CN112225375A - Pretreatment method of sucralose wastewater - Google Patents
Pretreatment method of sucralose wastewater Download PDFInfo
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- CN112225375A CN112225375A CN202011027949.2A CN202011027949A CN112225375A CN 112225375 A CN112225375 A CN 112225375A CN 202011027949 A CN202011027949 A CN 202011027949A CN 112225375 A CN112225375 A CN 112225375A
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- 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
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
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- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/24—Treatment of water, waste water, or sewage by flotation
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- 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
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- 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
- C02F1/5236—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents
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- 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
- C02F1/54—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using organic material
- C02F1/56—Macromolecular compounds
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- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/725—Treatment of water, waste water, or sewage by oxidation by catalytic oxidation
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- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/32—Nature of the water, waste water, sewage or sludge to be treated from the food or foodstuff industry, e.g. brewery waste waters
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Abstract
The invention relates to a method for pretreating sucralose wastewater, which is characterized by comprising the following steps: (1) the sucralose wastewater is sequentially treated by an adjusting tank, a coagulating sedimentation tank and a wet catalytic oxidation device; (2) continuously feeding the wastewater into a coagulating sedimentation tank, respectively adding a coagulant accounting for 0.02-0.04% of the weight of the wastewater and a coagulant aid accounting for 0.002-0.005%, controlling the pH value to be 6.5-7.5, reacting for 10-15min, feeding the wastewater into the sedimentation tank after the wastewater comes out, and keeping the wastewater for 1.5-2.5 h; (3) floating supernatant in the sedimentation tank, filtering floating slag through quartz sand, feeding wastewater into a membrane separation device, and feeding the formed inorganic high-salt wastewater and organic low-salt wastewater into an MVR evaporator respectively; (4) the evaporation condensate water enters a biochemical system, and the evaporation concentrated solution of the inorganic high-salinity wastewater returns to the regulating reservoir; and (4) the organic low-salt wastewater evaporation concentrated solution enters an incineration device. The invention has the advantages that: the ammonium chloride with the content of more than 90 percent can be obtained and can be recycled; the COD of the effluent treated by the biochemical system is stabilized below 150 mg/L; 3. the membrane system can continuously and stably operate, and the cleaning times are reduced.
Description
Technical Field
The invention belongs to the technical field of sewage treatment, and particularly relates to a method for pretreating sucralose production wastewater.
Technical Field
Sucralose, as a high-potency sweetener, has the advantages of no energy, high sweetness, high safety and the like, and is one of the most ideal sweeteners at present.
However, the wastewater generated in the production process of sucralose is often high in concentration, high in salt content and difficult to degrade, the ring-opening chain scission and degradation treatment of the organic wastewater containing ring-type high-molecular pollutants are difficult, if the pretreatment cannot achieve the effect, the subsequent biochemical treatment is difficult, and even the effluent cannot reach the standard.
The existing better treatment technology is a pretreatment mode of wet catalytic oxidation, membrane separation and MVR, the efficiency of wet catalytic oxidation is 50-60% due to excessive sugar in the wastewater, and more organic matters still exist in the treated wastewater; the wastewater after wet oxidation treatment enters a membrane separation device to separate organic matters from inorganic salts, but the continuous operation time of a membrane system is very short (short 2-3h and long 3-5 days) due to the high content of the organic matters and suspended matters SS in the wastewater, a filter element at the front end needs to be cleaned and replaced, and the cleaning of the filter element is very troublesome, so that the continuous operation of the membrane system and the efficiency of the whole device are influenced; waste water after membrane separation gets into the MVR device and carries out the evaporation concentration, and the ammonium chloride salt of output still contains a large amount of organic matters for the ammonium chloride salt colour is dark, impurity is many, and resource utilization's cost is high, and it is higher to dispose the expense when the danger is useless.
Disclosure of Invention
The invention aims to solve the problems in the existing sucralose wastewater treatment process, and provides a device and a method for pretreating sucralose production wastewater; the invention has better degradation effect on cyclic and heterocyclic macromolecular organic pollutants in water, can open a ring and break a chain, improves the biodegradability of wastewater, can separate organic matters and inorganic salts (ammonium chloride salts) in the wastewater by a membrane separation system, improves the concentration efficiency of an MVR system, greatly reduces the amount of concentrated solution, enables the generated ammonium chloride salts to be recycled, and reduces the disposal cost.
In order to achieve the purpose, the technical scheme adopted by the invention is as follows:
a method for pretreating sucralose wastewater comprises the following existing devices: equalizing basin, coagulating sedimentation pond, wet-type catalytic oxidation device, membrane separator, MVR evaporimeter, biochemical system, burn the device, its characterized in that: a coagulating sedimentation tank, an air flotation machine and a quartz sand filter are sequentially added behind the wet catalytic oxidation device;
the method comprises the following steps:
(1) waste water (CODcr is 80000-120000 mg/L) generated by sucralose is sequentially subjected to regulation by a regulating reservoir and treatment by a coagulating sedimentation tank (most of colloid is removed, part of COD is degraded), the waste water enters a wet catalytic oxidation device for catalytic oxidation treatment, and macromolecular organic matters in the waste water are cracked into micromolecular organic matters under the action of high temperature and high pressure (the pressure is 20-30MPa, and the temperature is 210 ℃);
(2) the waste water after wet catalytic oxidation (CODcr is 40000-50000 mg/L) enters a coagulating sedimentation tank, coagulant polyaluminium chloride accounting for 0.02-0.04% of the weight of the waste water and polyacrylamide accounting for 0.002-0.005% of the weight of the waste water are added, the PH of the waste water reaction is controlled to be 6.5-7.5, the waste water is reacted for 10-15min, the waste water enters the sedimentation tank after coming out, the retention time is 1.5-2.5h, after the sediment is dehydrated by a dehydration device, mud cakes are treated as dangerous waste, and the filtrate returns to an adjusting tank;
(3) floating the supernatant from the sedimentation tank (the floating device releases after being filled with pressurized air, a large amount of fine bubbles are formed in water), bringing suspended matters to the water surface through the bubbles, filtering a small amount of floating slag and suspended matters through quartz sand, enabling the wastewater filtered through the quartz sand to enter a membrane separation device (a nanofiltration membrane, wherein the diameter of micropores on the surface of the membrane is 0.5-10 nm), enabling inorganic salts and water molecules in the wastewater to penetrate through the membrane to form inorganic high-salt wastewater (CODcr is 8000 mg/L) and organic matters in the wastewater to be intercepted to form organic low-salt wastewater (the salt content is below 500mg/L and CODcr is 48000 mg/L) and respectively entering an MVR evaporator for treatment;
(4) evaporating condensed water (CODcr is below 2000 mg/L) obtained after inorganic high-salt wastewater passes through an MVR evaporator, allowing the condensed water to enter a biochemical system, and returning the obtained (inorganic high-salt wastewater) evaporation concentrated solution to a regulating tank; evaporating condensed water (CODcr is below 20000 mg/L) obtained after the organic low-salt wastewater passes through an MVR evaporator enters a biochemical system, and the obtained (organic low-salt wastewater) evaporation concentrated solution enters an incineration device.
Further, the adding amount of the coagulant polyaluminium chloride and the coagulant aid polyacrylamide in the step (2) is 0.03 percent and 0.003 percent of the weight of the wastewater respectively.
Further, the diameter of the micropores on the membrane surface of the membrane separation device in the step (3) is 2-8 nm.
Further, the diameter of the micropores on the membrane surface of the membrane separation device in the step (3) is 4-6 nm.
Through adding coagulant polyaluminium chloride and coagulant aid polyacrylamide into the waste water after wet catalytic oxidation, further deposit most suspended solid SS and colloid in the waste water, follow-up waste water passes through the air supporting device again, release tiny bubble after the air supporting device leads to pressurized gas to further detach the suspended solid SS in aquatic, but the air supporting device easily produces the dross, there is partial dross easily to get into follow-up system along with water, so add quartz sand after the air supporting goes out water and filter as safeguard measure, quartz sand can recycle.
The invention has the advantages that:
1, centrifuging the inorganic high-salt wastewater concentrated solution subjected to MVR evaporation concentration by using a centrifuge to obtain an ammonium chloride salt with the content of more than 90%, wherein the ammonium chloride salt is white in color and can be recycled for use in production of chemical fertilizers, so that the treatment cost of the original ammonium chloride salt as hazardous waste is greatly reduced (the treatment cost of each ton of hazardous waste is 3500 plus 4500 yuan/ton, and the ammonium chloride salt can be sold 500 yuan/ton);
2. the COD concentration of the wastewater (evaporation condensed water mixed liquid) subjected to MVR evaporation concentration treatment is reduced to be below 20000mg/L, the biochemical property is greatly improved, and the COD of the effluent can be ensured to be below 150mg/L after the wastewater enters a biochemical system and is subjected to two-stage anaerobic treatment and two-stage aerobic treatment;
3. after the wastewater after wet catalytic oxidation is treated by sedimentation, air flotation and quartz sand in a sedimentation tank, the content of organic matters and Suspended Solids (SS) in the wastewater entering a membrane separation system is greatly reduced, so that the membrane system can continuously and stably operate, the cleaning frequency is reduced (the cleaning time is prolonged from 3-5 days to 30 days), and the separation efficiency is improved.
Drawings
FIG. 1 is a schematic diagram of a process for pretreating sucralose wastewater.
Detailed Description
Example 1
A method for pretreating sucralose wastewater comprises the following specific implementation steps:
(1) waste water 5m generated by sucralose3The method comprises the following steps that (h) (CODcr is 100000 mg/L), the wastewater enters a regulating tank, the wastewater is stirred by air, ammonia water with the mass concentration of 20% is added into the regulating tank to regulate the PH to be 7.0, then the wastewater is pumped into a stirring reactor, 1500g of coagulant polyaluminium chloride and 150g of coagulant aid polyacrylamide are added, the PH of the wastewater is controlled to be 7, sedimentation is carried out for 2h, the wastewater enters a vertical flow sedimentation tank, precipitates are dehydrated by a screw-stacking dehydrator, sedimentated mud cakes are treated as dangerous waste, supernate enters a wet catalytic oxidation device to be subjected to catalytic oxidation treatment, the pressure is controlled to be 25MPa, the temperature is controlled to be 210 ℃, organic matters in the wastewater are cracked, heterocyclic, cyclic, long-chain and other difficultly-degradable macromolecular organic matters are changed into micromolecular organic matters;
(2) 5m of waste water after wet catalytic oxidation3Feeding the wastewater into a coagulating sedimentation tank (CODcr is 45000 mg/L), adding 1000g of coagulant polyaluminium chloride and 100g of coagulant aid polyacrylamide, controlling the pH of the wastewater to be 6.8, precipitating for 2h, feeding the wastewater into an inclined plate sedimentation tank after the wastewater comes out, dehydrating the precipitate by a screw stacking machine, treating the precipitate mud cake as dangerous waste, and feeding the supernatant into a subsequent system;
(3) the wastewater from the inclined plate sedimentation tank is subjected to air floatation (pressurized air is introduced into an air floatation device and then released, a large amount of fine bubbles are formed in the water, the pressure is 0.2 MPa), suspended matters are brought to the water surface through the bubbles, floating slag is removed through quartz sand filtration, the wastewater after quartz sand filtration enters a membrane separation device (a nanofiltration membrane, the diameter of micropores on the surface of the membrane is 5 nm), inorganic salts and water molecules in the wastewater penetrate through the membrane to form inorganic high-salt wastewater (CODcr is 8000mg/L-10000 mg/L), organic matters in the wastewater are intercepted to form organic low-salt wastewater (the salt content is 400mg/L, CODcr is 40000 mg/L), and the organic low-salt wastewater respectively enters an MVR evaporator for treatment;
(4) evaporating condensed water (CODcr is 2000 mg/L) obtained after the inorganic high-salt wastewater passes through the MVR evaporator, allowing the condensed water to enter a biochemical system, and returning the obtained (inorganic high-salt wastewater) evaporation concentrated solution to the regulating tank; the organic low-salt wastewater passes through an MVR evaporator to obtain evaporation condensed water (CODcr is 19000 mg/L) and enters a biochemical system, and the obtained (organic low-salt wastewater) evaporation concentrated solution enters an incineration device.
Example 2
(1) 2.5m of waste water generated by sucralose3The method comprises the following steps that (h) (CODcr is 100000 mg/L), the wastewater enters a regulating tank, the wastewater is stirred by air, ammonia water with the mass concentration of 20% is added into the regulating tank to regulate the pH value to 7.0, then the wastewater is pumped into a stirring reactor, 1000g of coagulant polyaluminium chloride and 100g of coagulant aid polyacrylamide are added, the pH value of the wastewater is controlled to 7, sedimentation is carried out for 2.2h, the wastewater enters a vertical flow sedimentation tank, precipitates are dehydrated by a screw-stacking dehydrator, a sedimentated mud cake is treated as dangerous waste, supernate enters a wet catalytic oxidation device to be subjected to catalytic oxidation treatment, the pressure is controlled to be 25MPa, the temperature is controlled to be 210 ℃, organic matters in the wastewater are cracked, and heterocyclic, cyclic, long-chain and other difficultly-degradable macromolecular organic matters are changed into micromolecular organic;
(2) 2.5m of waste water after wet catalytic oxidation3Feeding the wastewater into a coagulating sedimentation tank (CODcr is 45000 mg/L), adding 1000g of coagulant polyaluminium chloride and 100g of coagulant aid polyacrylamide, controlling the pH of the wastewater to be 6.8, precipitating for 2.2h, feeding the wastewater into an inclined plate sedimentation tank after the wastewater comes out, dehydrating the precipitate by a screw stacking machine, treating the precipitate mud cake as dangerous waste, and feeding the supernatant into a subsequent system;
(3) the wastewater from the inclined plate sedimentation tank is subjected to air floatation (pressurized air is introduced into an air floatation device and then released, a large amount of fine bubbles are formed in the water, the pressure is 0.4 MPa), suspended matters are brought to the water surface through the bubbles, floating slag is removed through quartz sand filtration, the wastewater after quartz sand filtration enters a membrane separation device (a nanofiltration membrane, the diameter of micropores on the surface of the membrane is 5 nm), inorganic salts and water molecules in the wastewater penetrate through the membrane to form inorganic high-salt wastewater (CODcr is 8000 mg/L), organic matters in the wastewater are intercepted to form organic low-salt wastewater (the salt content is 400mg/L and CODcr is 45000 mg/L), and the organic low-salt wastewater respectively enters an MVR evaporator for treatment;
(4) evaporating condensed water (CODcr is 2000 mg/L) obtained after the inorganic high-salt wastewater passes through the MVR evaporator, allowing the condensed water to enter a biochemical system, and returning the obtained (inorganic high-salt wastewater) evaporation concentrated solution to the regulating tank; evaporating condensed water (CODcr is below 15000 mg/L) obtained after the organic low-salt wastewater passes through an MVR evaporator enters a biochemical system, and the obtained (organic low-salt wastewater) evaporation concentrated solution enters an incineration device.
Comparative example 1
(1) Waste water 5m generated by sucralose3The method comprises the following steps that (h) (CODcr is 100000 mg/L), the wastewater enters a regulating tank, the wastewater is stirred by air, ammonia water with the mass concentration of 20% is added into the regulating tank to regulate the PH to be 7.0, then the wastewater is pumped into a stirring reactor, 1500g of coagulant polyaluminium chloride and 150g of coagulant aid polyacrylamide are added, the PH of the wastewater is controlled to be 7, sedimentation is carried out for 2h, the wastewater enters a vertical flow sedimentation tank, precipitates are dehydrated by a screw-stacking dehydrator, sedimentated mud cakes are treated as dangerous waste, supernate enters a wet catalytic oxidation device to be subjected to catalytic oxidation treatment, the pressure is controlled to be 25MPa, the temperature is controlled to be 210 ℃, organic matters in the wastewater are cracked, heterocyclic, cyclic, long-chain and other difficultly-degradable macromolecular organic matters are changed into micromolecular organic matters;
(2) 5m of waste water after wet catalytic oxidation3The wastewater enters a membrane separation device (a nanofiltration membrane, the diameter of micropores on the surface of the membrane is 5 nm), inorganic salt and water molecules in the wastewater penetrate through the membrane to form inorganic high-salt wastewater (CODcr is 3000 mg/L), organic matters in the wastewater are intercepted to form organic low-salt wastewater (the salt content is 200mg/L, the CODcr is 42000 mg/L), and the organic low-salt wastewater respectively enters an MVR evaporator for treatment;
(4) evaporating condensed water (CODcr is 3000 mg/L) obtained after the inorganic high-salt wastewater passes through an MVR evaporator, allowing the condensed water to enter a biochemical system, and returning the obtained (inorganic high-salt wastewater) evaporation concentrated solution to a regulating tank; evaporating condensed water (CODcr is 20000 mg/L) obtained after the organic low-salt wastewater passes through an MVR evaporator enters a biochemical system, and the obtained (organic low-salt wastewater) evaporating concentrated solution enters an incineration device.
Claims (8)
1. A method for pretreating sucralose wastewater comprises the following existing devices: equalizing basin, coagulating sedimentation pond, wet-type catalytic oxidation device, membrane separator, MVR evaporimeter, biochemical system, burn the device, its characterized in that: a coagulating sedimentation tank, an air flotation machine and a quartz sand filter are sequentially added behind the wet catalytic oxidation device;
the method comprises the following steps:
(1) waste water generated by the sucralose is treated by an adjusting tank, a coagulating sedimentation tank and a wet catalytic oxidation device in sequence;
(2) the waste water after wet catalytic oxidation enters a coagulating sedimentation tank, a coagulant of polyaluminium chloride accounting for 0.02-0.04% of the weight of the waste water and a coagulant aid of polyacrylamide accounting for 0.002-0.005% of the weight of the waste water are added, the PH of the waste water reaction is controlled to be 6.5-7.5, the reaction lasts for 10-15min, the waste water enters the sedimentation tank after coming out, and the retention time is 1.5-2.5 h;
(3) floating supernatant liquid from the sedimentation tank, filtering floating slag by quartz sand, feeding the wastewater filtered by the quartz sand into a membrane separation device, and feeding inorganic high-salt wastewater and organic low-salt wastewater formed by membrane separation into an MVR evaporator for treatment;
(4) evaporating condensed water obtained by MVR evaporation enters a biochemical system, and returning the obtained inorganic high-salt wastewater evaporation concentrated solution to the regulating tank; and the obtained evaporation concentrated solution of the organic low-salt wastewater enters an incineration device.
2. The method for pretreating sucralose wastewater according to claim 1, wherein the method comprises the following steps: the CODcr of the wastewater in the step (1) is 80000-120000 mg/L.
3. The method for pretreating sucralose wastewater according to claim 1, wherein the method comprises the following steps: the CODcr of the wastewater after the wet catalytic oxidation in the step (2) is 40000-50000 mg/L.
4. The method for pretreating sucralose wastewater according to claim 1, wherein the method comprises the following steps: in the step (2), the addition amounts of the coagulant polyaluminium chloride and the coagulant aid polyacrylamide are respectively 0.03 percent and 0.003 percent of the weight of the wastewater.
5. The method for pretreating sucralose wastewater according to claim 1, wherein the method comprises the following steps: and (4) in the step (3), the diameter of the micropores on the membrane surface of the membrane separation device is 0.5-10 nm.
6. The method for pretreating sucralose waste water according to any one of claims 1-5, wherein: in the step (3), the salt content of the organic low-salt wastewater is below 500mg/L, and the CODcr is 35000-48000 mg/L.
7. The method for pretreating sucralose waste water according to any one of claims 1-5, wherein: the CODcr of the inorganic high-salinity wastewater in the step (3) is 8000mg/L of 5000-.
8. The method for pretreating sucralose waste water according to any one of claims 1-5, wherein: CODcr of evaporated condensed water (after mixing) from the MVR evaporator in the step (3) is below 20000 mg/L.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113603293A (en) * | 2021-07-29 | 2021-11-05 | 汪春雨 | Treatment process of sewage manure urinal |
| CN114230085A (en) * | 2021-12-20 | 2022-03-25 | 安徽金禾实业股份有限公司 | Method for deep treatment and desalination of sucralose wastewater |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN113603293A (en) * | 2021-07-29 | 2021-11-05 | 汪春雨 | Treatment process of sewage manure urinal |
| CN114230085A (en) * | 2021-12-20 | 2022-03-25 | 安徽金禾实业股份有限公司 | Method for deep treatment and desalination of sucralose wastewater |
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