CN210683538U - System for be used for maize starch waste water resourceization - Google Patents
System for be used for maize starch waste water resourceization Download PDFInfo
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- CN210683538U CN210683538U CN201921745862.1U CN201921745862U CN210683538U CN 210683538 U CN210683538 U CN 210683538U CN 201921745862 U CN201921745862 U CN 201921745862U CN 210683538 U CN210683538 U CN 210683538U
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Abstract
The utility model discloses a system for corn starch waste water resourceization, the system is including the catch basin, the grit chamber, the reactor, the former feed liquid accumulator, draw the liquid accumulator, just permeate the membrane module, the thick water pond, the fresh water pond, reverse osmosis membrane module and sedimentation tank, wherein the catch basin is linked together with corn starch manufacturing enterprise's drainage pipe network, the catch basin is connected with the grit chamber through the pipeline, the grit chamber still is connected with the reactor through the pipeline, the reactor is connected with the former feed liquid accumulator through the pipeline, its method is: step 1, enabling the corn starch wastewater to enter a grit chamber; step 2, pumping the effluent of the grit chamber into a raw material liquid storage; step 3, pumping the inlet water in the raw material liquid storage into a sedimentation tank; step 4, realizing the reuse of water resources; step 5, realizing the complete recovery of resources; has the advantages that: the method still has the required sewage treatment effect under the conditions of simple flow, low energy consumption and less carbon emission. Realizes the complete recovery of water, carbon, nitrogen and phosphorus resources.
Description
Technical Field
The utility model relates to a system of waste water resourceization, in particular to a system for corn starch waste water resourceization.
Background
The corn starch wastewater has the characteristics of high COD (chemical oxygen demand), high SS (suspended solids), high TN (total transport potential), high TP (total transport pressure) and low pH (pH), and in order to meet the discharge requirements of the starch industrial water pollutant discharge standard (GB 25461-. Phosphorus is a non-renewable and irreplaceable strategic resource, is exhausted, mainly in the form of Phosphate (PO)4 3-，HPO4 2-，H2PO4 -) Are present. The recovery technology of phosphorus resources is various, and mainly comprises a chemical precipitation method, an enhanced biological phosphorus removal method and an adsorption method. The enhanced biological phosphorus removal method requires secondary treatment; the adsorption method has the advantages of simple process, reliable operation and the like, and additional desorption is needed if the phosphorus resource in the adsorbent is recovered.
Disclosure of Invention
The utility model discloses a main objective is in order to realize resources such as high-efficient recovery maize starch waste water normal water, carbon, nitrogen, phosphorus and heat energy and a system for maize starch waste water resourceization that provides.
The utility model provides a system for recycling corn starch wastewater, which comprises a water collecting tank, a grit chamber, a reactor, a raw material liquid storage, a drawing liquid storage, a forward osmosis membrane component, a concentrated water tank, a fresh water tank, a reverse osmosis membrane component and a sedimentation tank, wherein the water catch bowl is linked together with corn starch manufacturing enterprise's drainage pipe network, the water catch bowl is connected with the grit chamber through the pipeline, the grit chamber still is connected with the reactor through the pipeline, the reactor is connected with the raw material liquid accumulator through the pipeline, the reactor still is connected with the sedimentation tank through the pipeline, the raw material liquid accumulator also is connected with the sedimentation tank through the pipeline, the raw material liquid accumulator is connected through two pipelines with the liquid accumulator of drawing, the infiltration membrane subassembly assembly is on two connecting pipelines of raw material liquid accumulator and the liquid accumulator of drawing, the liquid accumulator of drawing still is connected with the dense water pond through the pipeline, the reverse osmosis membrane subassembly is established between dense water pond and fresh water pond.
Be provided with the grid in the catch basin and be used for holding back suspended solid and the floater in the sewage, be equipped with the sewage pump that the elevator pump was used for in the catch basin on the connecting line of catch basin and grit chamber and go into in the grit chamber, be equipped with first peristaltic pump and water source heat pump on the connecting line of grit chamber and reactor, the grit chamber is aeration grit chamber.
The reactor is an anaerobic membrane bioreactor, an ultrafiltration membrane component and an aeration stone are arranged in the reactor, and the effective area of an ultrafiltration membrane in the ultrafiltration membrane component is 0.1m2The size of the membrane is 320 multiplied by 220 multiplied by 5mm3The aperture of the membrane is 0.1 mu m, the surface of the ultrafiltration membrane component is aerated by biogas generated by anaerobic through an aeration pump by means of an aeration stone, a valve and a suction pump are assembled on a connecting pipeline between the reactor and the raw material liquid reservoir, and a sixth peristaltic pump is assembled on a connecting pipeline between the reactor and the sedimentation tank.
Be provided with conductivity meter and pH value tester in the former feed liquid accumulator, be equipped with the second peristaltic pump on the connecting line of former feed liquid accumulator and forward osmosis membrane subassembly, be equipped with the third peristaltic pump on the connecting line of forward osmosis membrane subassembly and draw liquid accumulator, be equipped with fourth peristaltic pump and water source heat pump on the connecting line of draw liquid accumulator and concentrated water pond, forward osmosis membrane subassembly comprises forward osmosis membrane and membrane piece, the effective area of forward osmosis membrane is 30cm2The depth of the flow channel is 2 mm.
The sedimentation tank is internally provided with a stirrer and a pH value tester.
The lifting pump, the first peristaltic pump, the water source heat pump, the aeration pump, the suction pump, the conductivity meter, the pH value tester, the second peristaltic pump, the third peristaltic pump, the fourth peristaltic pump, the water replenishing pump, the fifth peristaltic pump, the stirrer and the sixth peristaltic pump are all assembled on the existing equipment, and therefore specific models and specifications are not repeated.
The utility model provides a method for corn starch waste water resource, its method is as follows:
step 4, taking the inlet water in the concentrated water tank as concentrated water, taking the inlet water in the fresh water tank as fresh water, applying pressure on one side of the concentrated water tank to enable the water in the concentrated water tank to enter the fresh water tank through the reverse osmosis membrane assembly, concentrating the water in the concentrated water tank and then refluxing the concentrated water tank to the drawing liquid storage device, and directly recycling the water in the fresh water tank to realize the recycling of water resources;
and 5, regulating the conditions of the pH value and the nitrogen-magnesium-phosphorus ratio of the concentrated solution entering the sedimentation tank to generate struvite sediment in the sedimentation tank, recycling the struvite sediment as slow release fertilizer, and pumping the supernatant in the sedimentation tank into a reactor to realize the complete recovery of water, carbon, nitrogen, phosphorus and heat energy resources.
The grit chamber in step 1 is an aeration grit chamber.
The ultrafiltration membrane used in the ultrafiltration membrane component in the step 2 is a flat membrane, and the effective area of the single membrane is 0.1m2The size of the membrane is 320 multiplied by 220 multiplied by 5mm3The aperture of the membrane is 0.1 μm, the material of the membrane is polyvinylidene fluoride, and the material of the support plate is acrylonitrile-butadiene-styrene copolymer.
The forward osmosis membrane used in the forward osmosis membrane component in the step 3 belongs to an asymmetric membrane and consists of an active layer and a supporting layer, wherein the active layer is made of cellulose triacetate, the supporting layer is made of polyester, and the effective area of the forward osmosis membrane is 30cm2The depth of the flow channel is 2 mm.
The main supporting structure of the reverse osmosis membrane used by the reverse osmosis membrane component in the step 4 is polyester non-woven fabric which is calendered by a calender, the surface of the polyester non-woven fabric has no loose fibers and is hard and smooth, microporous engineering plastic polysulfone is poured on the surface of the non-woven fabric, the holes on the surface of the polysulfone layer are controlled to be 15nm, and the barrier layer is made of aromatic polyamide with high crosslinking degree and is 0.2um thick. The aromatic polyamide with high crosslinking degree is polymerized by benzene triacyl chloride and phenylenediamine.
The struvite in the step 5 is a slow release fertilizer containing Mg: n: the proportion of P is 1:1:1, and the pH value is controlled to be 8.5-9.5, thus being beneficial to the formation of the compound fertilizer.
The utility model discloses a theory of operation:
the corn starch wastewater enters a water collecting tank through a drainage pipe network of a corn starch production enterprise. After most suspended substances and floating objects are intercepted by the corn starch wastewater through the grating, the corn starch wastewater enters the grit chamber through the lifting pump. The effluent quality of the grit chamber is as follows: the COD concentration is 4500mg/L, the TN concentration is 420.78mg/L, NH4 +-N concentration of 400.57mg/L, TP concentration of 42mg/L, PO4 3-The P concentration was 40.35 mg/L.
Then, the effluent of the grit chamber exchanges heat with the effluent of the drawing liquid storage through a water source heat pump, the temperature is raised to 25 ℃ from 18 ℃, and then the effluent enters a reactor through a first peristaltic pump, and an ultrafiltration membrane component is arranged in the reactor to ensure that the effluent of the grit chamber exchanges heat with the effluent of the drawing liquid storage, and the temperature of the effluent is raised to 25 DEG CAnd an aerated stone. The effective area of the ultrafiltration membrane component is 0.1m2The size of the membrane is 320 multiplied by 220 multiplied by 5mm3The membrane pore size was 0.1. mu.m. After the operation is finished, concentrated solution with the volume of 1/11.5 of that of the raw water and effluent of the ultrafiltration membrane module with the volume of 10.5/11.5 are obtained. The membrane effluent rich in nitrogen and phosphorus substances is obtained while realizing low-carbon recovery of suspended matters and colloidal organic matters in the sewage, and the membrane effluent does not contain solid matters and pathogens and is rich in nitrogen and phosphorus elements, and enters a raw material liquid storage through a valve and a suction pump to recover nitrogen and phosphorus resources in the sewage; the reactor can be directly used for anaerobic digestion to produce methane, part of the methane generated by anaerobic digestion is aerated on the surface of the ultrafiltration membrane component by the aeration stone through the aeration pump, the membrane pollution reducing effect is more than 40%, the rest of the methane is directly recycled to realize energy recovery, and the methane recovery rate can reach about 85%. The aeration rate in the reactor is controlled to be 50L/h, the temperature is 25 ℃, the flux is controlled to be 20LMH and other parameter conditions during the operation. The method for cleaning the ultrafiltration membrane in the ultrafiltration membrane component is simple and convenient, the organic matters on the membrane are lightly scraped and returned to the concentrated solution, the surface of the membrane is cleaned by pure water with a certain volume, the cleaning solution is returned to the concentrated solution, then the surface of the membrane is washed by water until no obvious residual pollutant can be seen, finally sodium hypochlorite solution (with the effective chlorine concentration of 2000mg/L) is used for soaking for 2 hours, and then the residual chemical agent on the surface of the membrane is washed by water, so that 75% of the initial state can be recovered. The COD concentration of the effluent of the ultrafiltration section is 635mg/L, the TN concentration is 150.34mg/L, and NH4 +-N concentration of 132.56mg/L, TP concentration of 55.36mg/L, PO4 3-The P concentration was 54.28 mg/L.
In the forward osmosis process, water entering a raw material liquid storage device is used as raw material liquid, a high-salt solution of a main component KCl in common agricultural fertilizer potassium fertilizer is used as drawing liquid in a drawing liquid storage device, along with the operation of a forward osmosis system, the raw material liquid and the drawing liquid respectively enter a forward osmosis membrane assembly through a second peristaltic pump and a third peristaltic pump and then respectively return to the raw material liquid storage device and the drawing liquid storage device, and the volume of concentrated liquid is 1/10 of the raw material liquid. By utilizing high and low osmotic pressure difference, water in the raw material liquid reservoir continuously enters the drawing liquid reservoir through the forward osmosis membrane assembly, and the effective surface of the forward osmosis membrane in the forward osmosis membrane assemblyProduct of 30cm2(50 mm. times.60 mm) and the depth of the flow channel is 2 mm. The diluted draw solution in the draw solution storage device exchanges heat with the effluent of the grit chamber through a water source heat pump, and is replenished with water through a water replenishing pump when the water amount is insufficient, the temperature is reduced from 27 ℃ to 20 ℃, and then the diluted draw solution is pumped into a concentrated water tank; and continuously concentrating and enriching nitrogen and phosphorus resources in the concentrated raw material liquid in the raw material liquid storage device so as to facilitate the subsequent recovery of struvite. In the raw material liquid storage, a conductivity meter and a pH value tester are arranged. During the operation, the conditions of parameters such as cross flow speed of 15cm/s, temperature of 25 ℃, concentration of 2mol/L of draw solution and the like are controlled. After the forward osmosis membrane in the forward osmosis membrane component is operated, the membrane pollution is small, the forward osmosis membrane is easy to clean, and the membrane flux can be recovered by more than 85% only by carrying out physical cleaning for 15min (the gas-water ratio is 240L/h: 40L/h). The COD concentration of the concentrated solution in the forward osmosis section is 3530mg/L, the TN concentration is 765.74mg/L, and NH is added4 +-N concentration of 676.06mg/L, TP concentration of 493.38mg/L, PO4 3-The P concentration was 483.08 mg/L.
The water in the concentrated water tank is taken as concentrated water, the water in the fresh water tank is taken as fresh water directly, according to the high and low permeability pressure difference, the water in the fresh water tank can spontaneously enter the concentrated water tank to achieve the balance of two sides, and then a certain pressure is applied to one side of the concentrated water tank, so that the water in the concentrated water tank directly enters the fresh water tank through the reverse osmosis membrane component. The water in the concentrated water tank flows back to the drawing liquid storage after being concentrated, the water in the fresh water tank can be directly recovered, and the reuse rate of water resources reaches more than 55%.
And the concentrated solution in the raw material solution storage enters a sedimentation tank through a fifth peristaltic pump to carry out struvite chemical sedimentation. A pH value tester and a stirrer are arranged in the sedimentation tank. The pH value is adjusted to be 9.2, the reaction time is 20min, and N (NH)4 +)∶n(Mg2 +)∶n(PO3 4－) Is 4: 1.2: 1, stirring at 200rpm, precipitating for 1h, collecting supernatant, and drying the precipitate at 40 deg.C for 48h to obtain struvite precipitate. At the moment, nitrogen and phosphorus resources in the sewage are continuously concentrated and exist in a struvite precipitation form, the nitrogen and phosphorus resources can be recycled as slow release fertilizer, the nitrogen recovery rate reaches more than 85 percent, the phosphorus recovery rate reaches more than 82 percent, and the nitrogen and phosphorus resources can be recycledThe content of available phosphorus in the phosphorus-collecting product is up to more than 17%. The COD concentration of the supernatant of the sedimentation tank is 3530mg/L, the TN concentration is 298.72mg/L, and NH is added4 +-N concentration of 99.92mg/L, TP concentration of 88.9mg/L, PO4 3-The P concentration was 86.52 mg/L. And the supernatant of the sedimentation tank enters the reactor through a sixth peristaltic pump to further recover water, carbon, nitrogen, phosphorus and heat energy resources.
The utility model has the advantages that:
the technical scheme provided by the utility model compare in prior art, realized under the condition that the procedure is simple, low energy consumption, carbon emission are few, still have required sewage treatment effect. The complete recovery of water, carbon, nitrogen and phosphorus resources is realized, the water resources are efficiently recovered, and the water reuse rate is more than 55%; the carbon resource is efficiently recovered, and the methane recovery rate can reach 85 percent; the nitrogen and phosphorus resources are efficiently recovered, the nitrogen recovery rate reaches more than 85 percent, the phosphorus recovery rate reaches more than 82 percent, and the effective phosphorus content in the recovered phosphorus product reaches more than 17 percent; the pollution of the ultrafiltration membrane is small, and the membrane pollution effect can be reduced by more than 40% by aerating the membrane with methane; the forward osmosis membrane has small pollution and is easy to clean, and the membrane flux can be restored to more than 85 percent after physical cleaning for 15 min.
Drawings
Fig. 1 is the overall structure schematic diagram of the resource system of the present invention.
The labels in the above figures are as follows:
1. the device comprises a water collecting tank 2, a sand setting tank 3, a reactor 4, a raw material liquid storage 5, a drawing liquid storage 6, a forward osmosis membrane assembly 7, a concentrated water tank 8, a fresh water tank 9, a reverse osmosis membrane assembly 10, a sedimentation tank 11, a grid 12, a lifting pump 13, a first peristaltic pump 14, a water source heat pump 15, an aeration pump 16, an ultrafiltration membrane assembly 17, an aeration stone 18, a valve 19, a suction pump 20, a conductivity meter 21, a pH value tester 22, a second peristaltic pump 23, a third peristaltic pump 24, a fourth peristaltic pump 25, a water replenishing pump 26, a fifth peristaltic pump 27, a stirrer 28 and a sixth peristaltic pump.
Detailed Description
Please refer to fig. 1:
the utility model provides a system for corn starch waste water resource includes water collecting tank 1, grit chamber 2, reactor 3, raw material liquid accumulator 4, draw liquid accumulator 5, forward osmosis membrane subassembly 6, dense water tank 7, fresh water tank 8, reverse osmosis membrane subassembly 9 and sedimentation tank 10, wherein water collecting tank 1 is linked together with corn starch manufacturing enterprise's drainage pipe network, water collecting tank 1 is connected with grit chamber 2 through the pipeline, grit chamber 2 still is connected with reactor 3 through the pipeline, reactor 3 is connected with raw material liquid accumulator 4 through the pipeline, reactor 3 still is connected with sedimentation tank 10 through the pipeline, raw material liquid accumulator 4 also is connected with sedimentation tank 10 through the pipeline, raw material liquid accumulator 4 and draw liquid accumulator 5 are connected through two pipelines, osmotic membrane subassembly 6 assembles on two connecting pipelines of raw material liquid accumulator 4 and draw liquid accumulator 5, the drawing liquid storage 5 is also connected with a concentrated water tank 7 through a pipeline, and a reverse osmosis membrane component 9 is arranged between the concentrated water tank 7 and a fresh water tank 8.
Be provided with grid 11 in the catch basin 1 and be used for holding back suspended solid and the floater in the sewage, be equipped with on the connecting pipeline of catch basin 1 and grit chamber 2 in the sewage pump that elevator pump 12 is used for in the catch basin 1 goes into grit chamber 2, be equipped with first peristaltic pump 13 and water source heat pump 14 on the connecting pipeline of grit chamber 2 and reactor 3, grit chamber 2 is the aeration grit chamber.
The reactor 3 is an anaerobic membrane bioreactor, an ultrafiltration membrane component 16 and an aeration stone 17 are arranged in the reactor 3, and the effective area of an ultrafiltration membrane in the ultrafiltration membrane component 16 is 0.1m2The size of the membrane is 320 multiplied by 220 multiplied by 5mm3The aperture of the membrane is 0.1 μm, and the methane generated by anaerobic reaction is aerated on the surface of the ultrafiltration membrane component 16 by the aeration pump 15 and the aeration stone 17. A valve 18 and a suction pump 19 are arranged on a connecting pipeline between the reactor 3 and the raw material liquid storage tank 4, and a sixth peristaltic pump 28 is arranged on a connecting pipeline between the reactor 3 and the sedimentation tank 10.
A conductivity meter 20 and a pH value tester 21 are arranged in the raw material liquid storage 4, a second peristaltic pump 22 is assembled on a connecting pipeline between the raw material liquid storage 4 and the forward osmosis membrane assembly 6, a fifth peristaltic pump 26 is assembled on a connecting pipeline between the raw material liquid storage 4 and the sedimentation tank 10, and a third peristaltic pump is assembled on a connecting pipeline between the forward osmosis membrane assembly 6 and the drawing liquid storage 5A pump 23, a fourth peristaltic pump 24 and a water source heat pump 14 are arranged on a connecting pipeline of the drawing liquid storage 5 and the concentrated water tank 7, the forward osmosis membrane component 6 consists of a forward osmosis membrane and a membrane block, and the effective area of the forward osmosis membrane is 30cm2The depth of the flow channel is 2 mm.
The sedimentation basin 10 is equipped with a stirrer 27 and a pH tester 21.
The lift pump 12, the first peristaltic pump 13, the water source heat pump 14, the aeration pump 15, the suction pump 19, the conductivity meter 20, the pH tester 21, the second peristaltic pump 22, the third peristaltic pump 23, the fourth peristaltic pump 24 and the water supplement are all assembled by existing equipment, so that specific models and specifications are not described in detail.
The utility model provides a method for corn starch waste water resource, its method is as follows:
and 2, the effluent of the grit chamber 2 exchanges heat with the effluent of the drawing liquid storage 5 through a water source heat pump 14, the temperature is raised to 25 ℃ from 18 ℃, then the effluent is pumped into the reactor 3 by a first peristaltic pump 13 for treatment, an ultrafiltration membrane component 16 and an aeration stone 17 are arranged in the reactor 3, and the surface of the ultrafiltration membrane component 16 is aerated through the aeration pump 15 by means of the aeration stone 17 by using the methane generated by anaerobic reaction, so that membrane pollution is reduced. The water separated after being filtered by the ultrafiltration membrane component 16 is pumped into the raw material liquid storage 4 by a suction pump 19 through a valve 18;
and 4, taking the inlet water in the concentrated water tank 7 as concentrated water, directly taking the inlet water in the fresh water tank 8 as fresh water, and applying pressure on one side of the concentrated water tank 7 to enable the water in the concentrated water tank 7 to enter the fresh water tank 8 through the reverse osmosis membrane component 9. The water in the concentrated water tank 7 flows back to the drawing liquid storage 5 after being concentrated, and the water in the fresh water tank 8 can be directly recovered, so that the water resource can be recycled.
the grit chamber 2 in the step 1 is an aeration grit chamber.
The ultrafiltration membrane used in the ultrafiltration membrane component 16 in the step 2 is a flat membrane, and the effective area of the single membrane is 0.1m2The size of the membrane is 320 multiplied by 220 multiplied by 5mm3The aperture of the membrane is 0.1 μm, the material of the membrane is polyvinylidene fluoride, and the material of the support plate is acrylonitrile-butadiene-styrene copolymer.
The forward osmosis membrane used by the forward osmosis membrane component 6 in the step 3 belongs to an asymmetric membrane and consists of an active layer and a supporting layer, wherein the active layer is made of cellulose triacetate, the supporting layer is made of polyester, and the effective area of the forward osmosis membrane is 30cm2The depth of the flow channel is 2 mm.
The main supporting structure of the reverse osmosis membrane used by the reverse osmosis membrane component 9 in the step 4 is polyester non-woven fabric which is calendered by a calender, the surface of the polyester non-woven fabric has no loose fibers and is hard and smooth, microporous engineering plastic polysulfone is poured on the surface of the non-woven fabric, the holes on the surface of the polysulfone layer are controlled to be 15nm, and the barrier layer is made of aromatic polyamide with high crosslinking degree and has the thickness of 0.2 um. The aromatic polyamide with high crosslinking degree is polymerized by benzene triacyl chloride and phenylenediamine.
The struvite in the step 5 is a slow release fertilizer containing Mg: n: the proportion of P is 1:1:1, and the pH value is controlled to be 8.5-9.5, thus being beneficial to the formation of the compound fertilizer.
The utility model discloses a theory of operation:
the corn starch wastewater enters a water collecting tank 1 through a drainage pipe network of a corn starch production enterprise. After most suspended matters and floating objects are intercepted by the corn starch wastewater through the grating 11, the corn starch wastewater enters the grit chamber 2 through the lifting pump 12. The effluent quality of the grit chamber 2 is as follows: the COD concentration is 4500mg/L, the TN concentration is 420.78mg/L, NH4 +-N concentration of 400.57mg/L, TP concentration of 42mg/L, PO4 3-The P concentration was 40.35 mg/L.
Then, the effluent of the grit chamber 2 exchanges heat with the effluent of the drawing liquid storage 5 through a water source heat pump 14, the temperature is raised to 25 ℃ from 18 ℃, and then the effluent enters the reactor 3 through a first peristaltic pump 13, and an ultrafiltration membrane component 16 and an aeration stone 17 are arranged in the reactor 3. The effective area of the ultrafiltration membrane component 16 is 0.1m2The size of the membrane is 320 multiplied by 220 multiplied by 5mm3The membrane pore size was 0.1. mu.m. After the operation is finished, concentrated solution with the volume of 1/11.5 of that of the raw water and effluent of the ultrafiltration membrane module 16 with the volume of 10.5/11.5 are obtained. The membrane effluent rich in nitrogen and phosphorus substances is obtained while the low-carbon recovery of suspended matters and colloidal organic matters in the sewage is realized, and the membrane effluent does not contain solid matters and pathogens and is rich in nitrogen and phosphorus elements, and enters the raw material liquid storage 4 through the valve 18 and the suction pump 19 to recover nitrogen and phosphorus resources in the sewage; the reactor 3 can be directly used for anaerobic digestion to produce methane, part of the methane generated by anaerobic digestion is aerated on the surface of the ultrafiltration membrane component 16 by the aeration pump 15 and the aeration stone 17, the membrane pollution reducing effect is more than 40 percent, the rest of the methane is directly recycled to realize energy recovery, and the methane recovery rate can reach about 85 percent. The aeration rate in the reactor 3 is controlled to be 50L/h, the temperature is 25 ℃, the flux is controlled to be 20LMH and other parameter conditions during the operation. The method for cleaning the ultrafiltration membrane in the ultrafiltration membrane module 16 is simple and convenient, the organic matters on the membrane are lightly scraped and returned to the concentrated solution, the surface of the membrane is cleaned by pure water with a certain volume, the cleaning solution is returned to the concentrated solution, then the surface of the membrane is washed by water until no obvious residual pollutant is seen, finally sodium hypochlorite solution (with the effective chlorine concentration of 2000mg/L) is used for soaking for 2 hours, and then the sodium hypochlorite solution is used for cleaning the membrane, so that the concentration of the effective chlorineThe residual chemical agent on the surface of the film can be washed by water, and 75% of the original state can be recovered. The COD concentration of the effluent of the ultrafiltration section is 635mg/L, the TN concentration is 150.34mg/L, and NH4 +-N concentration of 132.56mg/L, TP concentration of 55.36mg/L, PO4 3-The P concentration was 54.28 mg/L.
In the forward osmosis process, water fed into a raw material liquid storage 4 is used as raw material liquid, a high-salt solution of a main component KCl in a common agricultural fertilizer potassium fertilizer is used as a drawing liquid in a drawing liquid storage 5, along with the operation of a forward osmosis system, the raw material liquid and the drawing liquid respectively enter a forward osmosis membrane assembly 6 through a second peristaltic pump 22 and a third peristaltic pump 23, and then respectively return to the raw material liquid storage 4 and the drawing liquid storage 5, and the volume of a concentrated solution is 1/10 of the raw material liquid. By utilizing high and low osmotic pressure difference, water in the raw material liquid storage 4 continuously enters the drawing liquid storage 5 through the forward osmosis membrane assembly 6, and the effective area of the forward osmosis membrane in the forward osmosis membrane assembly 6 is 30cm2(50 mm. times.60 mm) and the depth of the flow channel is 2 mm. The diluted draw solution in the draw solution storage 5 is subjected to heat exchange with the effluent water of the grit chamber 2 through a water source heat pump 14, water is supplemented through a water supplementing pump 25 when the water amount is insufficient, the temperature is reduced from 27 ℃ to 20 ℃, and then the diluted draw solution is pumped into a concentrated water tank 7 through a fourth peristaltic pump 24; and the nitrogen and phosphorus resources in the concentrated raw material liquid in the raw material liquid storage 4 are continuously concentrated and enriched so as to facilitate the subsequent recovery of struvite. In the raw material liquid reservoir 4, a conductivity meter 20 and a pH meter 21 are provided. During the operation, the conditions of parameters such as cross flow speed of 15cm/s, temperature of 25 ℃, concentration of 2mol/L of draw solution and the like are controlled. After the forward osmosis membrane in the forward osmosis membrane component 6 is operated, the membrane pollution is small, the cleaning is easy, and the membrane flux can be recovered by more than 85% only by carrying out 15min physical cleaning (gas-water ratio: 240L/h: 40L/h). The COD concentration of the concentrated solution in the forward osmosis section is 3530mg/L, the TN concentration is 765.74mg/L, and NH is added4 +-N concentration of 676.06mg/L, TP concentration of 493.38mg/L, PO4 3-The P concentration was 483.08 mg/L.
The water in the concentrated water tank 7 is taken as concentrated water, the water in the fresh water tank 8 is taken as fresh water directly, according to the high and low permeability pressure difference, the water in the fresh water tank 8 can enter the concentrated water tank 7 spontaneously to reach the balance of two sides, and then a certain pressure is applied to one side of the concentrated water tank 7, so that the water in the concentrated water tank 7 directly enters the fresh water tank 8 through the reverse osmosis membrane component 9. The water in the concentrated water tank 7 flows back to the drawing liquid storage 5 after being concentrated, the water in the fresh water tank 8 can be directly recycled, and the reuse rate of water resources reaches more than 55%.
The concentrated solution in the raw material liquid storage 4 enters the sedimentation tank 10 through a fifth peristaltic pump 26 to carry out struvite chemical sedimentation. The sedimentation tank 10 is provided with a pH value tester 21 and a stirrer 27. The pH value is adjusted to be 9.2, the reaction time is 20min, and N (NH)4 +)∶n(Mg2+)∶n(PO3 4－) Is 4: 1.2: 1, stirring at 200rpm, precipitating for 1h, collecting supernatant, and drying the precipitate at 40 deg.C for 48h to obtain struvite precipitate. At the moment, nitrogen and phosphorus resources in the sewage are continuously concentrated and exist in a struvite precipitation form, the nitrogen and phosphorus resources can be recycled as slow release fertilizer, the nitrogen and phosphorus resources are recycled, the nitrogen recovery rate reaches more than 85 percent, the phosphorus recovery rate reaches more than 82 percent, and the effective phosphorus content in the recycled phosphorus product reaches more than 17 percent. The COD concentration of the supernatant of the sedimentation tank 10 is 3530mg/L, the TN concentration is 298.72mg/L, and NH4 +-N concentration of 99.92mg/L, TP concentration of 88.9mg/L, PO4 3-The P concentration was 86.52 mg/L. The supernatant of the sedimentation tank 10 enters the reactor through a sixth peristaltic pump 28 to further recover water, carbon, nitrogen, phosphorus and heat energy resources.
Claims (5)
1. The utility model provides a system for be used for corn starch waste water resource which characterized in that: the device comprises a water collecting tank, a grit chamber, a reactor, a raw material liquid storage, a drawing liquid storage, a forward osmosis membrane assembly, a concentrated water tank, a fresh water tank, a reverse osmosis membrane assembly and a sedimentation tank, wherein the water collecting tank is communicated with a drainage pipe network of a corn starch production enterprise, the water collecting tank is connected with the grit chamber through a pipeline, the grit chamber is further connected with the reactor through a pipeline, the reactor is connected with the raw material liquid storage through a pipeline, the reactor is further connected with the sedimentation tank through a pipeline, the raw material liquid storage is also connected with the sedimentation tank through a pipeline, the raw material liquid storage and the drawing liquid storage are connected through two pipelines, the osmosis membrane assembly is assembled on two connecting pipelines of the raw material liquid storage and the drawing liquid storage, the drawing liquid storage is further connected with the concentrated water tank through a pipeline, and the reverse osmosis membrane assembly.
2. The system for recycling corn starch wastewater as claimed in claim 1, wherein: the collecting tank in be provided with the grid and be used for holding back suspended solid and the floater in the sewage, be equipped with the sewage pump that the elevator pump is used for in the collecting tank on the connecting line of collecting tank and grit chamber and go into in the grit chamber, be equipped with first peristaltic pump and water source heat pump on the connecting line of grit chamber and reactor, the grit chamber is aeration grit chamber.
3. The system for recycling corn starch wastewater as claimed in claim 1, wherein: the reactor is an anaerobic membrane bioreactor, an ultrafiltration membrane component and an aeration stone are arranged in the reactor, and the effective area of an ultrafiltration membrane in the ultrafiltration membrane component is 0.1m2The size of the membrane is 320 multiplied by 220 multiplied by 5mm3The aperture of the membrane is 0.1 mu m, the surface of the ultrafiltration membrane component is aerated by biogas generated by anaerobic through an aeration pump by means of an aeration stone, a valve and a suction pump are assembled on a connecting pipeline between the reactor and the raw material liquid reservoir, and a sixth peristaltic pump is assembled on a connecting pipeline between the reactor and the sedimentation tank.
4. The system for recycling corn starch wastewater as claimed in claim 1, wherein: the feed liquid accumulator in be provided with conductivity meter and pH value tester, be equipped with the second peristaltic pump on the connecting line of feed liquid accumulator and forward osmosis membrane subassembly, be equipped with the third peristaltic pump on the connecting line of forward osmosis membrane subassembly and draw liquid accumulator, be equipped with fourth peristaltic pump and water source heat pump on the connecting line of drawing liquid accumulator and concentrated water pond, the forward osmosis membrane subassembly comprises forward osmosis membrane and membrane piece, the effective area of forward osmosis membrane is 30cm2The depth of the flow channel is 2 mm.
5. The system for recycling corn starch wastewater as claimed in claim 1, wherein: and a stirrer and a pH value tester are assembled in the sedimentation tank.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN110550832A (en) * | 2019-10-17 | 2019-12-10 | 长春工程学院 | System and method for recycling corn starch wastewater |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN110550832A (en) * | 2019-10-17 | 2019-12-10 | 长春工程学院 | System and method for recycling corn starch wastewater |
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