlets of the anaerobic chambers are communicated with the gas collecting device to collect biogas;
3 equidistant liquid sampling ports are respectively and vertically arranged on the outer wall of the anaerobic chamber, so that the real-time monitoring of the water quality is facilitated; the bottom of the anaerobic chamber of the folded plate anaerobic biological flocculation plug flow tank is provided with a sludge discharge port I, and the sludge discharge port I is communicated with a sample inlet of the sludge dewatering device; and backflow pipes are arranged on the side surface of the sludge discharge port (I) from the sample outlet to the sample inlet of the folded plate anaerobic biological flocculation plug flow tank.
When the device is used, a compound biological flocculant is put into a downstream chamber of the first anaerobic chamber, and the compound biological flocculant is generated by inoculating seed liquid of autotrophic microorganisms with high flocculation capacity into a fermentation culture medium in a volume ratio of 5-10% and fermenting, wherein the adding ratio is 20-50 m L/L.
In the integrated device, the inclined plate aeration crystallization tank is divided into a pre-aeration settling chamber and a seed crystal suspension crystallization chamber in a semi-closed manner by a water seepage plate, and the pre-aeration settling chamber is communicated with the seed crystal suspension crystallization chamber; the volume ratio of the pre-aeration settling chamber to the seed crystal suspension crystallization chamber is 1: 3-5; the water inlet of the pre-aeration settling chamber is communicated with the water outlet of the folded plate anaerobic bio-flocculation plug flow tank; the water inlet of the seed crystal suspension crystallization chamber is communicated with the water outlet of the pre-aeration settling chamber through a pore passage at the lower part of the water seepage plate;
the vertical height of the water inlet level of the pre-aeration settling chamber is 5-10% lower than that of the water outlet level of the folded plate anaerobic bio-flocculation plug flow tank;
the crystal seed suspension crystallization chamber comprises an upper inclined plate separation area, a middle aeration stirring area and a lower crystal mud storage area; the inclined angle of the inclined plate of the upper inclined plate separation area is 10-15 degrees, the inclined direction of the inclined plate is opposite to the water flow direction in use, namely the inclined plate inclines from the water outlet side to the water inlet side; when the invention is used, the inclined plate has the functions of blocking particles and further strengthening the solid-liquid separation, so that the inclined direction is opposite to the water flow direction to play a role in blocking; the volume of the upper inclined plate separation area accounts for 1/4-1/3 of the seed crystal suspension crystallization chamber;
the inclined plate aeration crystallization tank adopts tubular microporous aeration as an aeration head, and the height of the aeration head which is 10-15% of the height of the bottom of the inclined plate aeration crystallization tank is uniformly and horizontally distributed at the bottom of the tank; the pipe diameter ratio of the branch pipe to the main pipe of the tubular microporous aeration head is 1: 1.5-2; the coverage rate of the micropores is 20% -60%;
the bottoms of the pre-aeration settling chamber and the seed crystal suspension type crystallization chamber are respectively provided with a sludge discharge port (II) and a sludge discharge port (III), and the sludge discharge port (II) and the sludge discharge port (III) are both connected with a sample inlet of the sludge dewatering device; an aerobic reflux pipe is arranged from the seed crystal suspension type crystallization chamber to the pre-aeration settling chamber and is driven by a reflux pump, and partial crystal mud is refluxed by the reflux pump.
In the integrated device, the dynamic ultrafiltration membrane reaction tank comprises at least 1 group of flat plate type membrane modules, and each group of the membrane modules is formed by pressing 5-100 membrane sheets; the membrane material adopts non-woven fabrics and/or a screen; the spinning density of the membrane component is 20-40 g/m2The membrane flux is 40-100L/(m)2H), the operating pressure is 0.3-0.5 MPa;
the upper end of the membrane component is provided with a pressure gauge for observing pressure intensity;
the vertical height of the water inlet level of the pre-aeration settling chamber is 5-10% lower than that of the water outlet level of the folded plate anaerobic bio-flocculation plug flow tank;
the vertical height of the water inlet level of the dynamic ultrafiltration membrane reaction tank is 5-10% lower than that of the water outlet level of the pre-aeration settling chamber;
the bottom of the dynamic ultrafiltration membrane reaction tank is provided with a disc microporous aeration head which is 10-15% of the height away from the bottom of the dynamic ultrafiltration membrane reaction tank; the two sides of the membrane component are provided with lateral microporous aeration heads, the aeration mode is intermittent aeration, the aeration interval is 3-6h, and the aeration time is 10-30 min;
a sludge discharge port (IV) is formed in the bottom of the dynamic ultrafiltration membrane reaction tank and is connected with a sample inlet of the sludge dewatering device;
an aerobic return pipe is arranged from the dynamic ultrafiltration membrane reaction tank to the inclined plate aeration crystallization tank, is driven by a return pump, and returns partial sludge by the return pump.
In the integrated device, the aeration-nanofiltration dual-function membrane reaction tank comprises two sets of flat plate type membrane assemblies, each set of flat plate type membrane assembly comprises at least 1 set of membrane assembly, the flat plate type membrane assemblies have nanofiltration and aeration functions, when one set of flat plate type membrane assembly is connected with an air pump for aeration, the other set of flat plate type membrane assembly is connected with a water outlet pump for nanofiltration, the interval is 1-2h, and the two sets of flat plate type membrane assemblies are exchangedThe membrane assembly is sleeved to perform aeration back washing on the original nanofiltration functional membrane assembly, each group of flat-plate membrane assemblies can be formed by pressing 5-20 membrane sheets, the membrane sheet material is hollow fiber, the membrane aperture of each flat-plate membrane assembly is 1-2 nm, and the membrane flux is 10-30L/(m & lt/m & gt)2·h)；
A sludge discharge port (V) is formed in the bottom of the aeration-nanofiltration dual-function membrane reaction tank and is connected with a sample inlet of the sludge dewatering device;
an aerobic reflux pipe is arranged from the aeration-nanofiltration difunctional membrane reaction tank to the inclined plate aeration crystallization tank, and the reflux proportion can be 10-20%.
In the integrated device, a sludge discharge port (VI) is formed in the bottom of the water collecting sedimentation tank and communicated with a sample inlet of the sludge dewatering device;
an anaerobic return pipe is arranged from the water collecting sedimentation tank to a first anaerobic chamber of the folded plate anaerobic biological flocculation plug flow tank, the return ratio is 10-20%, and 80-90% of the regenerated water in the water collecting sedimentation tank is used for circulating water of a farm.
The invention also provides a method for treating aquaculture wastewater by using the integrated aquaculture wastewater treatment device, which comprises the following steps:
(1) introducing culture wastewater into the culture wastewater storage tank, closing the pressure valve between the closed heating inner container and the normal-pressure cooling inner container in the U-shaped tubular hydrothermal reactor, pumping the culture wastewater into the U-shaped tubular hydrothermal reactor from the culture wastewater storage tank through a sample inlet pipe by using a lift pump, stopping the work of the lift pump when a liquid level sensor of the closed heating inner container monitors that the liquid level is 70% of the total inner container height, refluxing redundant wastewater in the sample inlet pipe to the culture wastewater storage tank, and closing the pressure valve between the sample inlet and the closed heating inner container to enable the closed heating inner container to be in a sealed state; controlling the closed heating liner to perform heating reaction;
(2) after the aquaculture wastewater in the step (1) completes hydrothermal reaction, opening the pressure valve between the closed heating liner and the normal-pressure cooling liner to enable the sample to automatically flow into the normal-pressure cooling liner by utilizing the principle of a U-shaped pipe; opening a valve of an ammonia gas delivery pipe by the cooling liner, releasing pressure, and introducing gas containing ammonia gas into the inclined plate aeration crystallization tank to increase the ammonia nitrogen concentration; then, opening the pressure valve between the sealed heating liner and the sample inlet, opening a lifting pump of the culture wastewater reservoir again for sample injection until the liquid level heights of the sealed heating liner and the normal-pressure cooling liner are both 70% of the heights of the liners, closing valves at two ends of the sealed heating liner, and repeating the step (1) to perform heating reaction on the sealed heating liner; the retention time of the wastewater in the normal-pressure cooling liner is the same as that of the wastewater in the closed heating liner, and the pressure of the wastewater in the sample outlet pipe is controlled to be restored to normal atmospheric pressure, wherein the temperature is 70-90 ℃;
(3) the culture wastewater treated in the step (2) flows to the high-temperature resistant pipe from the normal-pressure cooling liner through a lift pump;
(4) the aquaculture wastewater treated in the step (3) flows into the folded plate anaerobic biological flocculation plug flow tank from the upper side of the side surface of the folded plate anaerobic biological flocculation plug flow tank through a high-temperature-resistant pipe through a lifting pump, and after the flocculation and precipitation are strengthened by a biological flocculant in the first anaerobic chamber, the supernatant gradually flows through the rest anaerobic chambers in the folded plate anaerobic biological flocculation plug flow tank;
(5) enabling the supernatant of the folded plate anaerobic bioflocculation plug flow tank in the step (4) to flow into the pre-aeration settling chamber of the inclined plate aeration crystallization tank from top to bottom; then the magnesium agent solution and the pH value regulating agent are added after entering the seed crystal suspension crystallization chamber from the lower part of the pre-aeration settling chamber through a porous plate channel, and a nucleation crystallization reaction is carried out in an intermediate aeration stirring area; large granular phosphorus crystals are precipitated into the lower crystal mud storage area, small granular crystals enter the upper inclined plate separation area along with water flow, fall back to the middle aeration stirring area after encountering the obstruction of the upper inclined plate separation area, continue to grow by polymerization as crystal seeds, generate large granular phosphorus grains and then precipitate into the lower crystal mud storage area, and 10-20% of crystal mud in the lower crystal mud storage area flows back to the pre-aeration precipitation chamber;
(6) enabling the overflow liquid in the step (5) to flow into the dynamic ultrafiltration membrane reaction tank from top to bottom to further reduce the concentration of nitrogen and phosphorus in water; opening a lift pump, and allowing overflow liquid to flow to the aeration-nanofiltration dual-function membrane reaction tank from bottom to top through an ultrafiltration membrane of the dynamic ultrafiltration membrane reaction tank; 10-20% of sludge at the bottom of the tank flows back to the inclined plate aeration crystallization tank;
(7) enabling the filtrate in the step (6) to flow into the aeration-nanofiltration dual-function reaction tank from top to bottom; exchanging the functions of the two sets of nanofiltration membranes by adjusting the aeration-nanofiltration dual-function adjusting valve at intervals of 1-2 h; 10-20% of sludge at the bottom of the tank flows back to the inclined plate aeration crystallization tank;
(8) and (3) enabling the filtrate in the step (7) to flow into the water collecting sedimentation tank from top to bottom, enabling 80-90% of regenerated water to flow out of a water outlet and be used for circulating water of a farm, and enabling 10-20% of sludge at the bottom of the tank to flow back to the first anaerobic chamber of the folded plate anaerobic bioflocculation plug flow tank through an anaerobic return pipe for continuous treatment.
In the invention, in the step (1), the pressure and the temperature are monitored in real time through a pressure gauge and a temperature sensor in the whole heating process, and the change of the physicochemical property of a sample can also be sampled and monitored at regular time;
introducing gas containing ammonia gas into an inclined plate aeration crystallization tank to increase the ammonia nitrogen concentration so as to facilitate subsequent crystallization reaction;
the retention time of the wastewater in the normal-pressure cooling liner is the same as that of the wastewater in the closed heating liner, so that semi-continuous sample introduction and sample discharge are realized.
In the method, in the step (1), the heating temperature of the sealed heating inner container is controlled to be 110-150 ℃, the heating time is controlled to be 20-60min, and the reaction pressure is 2.0-5.0 Mpa;
in the step (3), the flow rate of the treated wastewater flowing to the high-temperature resistant pipe is controlled to be 0.5-1.0L/h by using a flow meter, and the retention time in the pipe can be 20-60 min;
the outlet water flowing into the folded plate anaerobic biological flocculation plug flow tank from the high temperature resistant pipe can have the temperature of 30-50 ℃;
the step (4) also comprises that the flow rate of wastewater inflow of the folded plate anaerobic biological flocculation plug flow pool can be 0.5-1.0L/h, sludge at the bottoms of several anaerobic chambers behind the first anaerobic chamber is forced to flow back to the first anaerobic chamber so as to further improve the anaerobic treatment efficiency, the sludge backflow proportion is 15-30%, the sludge backflow proportion of the anaerobic chambers can be different, and the retention time in the folded plate anaerobic biological flocculation plug flow pool is 48-96 h;
collecting partial gas from the gas collection port by using biogas generated in the folded plate anaerobic bioflocculation plug flow tank to detect the components and the concentration; the water quality change condition of the folded plate anaerobic biological flocculation plug flow tank is monitored by regularly collecting a part of liquid from the liquid sampling port;
in the step (5), the nuclear crystallization reaction time is 6-12h (namely, the hydraulic retention time can be 6-12 h);
in the step (6), the hydraulic retention time in the dynamic ultrafiltration membrane reaction tank can be 3-6 h;
the lateral microporous aeration heads perform primary aeration back washing on the ultrafiltration membrane of the dynamic ultrafiltration membrane reaction tank at intervals of 3-6h, wherein the aeration time is 10-30 min;
in the step (7), the hydraulic retention time of the aeration-nanofiltration bifunctional reaction tank is 3-6 h.
The invention has the following advantages:
(1) the U-shaped tubular hydrothermal reactor can greatly reduce the TS content of the wastewater, effectively kill pathogenic bacteria, pathogenic insect eggs and other harmful substances, decompose partial organic matters and shorten the subsequent anaerobic acid production time; although the TP content was unchanged, the IP content increased to 95-100% of TP. In addition, in the cooling process of the wastewater in the U-shaped tubular hydrothermal reactor, partial volatilized ammonia gas is introduced into the inclined plate aeration crystallization tank by virtue of internal pressure, so that the risk of secondary environmental problems caused by volatilization of ammonia gas into air is reduced, the concentration of ammonia nitrogen in the inclined plate aeration crystallization tank is increased, and the subsequent crystallization reaction is facilitated.
(2) The arrangement of the high-temperature resistant pipe between the U-shaped tubular hydrothermal reactor and the folded plate anaerobic biological flocculation plug flow tank not only plays a role in cooling wastewater, but also plays a role in preserving heat of the folded plate anaerobic biological flocculation plug flow tank, so that the anaerobic reaction is maintained in an optimal state of 30-50 ℃, the heat energy is effectively utilized, the anaerobic reaction time is shortened, and the methane production rate is accelerated.
(3) The biological flocculant in the folded plate anaerobic biological flocculation plug flow tank reduces the TS of the wastewater by 80-95 percent, shortens the anaerobic reaction time by 30-50 percent, and ensures that the COD value of the effluent of the supernatant is less than or equal to 1500 mg/L and less than or equal to 600 mg/L.
(4) The inclined plate aeration crystallization tank effectively reduces the content of nitrogen and phosphorus while further reducing the content of TS, generates struvite crystals at the same time, can be reused as a phosphorite substitute or a slow-control fertilizer, and has a supernatant effluent COD value of less than or equal to 500 mg/L and less than or equal to 300 mg/L, ammonia nitrogen of less than or equal to 400 mg/L and total phosphorus of less than or equal to 20 mg/L.
(5) The dynamic ultrafiltration membrane reaction tank has aerobic reaction and ultrafiltration functions, can further improve the effluent quality, the COD value of the supernatant effluent is less than or equal to 200 mg/L and less than or equal to 150 mg/L, the ammonia nitrogen is less than or equal to 200 mg/L, and the total phosphorus is less than or equal to 10 mg/L.
(6) The aeration-nanofiltration dual-function membrane reaction tank further improves the effluent quality to reach the reclaimed water standard of agriculture, forestry and animal husbandry in the reclaimed water quality standard (S L368 and 2006), the COD value of the effluent of the supernatant is more than or equal to 80 mg/L and less than or equal to 30 mg/L, the ammonia nitrogen is more than or equal to 20 mg/L, and the total phosphorus is more than or equal to 0.5 mg/L.
(7) 80-90% of water in the water collecting sedimentation tank is recycled for the farm, and 10-20% of sediment sedimentation part can flow back to the first anaerobic chamber of the folded plate anaerobic bioflocculation plug flow tank to adjust water conservancy conditions.
(8) The mud from the mud discharge pipe can be used for producing solid organic fertilizer after being treated by a dewatering device.
(9) The whole process of the integrated reaction device for treating the aquaculture wastewater can be automatically controlled by a sensor, the operation and the maintenance are convenient, the treatment efficiency and the effluent quality are not influenced by low temperature, and the recycling standard can be reached; the device is integrated, the occupied area is small, the integral movement is easy, and the device can be repeatedly installed and used for many times; changing waste into valuables to the maximum extent, realizing zero discharge of waste water, resource utilization and energy utilization.
Drawings
FIG. 1 is a top view of the integrated aquaculture wastewater treatment apparatus of the present invention.
FIG. 2 is a sectional view A-A of the integrated apparatus for treating aquaculture wastewater according to the present invention.
FIG. 3 is a sectional view B-B of the integrated apparatus for treating aquaculture wastewater according to the present invention.
FIG. 4 is a bottom view of the integrated device for treating aquaculture wastewater.
The respective symbols in the figure are as follows:
1U-shaped tubular hydrothermal reactor; 2, high temperature resistant pipe; 3, a folded plate anaerobic biological flocculation plug flow tank; 4, an inclined plate aeration crystallization tank; 5, a dynamic ultrafiltration membrane reaction tank; 6, an aeration-nanofiltration difunctional membrane reaction tank; 7, a water collecting sedimentation tank; 8, a culture wastewater storage tank; the normal pressure cooling inner container of the 9U-shaped tubular hydrothermal reactor; 10 an ammonia gas delivery pipe; 11, a first anaerobic chamber of a folded plate anaerobic bioflocculation plug flow tank; 12 an air collection port; 13 a partition plate; a second anaerobic chamber of the 14 folded plate anaerobic bioflocculation plug flow tank; a third anaerobic chamber of the 15 folded plate anaerobic bioflocculation plug flow tank; a fourth anaerobic chamber of the 16 folded plate anaerobic bioflocculation plug flow tank; 17 a liquid sampling port; 18 a bioflocculant; 19 a first sludge discharge port; 20 an anaerobic reflux pipe; 21 a waste water lift pump; 22 aeration-nanofiltration dual-function adjusting valve; 23 a lift pump; 24 side microporous aeration heads; 25 a seed crystal suspension crystallization chamber of the inclined plate aeration crystallization tank; 26 a pre-aeration settling chamber of the inclined plate aeration crystallization tank; 27 aeration air inlet pipe; 28 pipe type microporous aeration heads; 29 a sloping plate; 30 disc type microporous aeration heads; 31 ultrafiltration membrane; 32 an aerobic reflux pipe; 33 a nanofiltration membrane; 34 water outlet; 35 a wastewater sample inlet pipe; 36. 37 a pressure valve; a second sludge discharge port 38; 39 sludge discharge port III; a fourth sludge discharge port 40; a fifth sludge discharge port 41; and a sludge discharge port (VI) of 42.
Detailed Description
The present invention is further described with reference to the following drawings, but the present invention is not limited to the following embodiments, and those skilled in the art can modify the following embodiments or substitute the equivalent technical features of the above embodiments without departing from the spirit of the present invention. Such modifications and equivalents are intended to be included within the scope of the claims appended hereto.
Embodiment 1 Integrated device for treating aquaculture wastewater
As shown in FIG. 1, the integrated device for treating aquaculture wastewater comprises: the device comprises a U-shaped tubular hydrothermal reactor 1, a high-temperature resistant pipe 2, a folded plate anaerobic bioflocculation plug flow tank 3, an inclined plate aeration crystallization tank 4, a dynamic ultrafiltration membrane reaction tank 5, an aeration-nanofiltration bifunctional membrane reaction tank 6, a catchment sedimentation tank 7 and a culture wastewater storage tank 8.
As shown in fig. 3, when the reaction starts, firstly, the cultivation wastewater is introduced into the cultivation wastewater reservoir 8, the pressure valve 36 between the heating liner and the normal pressure cooling liner 9 in the U-shaped tubular hydrothermal reactor 1 is closed, then the cultivation wastewater is pumped into the U-shaped tubular hydrothermal reactor 1 from the cultivation wastewater reservoir 8 through the wastewater inlet pipe 35 by using the wastewater lift pump 21, when the liquid level sensor of the heating liner detects that the liquid level is 70% of the total liner height, the wastewater lift pump 21 stops working, the redundant wastewater in the wastewater inlet pipe 35 flows back to the cultivation wastewater reservoir 8, and the pressure valve 37 between the injection port and the heating liner is closed, so that the liner is in a sealed state; the heating temperature of the inner container is controlled to be 110-.
After hydrothermal reaction, a pressure valve 36 between a heating inner container and an atmospheric cooling inner container 9 is opened, so that a sample automatically flows into the atmospheric cooling inner container 9 by utilizing a U-shaped pipe principle, an ammonia gas conveying pipe 10 is opened by the atmospheric cooling inner container, pressure is released, meanwhile, gas containing ammonia gas is introduced into a pre-aeration settling chamber 26 of an inclined plate aeration crystallization tank 4, ammonia nitrogen concentration is increased, so that subsequent crystallization reaction is facilitated, then, a pressure valve 37 between the heating inner container and a sample inlet is also opened, a wastewater lifting pump 21 of a culture wastewater storage tank 8 is opened again for sample injection until the liquid level heights of the two inner containers are 70% of the total inner container height, valves at two ends of the heating inner container are closed, the heating inner container starts heating again, the retention time of wastewater in the atmospheric cooling inner container 9 is the same as that the wastewater in the closed heating inner container, the temperature is reduced to 70-90 ℃, the wastewater flows through a high temperature resistant pipe 2 at the flow rate of 0.5-1.0. 1.0L/h, the flow direction of the wastewater in a high temperature resistant pipe 2 is as shown in a first anaerobic bio-flocculation chamber (shown in a first drawing 2) which is shown in a high temperature resistant anaerobic flocculation chamber 3.
As shown in figure 2, after wastewater firstly flows through a downstream chamber of a first anaerobic chamber 11, the wastewater flows into an upstream chamber of the first anaerobic chamber 11 from a folded plate, a large amount of flocs are generated and precipitated under the action of a bioflocculant 18, supernatant flows into a second anaerobic chamber 14 without a partition plate 13, anaerobic sludge in the anaerobic chambers continuously decomposes organic matters to generate biogas, the biogas is collected to a gas collection device through a gas collection port 12, the supernatant flows to a fourth anaerobic chamber 16 through a third anaerobic chamber 15, and then flows into a pre-aeration precipitation chamber 26 of an inclined plate aeration crystallization tank 4 through an overflow weir, the COD value of the supernatant is less than or equal to 1500 mg/L and less than or equal to 600 mg/L, the retention time of the liquid in the folded plate anaerobic bioflocculation plug flow tank 3 is 48-96h, sludge at the bottom of the anaerobic chamber flows back to the first anaerobic biological flocculation chamber 11 through an anaerobic return pipe 20 during the period, the return ratio can be 15-30%, primary discharge can be carried out through a discharge port (one) 19 at intervals, the sludge sampling port 17 of the anaerobic biological flocculation plug flow tank 3 can be used for monitoring the change of wastewater, and the liquid collection condition can be carried out through a sampling tank 17.
As shown in figure 3, a tubular microporous aeration head 28 in a pre-aeration settling chamber 26 in an inclined plate aeration crystallization tank 4 is communicated with air through an aeration air inlet pipe 27, the indoor wastewater is aerated to accelerate the sedimentation of suspended matters, after the wastewater enters a seed crystal suspension crystallization chamber 25 from the lower part through a porous plate channel, a magnesium agent solution and a pH value regulating agent are added to enable the wastewater to generate a nucleation crystallization reaction in an intermediate aeration stirring zone, the hydraulic retention time can be 6-12h, generated large-particle phosphorus crystals settle in a crystal mud storage zone, small-particle crystals flow into an upper inclined plate 29 along with water flow, and fall back to the aeration stirring zone after being blocked by the inclined plate 29 to continue to grow together as seed crystals, the large-particle phosphorus crystals are generated and then settled in a crystal mud storage zone, supernatant flows into a dynamic ultrafiltration membrane tank 5 from top to bottom, 10-20% of crystal mud in the crystal mud storage zone flows back to the pre-aeration settling chamber 26 through an aerobic return pipe 32, the rest of crystal mud can be collected once through a mud discharge port 6348-96 h at an interval, the sludge discharge port 3548-96 h, and the COD value of the supernatant is equal to or less than or equal to 500 mg/L mg of the supernatant of the sludge in the pre-48 mg aeration settling chamber 26, and is equal to or less than or equal to or.
As shown in figure 3, the supernatant stays in the dynamic ultrafiltration membrane reaction tank 5 for 3-6h, the lift pump 23 is started, the wastewater flows to the aeration-nanofiltration dual-function membrane reaction tank 6 from bottom to top through the ultrafiltration membrane 31 to realize further water quality lifting, the disc type microporous aeration head 30 is always started during the period, oxygen is provided for microorganisms on the ultrafiltration membrane, a certain membrane flushing effect is achieved, the side microporous aeration heads 24 on the side face are aerated for 10-30min at intervals of 3-6h to achieve the effect of flushing the membrane in a large area so as to ensure stable membrane flux, 10-20% of sludge on the bottom of the tank flows back to the pre-aeration settling chamber 26 through the aerobic return pipe 32, and the rest sludge can be discharged for one time through the sludge discharge port (IV) 38 at intervals of 4-7 days, wherein the COD value of the effluent at the moment is not more than 200 mg/L and not more than 150 mg/L, the ammonia nitrogen is not more than 200 mg/L, and the total phosphorus is.
As shown in figure 3, the liquid after ultrafiltration stays in an aeration-nanofiltration dual-function membrane reaction tank 6 for 3-6 hours at an interval of 1-2 hours, the function of exchanging two sets of nanofiltration membranes 33 through an adjusting aeration-nanofiltration dual-function adjusting valve 22 is adjusted, the liquid flows into a final water-collecting sedimentation tank 7 through a nanofiltration functional membrane module, 10-20% of sludge at the bottom of the tank flows back to a pre-aeration sedimentation chamber 26 through an aerobic return pipe 32, the rest sludge can be discharged once through a sludge discharge port (V) 41 at an interval of 4-7 days, the COD value of the effluent in the final water-collecting sedimentation tank 7 is not less than 80 mg/L and not more than 30 mg/L, the ammonia nitrogen is not more than 20 mg/L, and the total phosphorus is not more than 0.5 mg/L, and the effluent quality basically can reach the ' reclaimed water standard for agricultural, forestry and animal husbandry ' in the reclaimed water quality standard (S L368 and 2006) ' and can flow out from a water outlet 34 and be used in a.
As shown in figure 4, 10-20% of sludge at the bottom of the water collecting sedimentation tank 7 flows back to the first anaerobic chamber 11 of the folded plate anaerobic biological flocculation plug flow tank 3 through the anaerobic return pipe 20, and the rest sludge can be discharged once through a sludge discharge port (VI) 42 at intervals of 7-14 days.
Example 2 use of Integrated apparatus for treatment of wastewater from farming- -recovery of wastewater resources and energy resources
The method comprises the steps of pouring aquaculture wastewater with the pH value of 6.4, the COD value of 6400 mg/L of 7700 mg/L, the ammonia nitrogen concentration of 675 mg/L0, the total phosphorus concentration of 137 mg/L and the solid content of 9% into a aquaculture wastewater storage tank 8, controlling the heating temperature of a U-shaped tubular hydrothermal reactor 1 to be 110 ℃ and the reaction pressure to be 2.0MPa through the embodiment, after heating for 30min, opening a pressure valve 36 between a heating liner and a normal-pressure cooling liner 9, enabling a sample to automatically flow into a normal-pressure cooling liner 9 by utilizing the principle of a U-shaped pipe, opening an ammonia gas conveying pipe 10, introducing gas containing ammonia into a pre-aeration settling chamber 26 of an inclined plate aeration crystallization tank 4, increasing the ammonia nitrogen concentration by 9.5%, then opening a pressure valve 37 between the heating liner and an injection port, starting a wastewater lifting pump 21 of the aquaculture wastewater storage tank 8 again to inject the sample until the liquid level of the two liners is 70% of the total liner height, closing valves at the two ends of the total liner, heating, restarting the heating liner, cooling the liner 9, after the wastewater in the liner 9-pressure valve is treated, the wastewater enters a wastewater collection tank 8, the anaerobic wastewater collection tank, the anaerobic wastewater collection wastewater from a high-anaerobic aerobic aeration tank 20 anaerobic flocculation tank through an inclined plate 20-6 anaerobic flocculation aeration tank 20-20 anaerobic flocculation aeration tank 8, a high-6 anaerobic flocculation aeration tank 26, a high-20 anaerobic flocculation aeration tank 8, a high-20 anaerobic flocculation sewage collection wastewater.
EXAMPLE 3 use of Integrated apparatus for treatment of wastewater from farming- -recovery of wastewater resources and energy resources
The method comprises the steps of pouring aquaculture wastewater with the pH value of 6.2, the COD value of 10900 mg/L of 11850 mg/L, the ammonia nitrogen concentration of 758 mg/L0, the total phosphorus concentration of 163 mg/L and the solid content of 9% into a aquaculture wastewater storage tank 8, controlling the heating temperature of a U-shaped tubular hydrothermal reactor 1 to 120 ℃ and the reaction pressure of 2.5MPa through the above embodiment, after heating for 50min, automatically flowing the wastewater into a normal-pressure cooling liner 9 by utilizing the principle of a U-shaped pipe, opening an ammonia gas conveying pipe 10 of the cooling liner, introducing gas containing ammonia gas into a pre-aeration settling chamber 26 of an inclined plate aeration crystallization tank 4, increasing the ammonia nitrogen concentration by 12%, then heating the liner for re-injection, restarting heating the wastewater in an atmospheric cooling liner 9 for 50min, cooling to 70 ℃, flowing the wastewater into an anaerobic bioflocculation push tank 3 through a high-temperature resistant pipe 2 at the flow rate of 1.0. L/h to a folded plate biological flocculation sewage tank 3, throwing 50m L bioflocculation wastewater in an anaerobic biological flocculation push-flow pond 3, throwing 18, throwing in an anaerobic biological flocculation sewage collection tank 3, collecting sewage slurry from a sewage collection tank 7, collecting sewage collection tank 20, a sewage collection tank 20, collecting sewage collection tank 20, a sewage collection tank 8, a sewage collection tank, a sewage.
EXAMPLE 4 use of Integrated apparatus for treatment of wastewater from farming- -recovery of wastewater resources and energy resources
The method comprises the steps of pouring aquaculture wastewater with the pH value of 6.3, the COD value of 9500 mg/L of 10160 mg/L, the ammonia nitrogen concentration of 737 mg/L0, the total phosphorus concentration of 141 mg/L and the solid content of 8% into a aquaculture wastewater storage tank 8, controlling the heating temperature of a U-shaped tubular hydrothermal reactor 1 to 130 ℃ and the reaction pressure of 2.5MPa through the embodiment, after heating for 40min, automatically flowing the wastewater into a normal-pressure cooling liner 9 by utilizing the principle of a U-shaped pipe, opening an ammonia gas conveying pipe 10 of the cooling liner, introducing gas containing ammonia gas into a pre-aeration settling chamber 26 of an inclined plate aeration crystallization tank 4, increasing the ammonia nitrogen concentration by 14.5%, then heating the liner for re-sampling, restarting heating, cooling the wastewater in the liner 9 for 40min after standing for 40min, cooling to 85 ℃, flowing the wastewater into a gas collecting pipe 2 to a sewage tank 3 through a gas collecting pipe 3 at the flow rate of 0.6/L/h to a sewage collecting sewage from a sewage collecting tank 3m L, a sewage collecting sewage from a sewage collecting tank 3, a sewage collecting sewage, a sewage collecting tank, a sewage collecting tank, a sewage collecting tank.
EXAMPLE 5 use of Integrated apparatus for treatment of wastewater from farming- -recovery of wastewater resources and energy resources
The method comprises the steps of pouring aquaculture wastewater with the pH value of 6.6, the COD value of 4800 mg/L of 5850 mg/L, the ammonia nitrogen concentration of 608 mg/L0, the total phosphorus concentration of 117 mg/L and the solid content of 8% into a aquaculture wastewater storage tank 8, controlling the heating temperature of a U-shaped tubular hydrothermal reactor 1 to 140 ℃ and the reaction pressure of 3.0MPa through the above embodiment, after heating for 40min, automatically flowing the wastewater into a normal-pressure cooling liner 9 by utilizing the principle of a U-shaped pipe, opening an ammonia gas conveying pipe 10 of the cooling liner, introducing gas containing ammonia gas into a pre-aeration settling chamber 26 of an inclined plate aeration crystallization tank 4, increasing the ammonia nitrogen concentration by 11%, heating again the ammonia nitrogen concentration, cooling to 90 ℃ after the wastewater in the normal-pressure cooling liner 9 stays for 40min, flowing the wastewater into a folded plate anaerobic bioflocculation plug flow tank 3 by a high-temperature resistant pipe 2 at the flow rate of 0.5L/h, feeding 18 of 20m L biological flocculant in per liter wastewater in an anaerobic biological flocculation plug flow basin 3, feeding the biological flocculant for 48h, collecting sewage from a sewage collection tank of a sewage collection tank 7 to a secondary anaerobic biological flocculation sedimentation tank, collecting sewage collection tank, collecting sewage from a primary sewage collection tank 7, a primary aeration tank 7, a primary sewage collection tank 7, a primary aeration tank 23-6-19 h, a primary sewage collection tank, a primary aeration tank for a secondary aerobic membrane aeration tank with a sewage sedimentation tank 23-19 h interval of a primary aeration tank 23-19 h, a secondary anaerobic biological flocculation sewage sedimentation tank, a secondary anaerobic biological flocculation sewage collection tank, a secondary aerobic membrane aeration sedimentation tank 23-19 h, a secondary aerobic membrane sedimentation tank 23-19 h, a secondary anaerobic biological flocculation sewage collection tank with a secondary anaerobic biological flocculation sewage collection tank 23-19 h interval, a secondary anaerobic biological flocculation sewage collection tank with a constant aeration tank 7 sewage flow interval, a constant.

Claims (10)

1. The utility model provides an integrated device of aquaculture wastewater treatment which characterized in that: the device comprises a culture wastewater storage tank, a U-shaped tubular hydrothermal reactor, a folded plate anaerobic bioflocculation plug flow tank, an inclined plate aeration crystallization tank, a dynamic ultrafiltration membrane reaction tank, an aeration-nanofiltration bifunctional membrane reaction tank and a water collection sedimentation tank;
the sample inlet of the U-shaped tubular hydrothermal reactor is connected with the sample outlet of the culture wastewater reservoir;
the sample outlet of the U-shaped tubular hydrothermal reactor is connected with the sample inlet of the folded plate anaerobic biological flocculation plug flow pool;
the sample outlet of the folded plate anaerobic biological flocculation plug flow tank is connected with the sample inlet of the inclined plate aeration crystallization tank;
the sample outlet of the inclined plate aeration crystallization tank is connected with the sample inlet of the dynamic ultrafiltration membrane reaction tank;
the sample outlet of the dynamic ultrafiltration membrane reaction tank is connected with the sample inlet of the aeration-nanofiltration dual-function membrane reaction tank;
a sample outlet of the aeration-nanofiltration bifunctional membrane reaction tank is connected with the water-collecting sedimentation tank;
the integrated device for treating the breeding wastewater adopts a container type;
one side of the U-shaped tubular hydrothermal reactor is provided with a sample inlet and a closed heating inner container, and the other side of the U-shaped tubular hydrothermal reactor is provided with a sample outlet and a normal-pressure cooling inner container;
pressure valves are respectively arranged between the sample inlet of the U-shaped tubular hydrothermal reactor and the closed heating inner container and between the closed heating inner container and the normal-pressure cooling inner container;
the closed heating inner container and the normal pressure cooling inner container are respectively provided with a sampling port, a pressure gauge and a temperature sensor; the normal pressure cooling liner is also provided with an air outlet pipe which is communicated with the inclined plate aeration crystallization tank;
and a sample outlet of the U-shaped tubular hydrothermal reactor is communicated with a sample inlet of the folded plate anaerobic biological flocculation plug flow pool by adopting a high-temperature resistant tube.
2. The integrated device of claim 1, wherein: the U-shaped tubular hydrothermal reactor is cast by steel materials, the length ratio of the outer diameter of the tube to the inner diameter of the tube of the U-shaped tubular hydrothermal reactor is 1.5-2: 1, and the length ratio of the inner diameter of the tube to the length of the tube is 1: 3-5.
3. The integrated device of claim 1 or 2, wherein: the high-temperature resistant pipe is arranged at the bottom of the folded plate anaerobic biological flocculation plug flow tank;
the high-temperature resistant pipe is made of tripropylene polyethylene.
4. The integrated device of claim 1 or 2, wherein: the integrated device also comprises a gas collecting device and a sludge dewatering device;
the folded plate anaerobic biological flocculation plug flow pool comprises 3-5 anaerobic chambers which are communicated, each anaerobic chamber comprises a downstream chamber and an upstream chamber, and the downstream chamber and the upstream chamber are divided by folded plate semi-closed; the top end of the folded plate is vertically connected with the inner wall of the top end of the folded plate anaerobic bioflocculation plug flow tank; the lower end inclination angle of the folded plate is 30-60 degrees, and the direction of the folded plate is inclined from the upstream chamber to the downstream chamber; the height from the lower end of the folded plate to the bottom of the folded plate anaerobic bioflocculation plug flow pool is 10% -30% of the height of the bottom of the folded plate anaerobic bioflocculation plug flow pool;
the volume ratio of the downstream chamber to the upstream chamber is 1: 4;
the volume of the anaerobic chamber arranged from the sample inlet of the folded plate anaerobic biological flocculation plug flow pool to the sample outlet thereof is sequentially increased, and the vertical height of the water inlet level of the anaerobic chamber is in a decreasing state; the top of the anaerobic chamber is provided with an air outlet, and the air outlet of the anaerobic chamber is communicated with the gas collecting device;
3 equidistant liquid sampling ports are respectively and vertically arranged on the outer wall of the anaerobic chamber; the bottom of the anaerobic chamber of the folded plate anaerobic biological flocculation plug flow tank is provided with a sludge discharge port I, and the sludge discharge port I is communicated with a sample inlet of the sludge dewatering device; return pipes are arranged on the side surface of the sludge discharge port (one) from the sample outlet to the sample inlet of the folded plate anaerobic biological flocculation plug flow pool; the anaerobic chamber at the water inlet of the folded plate anaerobic bioflocculation plug flow tank is called as a first anaerobic chamber.
5. The integrated device of claim 4, wherein: the inclined plate aeration crystallization tank is divided into a pre-aeration settling chamber and a seed crystal suspension crystallization chamber in a semi-closed manner by a water seepage plate, and the pre-aeration settling chamber is communicated with the seed crystal suspension crystallization chamber; the volume ratio of the pre-aeration settling chamber to the seed crystal suspension crystallization chamber is 1: 3-5; the water inlet of the pre-aeration settling chamber is communicated with the water outlet of the folded plate anaerobic bio-flocculation plug flow tank; the water inlet of the seed crystal suspension crystallization chamber is communicated with the water outlet of the pre-aeration settling chamber through a pore passage at the lower part of the water seepage plate;
the vertical height of the water inlet level of the pre-aeration settling chamber is 5-10% lower than that of the water outlet level of the folded plate anaerobic bio-flocculation plug flow tank;
the crystal seed suspension crystallization chamber comprises an upper inclined plate separation area, a middle aeration stirring area and a lower crystal mud storage area; the inclined angle of the inclined plate of the upper inclined plate separation area is 10-15 degrees, and the inclined direction of the inclined plate is opposite to the water flow direction in use; the volume of the upper inclined plate separation area accounts for 1/4-1/3 of the seed crystal suspension crystallization chamber;
the inclined plate aeration crystallization tank adopts tubular microporous aeration as an aeration head, and the height of the aeration head which is 10-15% of the height of the bottom of the inclined plate aeration crystallization tank is uniformly and horizontally distributed at the bottom of the tank; the pipe diameter ratio of the branch pipe to the main pipe of the tubular microporous aeration head is 1: 1.5-2; the coverage rate of the micropores is 20% -60%;
the bottoms of the pre-aeration settling chamber and the seed crystal suspension type crystallization chamber are respectively provided with a sludge discharge port (II) and a sludge discharge port (III), and the sludge discharge port (II) and the sludge discharge port (III) are both connected with a sample inlet of the sludge dewatering device; an aerobic reflux pipe is arranged from the seed crystal suspension type crystallization chamber to the pre-aeration settling chamber and is driven by a reflux pump, and partial crystal mud is refluxed by the reflux pump.
6. The integrated device of claim 5, wherein: the dynamic ultrafiltration membrane reaction tank comprises at least 1 group of flat plate type membrane assemblies, and each group of the membrane assemblies is formed by pressing 5-100 membrane sheets; the membrane material adopts non-woven fabrics and/or a screen; the spinning density of the membrane component is 20-40 g/m2The membrane flux is 40-100L/(m)2H), the operating pressure is 0.3-0.5 MPa;
a pressure gauge is arranged at the upper end of the membrane component to observe pressure intensity;
the vertical height of the water inlet level of the pre-aeration settling chamber is 5-10% lower than that of the water outlet level of the folded plate anaerobic bio-flocculation plug flow tank;
the vertical height of the water inlet level of the dynamic ultrafiltration membrane reaction tank is 5-10% lower than that of the water outlet level of the pre-aeration settling chamber;
the bottom of the dynamic ultrafiltration membrane reaction tank is provided with a disc microporous aeration head which is 10-15% of the height away from the bottom of the dynamic ultrafiltration membrane reaction tank; the two sides of the membrane component are provided with lateral microporous aeration heads, the aeration mode is intermittent aeration, the aeration interval is 3-6h, and the aeration time is 10-30 min;
a sludge discharge port (IV) is formed in the bottom of the dynamic ultrafiltration membrane reaction tank and is connected with a sample inlet of the sludge dewatering device;
an aerobic return pipe is arranged from the dynamic ultrafiltration membrane reaction tank to the inclined plate aeration crystallization tank, is driven by a return pump, and returns partial sludge by the return pump.
7. The integrated device of claim 6, wherein the aeration-nanofiltration bifunctional membrane reaction tank comprises two sets of flat-plate membrane components, each set of flat-plate membrane component comprises at least 1 set of membrane components, each set of flat-plate membrane component comprises 5-20 membrane sheets, the membrane sheets are made of hollow fibers, the membrane aperture of each flat-plate membrane component is 1-2 nm, and the membrane flux is 10-30L/(m)2·h)；
A sludge discharge port (V) is formed in the bottom of the aeration-nanofiltration dual-function membrane reaction tank and is connected with a sample inlet of the sludge dewatering device;
an aerobic reflux pipe is arranged from the aeration-nanofiltration difunctional membrane reaction tank to the inclined plate aeration crystallization tank, and the reflux proportion is 10-20%.
8. The integrated device of claim 6, wherein: the bottom of the water collecting sedimentation tank is provided with a sludge discharge port (VI), and the sludge discharge port (VI) is communicated with a sample inlet of the sludge dewatering device;
an anaerobic return pipe is arranged from the water collecting sedimentation tank to a first anaerobic chamber of the folded plate anaerobic biological flocculation plug flow tank, the return ratio is 10-20%, and 80-90% of the regenerated water in the water collecting sedimentation tank is used for circulating water of a farm.
9. A method for treating aquaculture wastewater using an integrated aquaculture wastewater treatment plant according to any one of claims 6 to 8, comprising the steps of:
(1) introducing culture wastewater into the culture wastewater storage tank, closing the pressure valve between the closed heating inner container and the normal-pressure cooling inner container in the U-shaped tubular hydrothermal reactor, pumping the culture wastewater into the U-shaped tubular hydrothermal reactor from the culture wastewater storage tank through a sample inlet pipe by using a lift pump, stopping the work of the lift pump when a liquid level sensor of the closed heating inner container monitors that the liquid level is 70% of the total inner container height, refluxing redundant wastewater in the sample inlet pipe to the culture wastewater storage tank, and closing the pressure valve between the sample inlet and the closed heating inner container to enable the closed heating inner container to be in a sealed state; controlling the closed heating liner to perform heating reaction;
(2) after the aquaculture wastewater in the step (1) completes hydrothermal reaction, opening the pressure valve between the closed heating liner and the normal-pressure cooling liner to enable the sample to automatically flow into the normal-pressure cooling liner by utilizing the principle of a U-shaped pipe; opening a valve of an ammonia gas delivery pipe by the cooling liner, releasing pressure, and introducing gas containing ammonia gas into the inclined plate aeration crystallization tank to increase the ammonia nitrogen concentration; then, opening the pressure valve between the sealed heating liner and the sample inlet, opening a lifting pump of the culture wastewater reservoir again for sample injection until the liquid level heights of the sealed heating liner and the normal-pressure cooling liner are both 70% of the heights of the liners, closing valves at two ends of the sealed heating liner, and repeating the step (1) to perform heating reaction on the sealed heating liner; controlling the pressure of the wastewater of the sample outlet pipe to return to normal atmospheric pressure, wherein the temperature is 70-90 ℃;
(3) the culture wastewater treated in the step (2) flows to the high-temperature resistant pipe from the normal-pressure cooling liner through a lift pump;
(4) the aquaculture wastewater treated in the step (3) flows into the upper part of the side surface of the folded plate anaerobic biological flocculation plug flow tank from a high-temperature-resistant pipe through a lifting pump, and after the flocculation and precipitation are strengthened by a biological flocculant in the first anaerobic chamber, the supernatant gradually flows through the rest anaerobic chambers of the folded plate anaerobic biological flocculation plug flow tank;
(5) enabling the supernatant of the folded plate anaerobic bioflocculation plug flow tank in the step (4) to flow into the pre-aeration settling chamber of the inclined plate aeration crystallization tank from top to bottom; then the magnesium agent solution and the pH value regulating agent are added after entering the seed crystal suspension crystallization chamber from the lower part of the pre-aeration settling chamber through a porous plate channel, and a nucleation crystallization reaction is carried out in an intermediate aeration stirring area; large granular phosphorus crystals are precipitated into the lower crystal mud storage area, small granular crystals enter the upper inclined plate separation area along with water flow, fall back to the middle aeration stirring area after encountering the obstruction of the upper inclined plate separation area, continue to grow by polymerization as crystal seeds, generate large granular phosphorus grains and then precipitate into the lower crystal mud storage area, and 10-20% of crystal mud in the lower crystal mud storage area flows back to the pre-aeration precipitation chamber;
(6) enabling the overflow liquid in the step (5) to flow into the dynamic ultrafiltration membrane reaction tank from top to bottom to further reduce the concentration of nitrogen and phosphorus in water; opening a lift pump, and allowing overflow liquid to flow to the aeration-nanofiltration dual-function membrane reaction tank from bottom to top through an ultrafiltration membrane of the dynamic ultrafiltration membrane reaction tank; 10-20% of sludge at the bottom of the tank flows back to the inclined plate aeration crystallization tank;
(7) enabling the filtrate in the step (6) to flow into the aeration-nanofiltration dual-function reaction tank from top to bottom; exchanging the functions of the two sets of nanofiltration membranes by adjusting the aeration-nanofiltration dual-function adjusting valve at intervals of 1-2 h; 10-20% of sludge at the bottom of the tank flows back to the inclined plate aeration crystallization tank;
(8) and (3) enabling the filtrate in the step (7) to flow into the water collecting sedimentation tank from top to bottom, enabling 80-90% of regenerated water to flow out of a water outlet and be used for circulating water of a farm, and enabling 10-20% of sludge at the bottom of the tank to flow back to the first anaerobic chamber of the folded plate anaerobic biological flocculation plug flow tank through an anaerobic return pipe to be continuously treated.
10. The method of claim 9, wherein: in the step (1), the heating temperature of the sealed heating inner container is controlled to be 110-150 ℃, the heating time is 20-60min, and the reaction pressure is 2.0-5.0 Mpa;
in the step (3), the flow rate of the treated wastewater flowing to the high-temperature resistant pipe is controlled to be 0.5-1.0L/h by using a flow meter, and the retention time in the pipe is 20-60 min;
the temperature of the outlet water flowing into the folded plate anaerobic biological flocculation plug flow tank from the high temperature resistant pipe is 30-50 ℃;
the step (4) also comprises that the wastewater inflow flow rate of the folded plate anaerobic biological flocculation plug flow pool is 0.5-1.0L/h, sludge at the bottoms of several anaerobic chambers behind the first anaerobic chamber is forced to flow back to the first anaerobic chamber, the sludge backflow proportion is 15-30%, and the retention time in the folded plate anaerobic biological flocculation plug flow pool is 48-96 h;
collecting partial gas from a gas collection port by using biogas generated in the folded plate anaerobic bioflocculation plug flow tank to detect the components and the concentration; the water quality change condition of the folded plate anaerobic biological flocculation plug flow tank is monitored by regularly collecting a part of liquid from the liquid sampling port;
in the step (5), the time of the nuclear crystallization reaction is 6-12 h;
in the step (6), the hydraulic retention time in the dynamic ultrafiltration membrane reaction tank is 3-6 h;
the lateral microporous aeration heads perform primary aeration back washing on the ultrafiltration membrane of the dynamic ultrafiltration membrane reaction tank at intervals of 3-6h, wherein the aeration time is 10-30 min;
in the step (7), the hydraulic retention time of the aeration-nanofiltration bifunctional reaction tank is 3-6 h.
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