CN110550832A - System and method for recycling corn starch wastewater - Google Patents
System and method for recycling corn starch wastewater Download PDFInfo
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- CN110550832A CN110550832A CN201910989225.7A CN201910989225A CN110550832A CN 110550832 A CN110550832 A CN 110550832A CN 201910989225 A CN201910989225 A CN 201910989225A CN 110550832 A CN110550832 A CN 110550832A
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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
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- 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
- C02F1/441—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by reverse osmosis
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- 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
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- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/445—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by forward osmosis
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Abstract
The invention discloses a system and a method for recycling corn starch wastewater, wherein the system 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 also connected with the reactor through a pipeline, the reactor is connected with the raw material liquid storage through a pipeline, and the method comprises the following steps: 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 invention relates to a system and a method for recycling wastewater, in particular to a system and a method for recycling corn starch wastewater.
Background
4 3- 4 2- 2 4 -The corn starch wastewater has the characteristics of high COD (chemical oxygen demand), high SS (suspended solids), high TN (total phosphorus) and high TP (total phosphorus) and low pH (pH), and in order to meet the discharge requirements of the discharge Standard of Water pollutants for the starch industry (GB 25461-.
Disclosure of Invention
the invention mainly aims to provide a system and a method for recycling corn starch wastewater, which can realize the high-efficiency recovery of water, carbon, nitrogen, phosphorus, heat energy and other resources in the corn starch wastewater.
The system for recycling the corn starch wastewater 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, the effective area of an ultrafiltration membrane in the ultrafiltration membrane component is 0.1m 2, the size length multiplied by the width multiplied by the height multiplied by 320 multiplied by 220 multiplied by 5mm 3, the membrane aperture is 0.1 mu m, the surface of the ultrafiltration membrane component is aerated by the anaerobic generated biogas through the aeration pump by means of the aeration stone, a valve and a suction pump are assembled on a connecting pipeline between the reactor and a raw material liquid reservoir, and a sixth peristaltic pump is assembled on a connecting pipeline between the reactor and a 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 pipeline of former feed liquid accumulator and forward osmosis membrane subassembly, be equipped with the third peristaltic pump on the connecting pipeline of forward osmosis membrane subassembly and draw liquid accumulator, be equipped with fourth peristaltic pump and water source heat pump on the connecting pipeline 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 30cm 2, the runner degree of depth 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 invention provides a method for recycling corn starch wastewater, which comprises the following steps:
Step 1, enabling the corn starch wastewater to enter a water collecting tank through a drainage pipe network of a corn starch production enterprise, intercepting most suspended matters and floating matters by the corn starch wastewater entering the water collecting tank through a grating, and then enabling the corn starch wastewater to enter a grit chamber through a lifting pump;
Step 2, the effluent of the grit chamber exchanges heat with the effluent of a drawing liquid storage through a water source heat pump, the temperature is raised to 25 ℃ from 18 ℃, and then the effluent is pumped into a reactor for treatment, an ultrafiltration membrane component and aeration stones are arranged in the reactor, the surface of the ultrafiltration membrane component is aerated through the aeration pump by means of the aeration stones to reduce membrane pollution, and the water separated after being filtered by the ultrafiltration membrane component is pumped into a raw material liquid storage through a valve;
Step 3, taking the inlet water in the raw material liquid storage as raw material liquid, taking a high-salt solution of main component KCl in common agricultural fertilizer potash fertilizer as an extraction liquid in an extraction liquid storage, continuously passing the water in the raw material liquid storage through a forward osmosis membrane assembly to enter the extraction liquid storage along with the operation of a forward osmosis system, carrying out heat exchange on the diluted extraction liquid and the outlet water of a sand basin through a water source heat pump, supplementing water through a water supplementing pump when the water amount is insufficient, reducing the temperature from 27 ℃ to 20 ℃, then pumping the diluted extraction liquid into a concentrated water basin, and continuously concentrating and enriching nitrogen and phosphorus resources in the concentrated raw material liquid in the raw material liquid storage and pumping the concentrated raw material liquid into a sedimentation basin;
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 module in the step 2 is a flat membrane, the effective area of the single membrane is 0.1m 2, the length, width and height of the membrane sheet are 320 x 220 x 5mm 3, the pore diameter 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 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, the effective area of the forward osmosis membrane is 30cm 2, and the depth of a 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 working principle of the invention is as follows:
the corn starch wastewater enters a water collecting tank through a drainage pipe network of a corn starch production enterprise, the corn starch wastewater enters a grit chamber through a lift pump after most suspended matters and floating matters are intercepted by a grid, and the effluent quality of the grit chamber comprises the COD concentration of 4500mg/L, the TN concentration of 420.78mg/L, the NH 4 + -N concentration of 400.57mg/L, the TP concentration of 42mg/L and the PO 4 3- -P concentration of 40.35 mg/L.
Then, the effluent of the grit chamber is subjected to heat exchange with the effluent of a drawing liquid storage through a water source heat pump, the temperature is raised to 25 ℃ from 18 ℃, then the effluent enters a reactor through a first peristaltic pump, an ultrafiltration membrane module and an aerator stone are arranged in the reactor, the effective area of the ultrafiltration membrane module is 0.1m 2, the size of the membrane is 320 x 220 x 5mm 3, the pore diameter of the membrane is 0.1 mu m, 1/11.5 of the volume of raw water is obtained after the operation is finished, 10.5/11.5 of the ultrafiltration membrane module is used for yielding water rich in nitrogen and phosphorus substances while realizing low-carbon recovery of suspended substances and colloidal organic matters in sewage, the effluent is free of solid substances and pathogens and 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 sewage, anaerobic digestion can be directly carried out in the reactor to produce methane, a part of the anaerobic digestion can be directly carried out on the surface of the ultrafiltration membrane module through the aerator stone to carry out aeration on the surface to reduce the membrane pollution effect recovery of more than 40%, the energy, the recovery can be directly, the recovery of the energy, the recovery of the residual sewage can be recovered by the sewage, the sewage is used for controlling the chemical concentration of a simple method, the sewage is carried out, the sewage is carried out, the sewage.
In the forward osmosis process, water entering a raw material liquid storage is used as raw material liquid, a high-salt solution of a main component KCl in a common agricultural fertilizer potash fertilizer is used as drawing liquid in a drawing liquid storage, 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 along with the operation of a forward osmosis system, then the forward osmosis membrane assembly respectively returns to the raw material liquid storage and the drawing liquid storage, the volume of the concentrated liquid is 1/10 of the raw material liquid, water in the raw material liquid storage continuously enters the drawing liquid storage through the forward osmosis membrane assembly by utilizing high and low permeability pressure difference, the effective area of a forward osmosis membrane in the forward osmosis membrane assembly is 30cm 2 (50mm multiplied by 60mm), the depth of a flow channel is 2mm, the drawn liquid diluted in the drawing liquid storage is subjected to heat exchange with water discharged from a sand basin through a water source heat pump, when the water quantity is insufficient, water is supplemented through a water supplementing pump, the temperature is reduced from 27 ℃ to 20 ℃, the forward osmosis membrane assembly is pumped into a concentrated water pool, the nitrogen and phosphorus resource is continuously enriched in the raw material liquid storage, the continuous enrichment of continuous recovery of continuous struvite, the continuous recovery of the subsequent struvite permeation, the test, the concentration of the forward osmosis membrane assembly is carried out, the test, the pH value is set by adopting a pH value of a concentration of a pH meter, the concentration of a concentration meter, the test instrument, the test period of a concentration of a pH meter is equal to be equal to 25.
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%.
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, N (NH 4 +) to N (Mg 2 +) to N (PO 3 4- ) is 4: 1.2: 1, the stirring speed is 200rpm, the sedimentation time is 1h, the sediment part is dried for 48h at 40 ℃ after the supernatant is collected, so that struvite sediment is obtained, at the moment, nitrogen and phosphorus resources in the sewage are continuously concentrated and exist in a struvite sedimentation form, the struvite sediment can be used as a slow release fertilizer for recycling, the nitrogen and phosphorus resources are recycled, the nitrogen recycling rate is more than 85%, the phosphorus recycling rate is more than 82%, the effective phosphorus content in the recycled phosphorus product is more than 17%, the COD concentration of the supernatant in the sedimentation tank is 3530Mg/L, the TN concentration is 298.72Mg/L, the NH 4 + -N concentration is 99.92Mg/L, the TP concentration is 88.9 Mg/9, the peristaltic concentration is more than 17 Mg/L, the supernatant is further enters a sixth peristaltic pump, the P concentration is 46 86.52Mg/L, and the supernatant is subjected to pass through a third peristaltic pump to react with the nitrogen and the.
The invention has the beneficial effects that:
Compared with the prior art, the technical scheme provided by the invention realizes the required sewage treatment effect under the conditions of simple process, low energy consumption and less carbon emission. 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 a schematic view of the overall structure of the recycling system of the present invention.
The labels in the above figures are as follows:
1. a water collecting tank 2, a grit chamber 3, a reactor 4, a raw material liquid storage 5 and a drawing liquid storage
6. A forward osmosis membrane component 7, a concentrated water tank 8, a fresh water tank 9, a reverse osmosis membrane component 10 and a sedimentation tank
11. A grid 12, a lifting pump 13, a first peristaltic pump 14, a water source heat pump 15 and an aeration pump
16. Ultrafiltration membrane component 17, aeration stone 18, valve 19, suction pump 20 and conductivity meter
21. a PH value tester 22, a second peristaltic pump 23, a third peristaltic pump 24 and 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 invention provides a system for recycling corn starch wastewater, which comprises a water collecting tank 1, a grit chamber 2, a reactor 3, a raw material liquid storage 4, a drawing liquid storage 5, a forward osmosis membrane assembly 6, a concentrated water tank 7, a fresh water tank 8, a reverse osmosis membrane assembly 9 and a sedimentation tank 10, wherein the water collecting tank 1 is communicated with a drainage pipe network of a corn starch production enterprise, the water collecting tank 1 is connected with the grit chamber 2 through a pipeline, the grit chamber 2 is also connected with the reactor 3 through a pipeline, the reactor 3 is connected with the raw material liquid storage 4 through a pipeline, the reactor 3 is also connected with the sedimentation tank 10 through a pipeline, the raw material liquid storage 4 and the drawing liquid storage 5 are connected through two pipelines, the osmosis membrane assembly 6 is assembled on the two connecting pipelines of the raw material liquid storage 4 and the drawing liquid storage 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, the effective area of an ultrafiltration membrane in the ultrafiltration membrane component 16 is 0.1m 2, the size length multiplied by the width multiplied by the height is 320 multiplied by 220 multiplied by 5mm 3, the membrane aperture is 0.1 mu m, the anaerobic generated biogas is used for aerating the surface of the ultrafiltration membrane component 16 by the aeration stone 17 through an aeration pump 15, a valve 18 and a suction pump 19 are arranged on a connecting pipeline between the reactor 3 and a raw material liquid storage 4, and a sixth peristaltic pump 28 is arranged on a connecting pipeline between the reactor 3 and a sedimentation tank 10.
Be provided with conductivity meter 20 and PH value tester 21 in the former feed liquid accumulator 4, be equipped with second peristaltic pump 22 on the connecting pipeline of former feed liquid accumulator 4 and positive osmotic membrane subassembly 6, be equipped with fifth peristaltic pump 26 on the connecting pipeline of former feed liquid accumulator 4 and sedimentation tank 10, be equipped with third peristaltic pump 23 on the connecting pipeline of positive osmotic membrane subassembly 6 and draw liquid accumulator 5, be equipped with fourth peristaltic pump 24 and water source heat pump 14 on the connecting pipeline of drawing liquid accumulator 5 and dense pond 7, positive osmotic membrane subassembly 6 comprises positive osmotic membrane and membrane piece, the effective area of positive osmotic membrane is 30cm 2, the runner depth 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 invention provides a method for recycling corn starch wastewater, which comprises the following steps:
step 1, corn starch wastewater enters a water collecting tank 1 through a drainage pipe network of a corn starch production enterprise, and the corn starch wastewater entering the water collecting tank 1 enters a grit chamber 2 through a lifting pump 12 after most suspended matters and floating matters are intercepted by a grating 11;
And 2, performing heat exchange on the effluent of the grit chamber 2 and the effluent of the drawing liquid storage 5 through a water source heat pump 14, raising the temperature from 18 ℃ to 25 ℃, pumping the effluent into the reactor 3 by a first peristaltic pump 13 for treatment, arranging an ultrafiltration membrane component 16 and an aeration stone 17 in the reactor 3, and aerating the surface of the ultrafiltration membrane component 16 by the anaerobic generated biogas through an aeration pump 15 by means of the aeration stone 17 to reduce membrane pollution. 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;
Step 3, taking the inlet water in the raw material liquid storage 4 as a raw material liquid, taking a high-salt solution of a main component KCl in a common agricultural fertilizer potash fertilizer as a drawing liquid in the drawing liquid storage 5, along with the operation of a forward osmosis system, utilizing a high and low permeability pressure difference to enable water in the raw material liquid storage 4 to continuously enter the drawing liquid storage 5 through the forward osmosis membrane assembly 6, enabling the diluted drawing liquid to pass through the water source heat pump 14 to exchange heat with outlet water of the grit chamber 2, supplementing water through a water supplementing pump 25 when the water quantity is insufficient, reducing the temperature from 27 ℃ to 20 ℃, then pumping the diluted drawing liquid into the concentrated water tank 7 through a fourth peristaltic pump 24, and continuously concentrating and enriching nitrogen and phosphorus resources in the concentrated raw material liquid in the raw material liquid storage 4 and pumping the concentrated and enriched nitrogen and phosphorus resources into the sedimentation tank 10 through a fifth peristaltic pump 26;
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.
Step 5, enabling the concentrated solution entering the sedimentation tank 10 to generate struvite sediment in the sedimentation tank 10 by adjusting the conditions of the pH value and the nitrogen-magnesium-phosphorus ratio to be recycled as slow release fertilizer, and pumping the supernatant in the sedimentation tank 10 into the reactor 3 by a sixth peristaltic pump 28 to realize the complete recovery of water, carbon, nitrogen, phosphorus and heat energy resources;
The grit chamber 2 in the step 1 is an aeration grit chamber.
The ultrafiltration membrane used in the ultrafiltration membrane module 16 in the step 2 is a flat membrane, the effective area of the single membrane is 0.1m 2, the size length × width × height of the membrane is 320 × 220 × 5mm 3, the pore diameter of the membrane is 0.1 μm, the membrane material is polyvinylidene fluoride, and the support plate material 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, the effective area of the forward osmosis membrane is 30cm 2, and the depth of a 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 working principle of the invention is as follows:
Corn starch wastewater enters a water collecting tank 1 through a drainage pipe network of a corn starch production enterprise, the corn starch wastewater enters a grit chamber 2 through a lifting pump 12 after most suspended matters and floating matters are intercepted by a grating 11, and the effluent quality of the grit chamber 2 comprises the COD concentration of 4500mg/L, the TN concentration of 420.78mg/L, the NH 4 + -N concentration of 400.57mg/L, the TP concentration of 42mg/L and the PO 4 3- -P concentration of 40.35 mg/L.
Then, the effluent of the grit chamber 2 passes through a water source heat pump 14 to exchange heat with the effluent of a drawing liquid storage 5, the temperature is raised to 25 ℃ from 18 ℃, then the effluent enters a reactor 3 through a first peristaltic pump 13, an ultrafiltration membrane module 16 and an aeration stone 17 are arranged in the reactor 3, the effective area of the ultrafiltration membrane module 16 is 0.1m 2, the size length x width x height of the membrane is 320 x 220 x 5mm 3, the pore diameter of the membrane is 0.1 μm, after the operation is finished, 1/11.5 volume of concentrate of raw water is obtained, 10.5/11.5 volume of the ultrafiltration membrane module 16 produces water, the effluent of the membrane rich in nitrogen and phosphorus substances is obtained while low-carbon recovery of suspended substances and colloidal organic substances in sewage is realized, the effluent of the membrane rich in nitrogen and phosphorus substances is obtained because the effluent does not contain solid substances and pathogens and is rich in nitrogen and phosphorus elements, the effluent enters a raw material liquid storage 4 through a valve 18 and a suction pump 19 to recover nitrogen and phosphorus resources in the sewage, anaerobic digestion can be used for producing methane directly in the reactor 3, a part of the anaerobic digestion, the sewage can be used for producing methane, the sewage can be used for directly used for controlling the concentration of sewage, the sewage is recovered by a sewage, the sewage is obtained by using a sewage, the sewage is obtained by using a simple aeration pump 15, the sewage is used for removing method for removing the sewage, the sewage is used for removing the sewage, the sewage is used for removing method for removing the sewage, the sewage is used for removing the.
In the forward osmosis process, water entering a raw material liquid storage 4 is used as raw material liquid, a high-salt solution of main component KCl in common agricultural fertilizer potash fertilizer is used as drawing liquid in a drawing liquid storage 5, 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 along with the operation of a forward osmosis system, the volume of the concentrated liquid is 1/10 of the raw material liquid, water in the raw material liquid storage 4 continuously enters the drawing liquid storage 5 through the forward osmosis membrane assembly 6 by utilizing high and low osmotic pressure difference, the effective area of a forward osmosis membrane in the forward osmosis membrane assembly 6 is 30cm 2 (50mm multiplied by 60mm), the depth of a flow channel is 2mm, the drawn liquid diluted in the drawing liquid storage 5 passes through a water source heat pump 14 to exchange heat with water discharged from a sand basin 2, water replenishing is carried out through a water pump 25 to replenish water, the osmotic membrane is lowered from 27 ℃ to 20 ℃ and then passes through a fourth water tank 7, the continuous peristaltic pump 4 after the concentrated liquid in the raw material liquid storage 5 is pumped into the sewage storage 4, the sewage storage is easy to recover the sewage concentration of a sewage concentration meter, the bird pollution recovery device, the sewage is reached by a concentration of 240-21-29 mg, the concentration of a PH-29 Mg-21-10 Mg concentration (the P-200-10-L sewage concentration sewage-2P sewage concentration tester, the sewage is easily recovered after the sewage is tested.
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%.
Concentrated solution in a raw material solution storage 4 enters a sedimentation tank 10 through a fifth peristaltic pump 26 to carry out struvite chemical sedimentation, a PH value tester 21 and a stirrer 27 are arranged in the sedimentation tank 10, the PH value is adjusted to be 9.2, the reaction time is 20min, N (NH 4 +) to N (Mg 2+) to N (PO 3 4- ) are 4: 1.2: 1, the stirring speed is 200rpm, the sedimentation time is 1h, a sediment part is dried for 48h at 40 ℃ after supernatant fluid is collected, and a struvite sediment is obtained, at the moment, nitrogen and phosphorus resources in sewage are continuously concentrated and exist in a struvite sediment form, the struvite sediment can be recycled as slow release fertilizer, so that the nitrogen and phosphorus resources are recycled, the nitrogen recovery rate is more than 85%, the phosphorus recovery rate is more than 82%, the effective phosphorus content in a recycled phosphorus product is more than 17%, the COD concentration of the supernatant fluid in the sedimentation tank 10 is 3530Mg/L, the TN concentration is 298.72Mg/L, the NH 56-N concentration is 99.92Mg/L, the TP concentration is 88 Mg/L, the P concentration is 9.88 Mg/8 Mg/L, the P concentration is 4625 Mg/86.52 Mg/L, the P concentration is further fed into a sixth peristaltic pump, and the heat energy recovery tank 10 is fed into a reaction water.
Claims (10)
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 as claimed in claim 1, wherein the reactor is an anaerobic membrane bioreactor, the reactor is internally provided with an ultrafiltration membrane module and an aeration stone, the effective area of an ultrafiltration membrane in the ultrafiltration membrane module is 0.1m 2, the size of the membrane is 3 mm with the length multiplied by the width multiplied by the height multiplied by 320 multiplied by 220 multiplied by 5mm, the pore diameter of the membrane is 0.1 μm, the anaerobic generated biogas is used for aerating the surface of the ultrafiltration membrane module by the aeration stone through the aeration pump, a valve and a suction pump are arranged on a connecting pipeline between the reactor and a raw material liquid reservoir, and a sixth peristaltic pump is arranged on a connecting pipeline between the reactor and a sedimentation tank.
4. The system for recycling the corn starch wastewater as claimed in claim 1, wherein a conductivity meter and a pH value tester are arranged in the raw material liquid reservoir, a second peristaltic pump is arranged on a connecting pipeline between the raw material liquid reservoir and the forward osmosis membrane module, a third peristaltic pump is arranged on a connecting pipeline between the forward osmosis membrane module and the draw liquid reservoir, a fourth peristaltic pump and a water source heat pump are arranged on a connecting pipeline between the draw liquid reservoir and the concentrated water tank, the forward osmosis membrane module comprises a forward osmosis membrane and a membrane block, the effective area of the forward osmosis membrane is 30cm 2, and the depth of a 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.
6. A method for recycling corn starch wastewater is characterized by comprising the following steps: the method comprises the following steps:
Step 1, enabling the corn starch wastewater to enter a water collecting tank through a drainage pipe network of a corn starch production enterprise, intercepting most suspended matters and floating matters by the corn starch wastewater entering the water collecting tank through a grating, and then enabling the corn starch wastewater to enter a grit chamber through a lifting pump;
step 2, the effluent of the grit chamber exchanges heat with the effluent of a drawing liquid storage through a water source heat pump, the temperature is raised to 25 ℃ from 18 ℃, and then the effluent is pumped into a reactor for treatment, an ultrafiltration membrane component and aeration stones are arranged in the reactor, the surface of the ultrafiltration membrane component is aerated through the aeration pump by means of the aeration stones to reduce membrane pollution, and the water separated after being filtered by the ultrafiltration membrane component is pumped into a raw material liquid storage through a valve;
step 3, taking the inlet water in the raw material liquid storage as raw material liquid, taking a high-salt solution of main component KCl in common agricultural fertilizer potash fertilizer as an extraction liquid in an extraction liquid storage, continuously passing the water in the raw material liquid storage through a forward osmosis membrane assembly to enter the extraction liquid storage along with the operation of a forward osmosis system, carrying out heat exchange on the diluted extraction liquid and the outlet water of a sand basin through a water source heat pump, supplementing water through a water supplementing pump when the water amount is insufficient, reducing the temperature from 27 ℃ to 20 ℃, then pumping the diluted extraction liquid into a concentrated water basin, and continuously concentrating and enriching nitrogen and phosphorus resources in the concentrated raw material liquid in the raw material liquid storage and pumping the concentrated raw material liquid into a sedimentation basin;
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.
7. The method as claimed in claim 6, wherein the ultrafiltration membrane used in the ultrafiltration membrane module of step 2 is a flat membrane, the effective area of the single membrane is 0.1m 2, the membrane size is 320 x 220 x 5mm 3, the pore diameter 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.
8. The method as claimed in claim 6, wherein the forward osmosis membrane used in the forward osmosis membrane module in the step 3 belongs to an asymmetric membrane, and comprises an active layer and a support layer, wherein the active layer is made of triacetyl cellulose, the support layer is made of polyester, the effective area of the forward osmosis membrane is 30cm 2, and the depth of the flow channel is 2 mm.
9. The method for recycling corn starch wastewater as claimed in claim 6, wherein the method comprises the following steps: the main supporting structure of the reverse osmosis membrane used in 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 in the surface of the polysulfone layer are controlled to be 15nm, the barrier layer is made of aromatic polyamide with high crosslinking degree, the thickness of the aromatic polyamide is 0.2um, and the aromatic polyamide with high crosslinking degree is formed by polymerizing benzene triacyl chloride and phenylenediamine.
10. the method for recycling corn starch wastewater as claimed in claim 6, wherein the method comprises the following steps: 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.
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