CN117430294B - Ion exchange salt-containing washing water recycling system and method - Google Patents
Ion exchange salt-containing washing water recycling system and method Download PDFInfo
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- CN117430294B CN117430294B CN202311744239.5A CN202311744239A CN117430294B CN 117430294 B CN117430294 B CN 117430294B CN 202311744239 A CN202311744239 A CN 202311744239A CN 117430294 B CN117430294 B CN 117430294B
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 338
- 238000005406 washing Methods 0.000 title claims abstract description 189
- 150000003839 salts Chemical class 0.000 title claims abstract description 100
- 238000005342 ion exchange Methods 0.000 title claims abstract description 98
- 238000004064 recycling Methods 0.000 title claims abstract description 65
- 238000000034 method Methods 0.000 title claims abstract description 31
- 229920002472 Starch Polymers 0.000 claims abstract description 79
- 235000019698 starch Nutrition 0.000 claims abstract description 79
- 239000008107 starch Substances 0.000 claims abstract description 79
- 238000001223 reverse osmosis Methods 0.000 claims abstract description 67
- 239000012267 brine Substances 0.000 claims abstract description 58
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 claims abstract description 58
- 239000012153 distilled water Substances 0.000 claims abstract description 22
- 239000012466 permeate Substances 0.000 claims abstract description 20
- 240000008042 Zea mays Species 0.000 claims abstract description 18
- 235000005824 Zea mays ssp. parviglumis Nutrition 0.000 claims abstract description 18
- 235000002017 Zea mays subsp mays Nutrition 0.000 claims abstract description 18
- 235000005822 corn Nutrition 0.000 claims abstract description 18
- 238000002791 soaking Methods 0.000 claims abstract description 12
- 238000001704 evaporation Methods 0.000 claims description 16
- 238000007599 discharging Methods 0.000 claims description 8
- 238000001816 cooling Methods 0.000 claims description 5
- 238000002156 mixing Methods 0.000 claims description 5
- 239000002994 raw material Substances 0.000 claims description 5
- 230000009467 reduction Effects 0.000 abstract description 10
- 239000002351 wastewater Substances 0.000 abstract description 9
- 238000004134 energy conservation Methods 0.000 abstract description 6
- 238000003860 storage Methods 0.000 description 17
- 239000003513 alkali Substances 0.000 description 15
- 230000008020 evaporation Effects 0.000 description 13
- 230000000694 effects Effects 0.000 description 10
- 241001465754 Metazoa Species 0.000 description 9
- 230000008929 regeneration Effects 0.000 description 9
- 238000011069 regeneration method Methods 0.000 description 9
- 102000004169 proteins and genes Human genes 0.000 description 7
- 108090000623 proteins and genes Proteins 0.000 description 7
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 6
- 239000000498 cooling water Substances 0.000 description 6
- 238000004519 manufacturing process Methods 0.000 description 6
- 239000008213 purified water Substances 0.000 description 6
- 238000003756 stirring Methods 0.000 description 6
- 238000000746 purification Methods 0.000 description 5
- 239000000243 solution Substances 0.000 description 5
- NWUYHJFMYQTDRP-UHFFFAOYSA-N 1,2-bis(ethenyl)benzene;1-ethenyl-2-ethylbenzene;styrene Chemical compound C=CC1=CC=CC=C1.CCC1=CC=CC=C1C=C.C=CC1=CC=CC=C1C=C NWUYHJFMYQTDRP-UHFFFAOYSA-N 0.000 description 4
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 4
- 230000009286 beneficial effect Effects 0.000 description 4
- 239000003456 ion exchange resin Substances 0.000 description 4
- 229920003303 ion-exchange polymer Polymers 0.000 description 4
- 235000015097 nutrients Nutrition 0.000 description 4
- 230000003204 osmotic effect Effects 0.000 description 4
- 230000008569 process Effects 0.000 description 4
- 238000010586 diagram Methods 0.000 description 3
- 238000001914 filtration Methods 0.000 description 3
- 239000012528 membrane Substances 0.000 description 3
- 239000006227 byproduct Substances 0.000 description 2
- 230000005611 electricity Effects 0.000 description 2
- 238000005374 membrane filtration Methods 0.000 description 2
- 239000011347 resin Substances 0.000 description 2
- 229920005989 resin Polymers 0.000 description 2
- 239000011780 sodium chloride Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 229930192334 Auxin Natural products 0.000 description 1
- 241000894006 Bacteria Species 0.000 description 1
- 229920002261 Corn starch Polymers 0.000 description 1
- 229920002527 Glycogen Polymers 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 239000002363 auxin Substances 0.000 description 1
- 239000000084 colloidal system Substances 0.000 description 1
- 239000002131 composite material Substances 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 239000008120 corn starch Substances 0.000 description 1
- 238000005202 decontamination Methods 0.000 description 1
- 230000003588 decontaminative effect Effects 0.000 description 1
- 238000010612 desalination reaction Methods 0.000 description 1
- 238000011033 desalting Methods 0.000 description 1
- 238000007865 diluting Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 229940096919 glycogen Drugs 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 150000002500 ions Chemical class 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000006386 neutralization reaction Methods 0.000 description 1
- 235000016709 nutrition Nutrition 0.000 description 1
- 230000035764 nutrition Effects 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 230000001376 precipitating effect Effects 0.000 description 1
- 239000002243 precursor Substances 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 230000001737 promoting effect Effects 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
- 239000012498 ultrapure water Substances 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
Classifications
-
- 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
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J49/00—Regeneration or reactivation of ion-exchangers; Apparatus therefor
- B01J49/60—Cleaning or rinsing ion-exchange beds
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J49/00—Regeneration or reactivation of ion-exchangers; Apparatus therefor
- B01J49/70—Regeneration or reactivation of ion-exchangers; Apparatus therefor for large scale industrial processes or applications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/42—Treatment of water, waste water, or sewage by ion-exchange
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/041—Treatment of water, waste water, or sewage by heating by distillation or evaporation by means of vapour compression
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/441—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by reverse osmosis
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/34—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32
- C02F2103/36—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32 from the manufacture of organic compounds
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2303/00—Specific treatment goals
- C02F2303/14—Maintenance of water treatment installations
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The invention provides an ion exchange salt-containing washing water recycling system and method, comprising a low-salt washing water tank, a multi-salt washing water tank, a reverse osmosis device and an MVR evaporator; the low-salt washing water tank is used for collecting low-salt washing water; the multi-salt washing water tank is used for collecting multi-salt washing water; the reverse osmosis device is used for processing the low-salt washing water to obtain permeate water and reverse osmosis concentrated water, wherein the permeate water is returned to the starch sugar ion exchange system for recycling, and the reverse osmosis concentrated water enters the multi-salt washing water tank; the MVR evaporator is used for processing the multi-salt washing water and the reverse osmosis concentrated water together to obtain distilled water and concentrated brine; wherein, distilled water is returned to the starch sugar ion exchange system for recycling, and the strong brine is merged into a corn soaking water evaporator of a starch sugar feed starch workshop for recycling. The ion exchange salt-containing washing water recycling system and method provided by the invention can reduce the treatment cost of ion exchange salt-containing washing water, promote energy conservation and emission reduction, and realize zero wastewater discharge in the starch sugar industry.
Description
Technical Field
The invention belongs to the technical field of water treatment, and particularly relates to an ion exchange salt-containing washing water recycling system and method.
Background
In the current processing process of producing starch sugar by using starch as a raw material, although many enterprises begin to adopt countercurrent-like continuous ion exchange to remove salt impurities in sugar liquor, so that the amount of ion exchange salt-containing (mainly sodium chloride) washing water generated during regeneration of ion exchange resin is greatly reduced, the generation amount of salt-containing washing water is still 0.5-3.0 tons (the difference of the amount is mainly caused by different desalting burdens due to the difference of starch sugar varieties or raw materials) per ton of starch sugar dry matter produced, the yield of starch sugar of about three tens of millions of tons per year is realized in the whole industry of China, and the total amount of salt-containing washing water is in the class of fifty to sixty thousand tons. The current salt-containing washing water in the starch sugar industry has no good application, and can only be sent to a decontamination water station for treatment and discharge after reaching standards, and the cost of the discharge of the salt-containing washing water of most enterprises is calculated to be more than ten yuan per ton. Therefore, how to realize water conservation and emission reduction is a great subject in the starch sugar industry, and the realization of emission reduction from the production line source is an optimal way for reducing environmental pollution.
For this reason, those skilled in the art have attempted to purify the ion-exchanged brine by evaporation concentration and then repeat the resin regeneration wash for ion exchange to achieve emission reduction. However, the evaporation and concentration cost is high (the cost of evaporation and concentration is more than ten yuan per ton even by adopting an efficient and energy-saving MVR evaporator), and the difficulty of treating the concentrated brine obtained after concentration in a sewage station is higher, so that the scheme of reducing the emission of the ion exchange brine is not suitable to be implemented by adopting the evaporation and concentration method.
Those skilled in the art have also attempted to purify the ion exchange brine by membrane filtration and then use the purified water for ion exchange resin regeneration washing. However, the water yield of the scheme is low, the purified water obtained under normal conditions is less than sixty percent, and the problem that the strong brine cannot be reasonably treated also exists, so that the scheme for reducing the emission of the ion exchange brine is not suitable to be implemented by a membrane filtration method.
Therefore, there is a need in the industry to develop a technology capable of realizing the recycling of the ion exchange brine at low cost, promoting the energy conservation and emission reduction of the starch sugar production and relieving the environmental protection pressure of the industry.
Disclosure of Invention
The embodiment of the invention provides a system and a method for recycling ion exchange salt-containing washing water, which aim to reduce the treatment cost of the ion exchange salt-containing washing water and promote energy conservation and emission reduction.
In order to achieve the above purpose, the invention adopts the following technical scheme: in a first aspect, an ion exchange salt-containing wash water recycling system is provided, comprising a low-salt wash water tank, a multi-salt wash water tank, a reverse osmosis device and an MVR evaporator; the low-salt washing water tank is used for connecting a starch sugar ion exchange system and collecting low-salt washing water in a low-salt period; the multi-salt washing water tank is used for connecting a starch sugar ion exchange system and collecting multi-salt washing water in a multi-salt period; the reverse osmosis device is connected with the low-salt washing water tank and the multi-salt washing water tank, and is used for processing the low-salt washing water to obtain permeate water and reverse osmosis concentrated water, wherein the permeate water is returned to the starch sugar ion exchange system for recycling, and the reverse osmosis concentrated water enters the multi-salt washing water tank; the MVR evaporator is connected with the multi-salt washing water tank and the starch sugar ion exchange system, and is used for processing the multi-salt washing water and the reverse osmosis concentrated water together to obtain distilled water and concentrated brine; wherein, distilled water is returned to the starch sugar ion exchange system for recycling, and the strong brine is merged into a corn soaking water evaporator of a starch sugar feed starch workshop for recycling.
With reference to the first aspect, in one possible implementation manner, a heat exchanger is connected between the low-salt water washing tank and the reverse osmosis device, and cooling water circulates in the heat exchanger, and the cooling water is used for cooling the low-salt water washing flowing through the heat exchanger.
In some embodiments, a water storage tank is connected between the heat exchanger and the reverse osmosis device, and a metering pump is connected to the water storage tank and is used for quantitatively extracting alkali liquor into the water storage tank to neutralize low-salt washing water.
Illustratively, the low-salt water washing tank, the multi-salt water washing tank and the water storage tank are respectively provided with a stirring device.
The ion exchange salt-containing washing water recycling system provided by the invention has the beneficial effects that: compared with the prior art, the ion exchange salt-containing washing water recycling system has the advantages that the salt-containing washing water produced by the starch sugar ion exchange system is subjected to time-division collection treatment, the low-salt washing water is collected by the low-salt washing water tank, the multi-salt washing water is collected by the multi-salt washing water tank, so that the low-salt washing water can be directly treated by the reverse osmosis device, the permeate water produced after the treatment is directly returned to the starch sugar ion exchange system for recycling, the reverse osmosis concentrated water is mixed into the multi-salt washing water and is evaporated and concentrated by the MVR evaporator, distilled water and a small amount of concentrated brine which can be recycled by the starch sugar ion exchange system are obtained, the concentrated brine is mixed into the corn soaking water evaporator of the starch sugar feed starch workshop for recycling, the whole recycling of the ion exchange salt-containing washing water and the zero wastewater discharge are realized, the energy conservation and emission reduction effects are remarkable, the treatment capacity of the MVR evaporator can be greatly reduced by respectively treating the low-salt washing water and the multi-salt washing water, and the ion exchange salt-containing treatment cost can be greatly reduced, and the enterprise burden can be reduced.
In a second aspect, the embodiment of the invention also provides a method for recycling the ion exchange brine, which adopts the ion exchange brine recycling system and comprises the following steps:
discharging low-salt washing water generated by each ion-exchange column of the starch sugar ion-exchange system in a low-salt period into a low-salt washing water tank, and discharging multi-salt washing water generated by each ion-exchange column of the starch sugar ion-exchange system in a multi-salt period into a multi-salt washing water tank;
treating the low-salt washing water by a reverse osmosis device to obtain permeate water and reverse osmosis concentrated water; wherein, the permeate water returns to the starch sugar ion exchange system for recycling, and the reverse osmosis concentrated water is discharged into a multi-salt water washing tank and mixed with the multi-salt water washing;
evaporating and concentrating the mixed reverse osmosis concentrated water and multi-salt washing water through an MVR evaporator to obtain distilled water and concentrated brine;
and returning distilled water to the starch sugar ion exchange system for recycling, and discharging the strong brine into a corn soaking water evaporator of a starch sugar raw material starch workshop for recycling.
With reference to the second aspect, in one possible implementation manner, a ratio of the low-salt wash water discharged into the low-salt wash water tank to the multi-salt wash water discharged into the multi-salt wash water tank is four to one.
For example, the salt content of the low-salt washing water is 0.18-0.22%, and the salt content of the multi-salt washing water is 1.8-2.2%.
The total dry matter concentration of the strong brine is 28-35%, and the salt content is 18-22%.
In some embodiments, the reverse osmosis unit further comprises, prior to the low salt wash water treatment: and carrying out heat exchange cooling on the low-salt washing water through a heat exchanger.
In some embodiments, the reverse osmosis unit further comprises, prior to the low salt wash water treatment: mixing alkali liquor in the low-salt washing water to neutralize the acidity of the low-salt washing water.
The method for recycling the ion exchange salt-containing washing water has the beneficial effects that: compared with the prior art, the method for recycling the ion exchange salt-containing washing water has the advantages that the low-salt washing water generated by the starch sugar ion exchange system can be subjected to reverse osmosis treatment by using the ion exchange salt-containing washing water recycling system to obtain the permeate water and the reverse osmosis concentrated water, and the multi-salt washing water generated by the reverse osmosis concentrated water and the starch sugar ion exchange system is subjected to evaporation concentration treatment by using the MVR evaporator to obtain the distilled water and the concentrated brine, wherein the permeate water and the distilled water can be directly returned to the starch sugar ion exchange system as the purified water for recycling, and the concentrated brine is merged into the corn soaking water evaporator of the starch sugar starch workshop for recycling, so that not only can the whole recycling of the ion exchange salt-containing washing water and zero wastewater discharge be realized, but also the energy saving and emission reduction effects are obvious, and the MVR evaporator only needs to evaporate and concentrate the multi-salt washing water and the reverse osmosis concentrated water which occupy a relatively small amount, so that the total treatment cost of the ion exchange salt-containing washing water can be greatly reduced, and the burden of enterprises can be lightened.
Drawings
FIG. 1 is a schematic diagram of a system for recycling ion exchange brine in accordance with an embodiment of the present invention;
FIG. 2 is a block diagram showing steps of a method for recycling ion exchange brine according to an embodiment of the present invention;
FIG. 3 is a block diagram II of a method for recycling ion exchange brine.
In the figure: 1. a low salt water washing tank; 2. a multi-salt water washing tank; 3. a reverse osmosis device; 4. an MVR evaporator; 5. a heat exchanger; 6. a water storage tank; 7. a metering pump; 8. an alkali liquor storage tank; 9. and a stirring device.
Detailed Description
In order to make the technical problems, technical schemes and beneficial effects to be solved more clear, the invention is further described in detail below with reference to the accompanying drawings and embodiments. It should be understood that the specific embodiments described herein are for purposes of illustration only and are not intended to limit the scope of the invention.
Referring to fig. 1 and 2, an ion exchange salt-containing washing water recycling system provided by the invention will now be described. The ion exchange salt-containing washing water recycling system comprises a low-salt washing water tank 1, a multi-salt washing water tank 2, a reverse osmosis device 3 and an MVR evaporator 4; the low-salt water washing tank 1 is used for connecting a starch sugar ion exchange system and collecting low-salt water washing in a low-salt period; the multi-salt water washing tank 2 is used for connecting a starch sugar ion exchange system and collecting multi-salt water washing water in a multi-salt period; the reverse osmosis device 3 is connected with the low-salt water washing tank 1 and the multi-salt water washing tank 2, and the reverse osmosis device 3 is used for processing low-salt water washing to obtain permeate water and reverse osmosis concentrated water, wherein the permeate water is returned to the starch sugar ion exchange system for recycling, and the reverse osmosis concentrated water enters the multi-salt water washing tank 2; the MVR evaporator 4 is connected with the multi-salt water washing tank 2 and connected with a starch sugar ion exchange system, and the MVR evaporator 4 is used for processing multi-salt water washing and reverse osmosis concentrated water together to obtain distilled water and concentrated brine; wherein, distilled water is returned to the starch sugar ion exchange system for recycling, and the strong brine is merged into a corn soaking water evaporator of a starch sugar feed starch workshop for recycling.
It should be noted that, in this embodiment, the starch sugar ion exchange system is the prior art, and mainly includes a plurality of ion exchange columns cascaded in turn, each ion exchange column generates brine with different concentrations in different regeneration washing periods, in this embodiment, the salt content of the salt-containing washing water produced in the low salt period of the regeneration washing of each ion exchange column is about 0.18-0.22%, i.e. the low salt washing water, and the salt content of the salt-containing washing water produced in the multi-salt period of the regeneration washing of each ion exchange column is 1.8-2.2%, i.e. the multi-salt washing water, the low salt washing water is collected in the low salt period by the low salt washing water tank 1, and the multi-salt washing water is collected in the multi-salt period by the multi-salt washing water tank 2, thereby achieving the purpose of collecting the brine with different concentrations in different periods for corresponding treatment.
It should be explained that the reverse osmosis device 3 is a mature device which is used in the preparation of high purity water, desalination of brackish water and wastewater treatment technology, and is a mature device which can effectively remove charged ions, inorganic matters, colloid particles, bacteria, organic matters and the like in water, and the working principle of the reverse osmosis device is not described in detail herein; the low-salt washing water passes through a reverse osmosis device 3 to obtain high-quality pure osmosis water and reverse osmosis concentrated water, wherein the reverse osmosis concentrated water is equivalent to brine with higher salt content, is discharged into a multi-salt washing water tank 2, is mixed with the multi-salt washing water, and is subjected to MVR evaporation concentration, and the osmosis water can be directly returned to a starch sugar ion exchange system for recycling and reutilization, and is mainly used for the process of ion exchange resin regeneration washing.
The MVR evaporator 4 is also a conventional mature device, and the product of the multi-salt washing water with higher salt content after MVR evaporation concentration is distilled water and strong brine, and the working principle thereof is not described in detail here. The distilled water after evaporation and concentration can be directly returned to an ion exchange resin regeneration washing unit of a starch sugar ion exchange system for recycling, the strong brine mainly contains about 20% of salt, about 5-8% of sugar and about 3-7% of protein, and the total dry matter concentration of the mixed water is about 32%, so that the mixed water can be utilized in a corn steep water evaporator (used for producing corn steep liquor, which is a byproduct of corn starch and contains abundant soluble proteins, auxins and some precursor substances) in a starch workshop, and can be used as an action feed, the corn steep water evaporator is usually a multi-effect evaporator, and the strong brine can be particularly incorporated into the end effect of the multi-effect evaporator, and the concentration of the salt in the strong brine can be diluted by hundreds of times and then fed into a proper animal feeding concentration, and the sugar and the protein contained in the strong brine can also increase nutrition of the corn steep liquor as animal feed.
Therefore, the method realizes the full recycling of the salt-containing washing water produced by the starch sugar ion exchange system, solves the difficult problems of pollution-free treatment and recycling of the strong brine, avoids the generation of waste water from the production source, and is an effective and practical excellent scheme for realizing zero waste water emission in the starch sugar processing industry.
Compared with the prior art, the ion exchange salt-containing washing water recycling system provided by the embodiment is characterized in that the salt-containing washing water produced by the starch sugar ion exchange system is subjected to time-division collection treatment, the low-salt washing water is collected by the low-salt washing water tank 1, the multi-salt washing water is collected by the multi-salt washing water tank 2, so that the low-salt washing water can be directly treated by the reverse osmosis device 3, the permeate water produced after the treatment is directly returned to the starch sugar ion exchange system for recycling, the reverse osmosis concentrated water is mixed into the multi-salt washing water and is evaporated and concentrated by the MVR evaporator 4, distilled water and a small amount of concentrated brine which can be recycled by the starch sugar ion exchange system are obtained, the concentrated brine is merged into the corn soaking water evaporator of a starch sugar raw starch workshop for recycling, the whole recycling of the ion exchange salt-containing washing water and the zero wastewater discharge are realized, the energy conservation and emission reduction effects are remarkable, the treatment amount of the MVR evaporator 4 can be greatly reduced by respectively treating the low-salt washing water and the multi-salt washing water, and the processing cost of the ion exchange salt-containing washing water can be greatly reduced.
In some embodiments, referring to fig. 2, a heat exchanger 5 is connected between the low-salt wash water tank 1 and the reverse osmosis device 3, and cooling water circulates in the heat exchanger 5, wherein the cooling water is used for cooling the low-salt wash water flowing through the heat exchanger 5. The heat exchanger 5 can be a plate heat exchanger, and the cooling water circularly flowing through the heat exchanger 5 exchanges heat with the low-salt washing water passing through the heat exchanger 5, so that the low-salt washing water is cooled and then enters the reverse osmosis device 3, and the influence on the permeation effect caused by expansion (filtration Kong Biancu) of a filter membrane in the reverse osmosis device 3 due to the fact that the temperature of the low-salt washing water is too high is avoided.
In some possible implementations, referring to fig. 1, a water storage tank 6 is connected between the heat exchanger 5 and the reverse osmosis device 3, a metering pump 7 is connected to the water storage tank 6, and the metering pump 7 is used for quantitatively extracting alkali liquor from the water storage tank 6 to neutralize low-salt washing water. Because the low-salt washing water has weak acidity, alkali liquor is mixed into the low-salt washing water in the water storage tank 6 before entering the reverse osmosis device 3 to neutralize the acidity of the low-salt washing water, so that the osmotic water generated after osmotic filtration by the reverse osmosis device 3 is ensured to be directly recycled to the starch sugar ion exchange system; specifically, in this embodiment, the alkali solution may be sodium hydroxide with thirty percent concentration contained in the alkali solution storage tank 8, and a fixed amount of alkali solution is pumped into the water storage tank 6 by the metering pump 7 according to the amount of low-salt washing water in the water storage tank 6, so that the low-salt washing water is neutralized with the alkali solution in the water storage tank 6.
Specifically, as shown in fig. 1, in this embodiment, stirring devices 9 are disposed in the low-salt water tank 1, the multi-salt water tank 2, and the water storage tank 6. The stirring device 9 is arranged, so that the low-salt washing water can be prevented from precipitating in the low-salt washing water tank 1, the mixing uniformity of the low-salt washing water is ensured, the low-salt washing water (with a certain salt content) entering the water storage tank 6 can be completely neutralized with the alkali liquor which is quantitatively extracted, and the influence of acidity or alkalinity on the liquid entering the reverse osmosis device 3 on the recycling of the permeate water is avoided; the low-salt washing water and the alkali liquor are stirred in the water storage tank 6 through the stirring device 9, so that the neutralization reaction efficiency can be improved, and the low-salt washing water and the alkali liquor can be completely neutralized; reverse osmosis dense water and multi-salt wash water are stirred and mixed in the multi-salt wash water tank 2 through the stirring device 9, so that the concentration uniformity of the solution in the multi-salt wash water tank 2 can be ensured, and the evaporation concentration efficiency and quality of the MVR evaporator 4 can be improved.
Based on the same inventive concept, the embodiment of the application also provides an ion exchange salt-containing washing water recycling method, which adopts the ion exchange salt-containing washing water recycling system and specifically comprises the following steps:
step S100, discharging low-salt washing water generated by each ion exchange column of the starch sugar ion exchange system in a low-salt period into a low-salt washing water tank 1, and discharging multi-salt washing water generated by each ion exchange column of the starch sugar ion exchange system in a multi-salt period into a multi-salt washing water tank 2;
step S200, treating low-salt washing water through a reverse osmosis device 3 to obtain permeate water and reverse osmosis concentrated water; wherein, the permeate water returns to the starch sugar ion exchange system for recycling, and the reverse osmosis concentrated water is discharged into the multi-salt washing water tank 2 and mixed with the multi-salt washing water;
step S300, evaporating and concentrating the mixed reverse osmosis concentrated water and multi-salt washing water through an MVR evaporator 4 to obtain distilled water and concentrated brine;
and step S400, returning distilled water to the starch sugar ion exchange system for recycling, and discharging the strong brine into a corn soaking water evaporator of a starch sugar raw material starch workshop for recycling.
Compared with the prior art, the method for recycling the ion exchange salt-containing washing water provided by the embodiment has the advantages that the salt-containing washing water generated by the starch sugar ion exchange system is collected in a time-sharing manner, the low-salt washing water with higher yield can be subjected to reverse osmosis treatment to obtain the permeable water which can be directly recycled, the reverse osmosis concentrated water with higher salt content and the multi-salt washing water with lower yield are mixed and then evaporated and concentrated by the MVR evaporator 4 to obtain the distilled water which can be directly recycled, and meanwhile, the concentrated brine generated by the MVR evaporator 4 is used for diluting by the corn soaking water evaporator and then is recycled as animal feed, so that the whole recycling of the salt-containing washing water and the zero-wastewater discharge production of starch sugar are realized, the energy conservation and the emission reduction are facilitated, and the total treatment cost of the ion exchange salt-containing washing water can be greatly reduced and the enterprise burden is lightened because the cost of the reverse osmosis process is lower than that of the MVR evaporation and concentration process.
Specifically, in the above step S100, the ratio of the low-salt wash water discharged into the low-salt wash water tank 1 to the multi-salt wash water discharged into the multi-salt wash water tank 2 is four to one. By controlling the production process of the starch sugar ion exchange system, washing water with different salt concentration is collected in different time periods, washing water with higher salt content is produced in a multi-salt period under normal conditions, the salt content of washing water with salt produced in a low-salt period is low and large, and finally, the collection ratio of the washing water with low salt content to the washing water with multi-salt content is four to one, so that the method is optimal in economical efficiency and treatment effect.
For example, in this embodiment, the salt content of the low-salt wash water is 0.18-0.22%, and the salt content of the multi-salt wash water is 1.8-2.2%. Specifically, the low-salt washing water with the salt content of 0.2% is collected in the low-salt period for reverse osmosis treatment, and the multi-salt washing water with the salt content of 2.0% is collected in the multi-salt period for MVR evaporation concentration treatment, so that the treatment effect is good and the economy is good.
The total dry matter concentration of the strong brine in the embodiment is 28-35%, and the salt content is 18-22%. Specifically, the strong brine produced after MVR evaporation and concentration is about 20% in salt content, 5-8% in sugar content and about 3-7% in protein content, wherein sugar and protein can be used as nutrient substances of animal feed, and the salt concentration is too high to be directly fed by animals, so that the strong brine is integrated into a corn soaking water evaporator of a starch glycogen starch workshop, specifically can be integrated into the tail effect of the corn soaking water evaporator, and the salt concentration in the strong brine can be diluted by hundreds of times to be suitable for direct feeding of animals, thereby realizing recycling and zero emission of the strong brine.
It should be noted that, before the step S200, the method further includes a step S101: the low-salt washing water is subjected to heat exchange and cooling through a heat exchanger 5. The cooling water circularly flowing through the heat exchanger 5 exchanges heat with the low-salt washing water passing through the heat exchanger 5, so that the low-salt washing water enters the reverse osmosis device 3 after being cooled, and the influence on the permeation effect caused by expansion of a filter membrane in the reverse osmosis device 3 due to overhigh temperature of the low-salt washing water is avoided.
It should be explained that the step S102 is further included before the step S200: mixing alkali liquor in the low-salt washing water to neutralize the acidity of the low-salt washing water. Specifically, the alkali liquor can adopt thirty percent sodium hydroxide, and the acidity of the low-salt washing water can be neutralized by mixing the alkali liquor into the low-salt washing water, so that the osmotic water generated after the osmotic filtration of the reverse osmosis device 3 can be ensured to be directly recycled to the starch sugar ion exchange system.
One specific example of the method for recycling the ion exchange salt-containing washing water provided in the embodiment is as follows:
for the total amount of the salt-containing washing water (comprising the low salt washing water amount produced in the low salt period and the multi-salt washing water amount produced in the multi-salt period) produced in the starch sugar ion exchange system, 80% of the salt-containing washing water is mainly containing sugar (the sugar content is 0.2-0.3%) and the salt is auxiliary (the salt content is about 0.2%), namely the low salt washing water; in addition, 20% of the salt-containing washing water is mainly containing salt (the salt content is about 2.0%) and the protein is auxiliary (the protein content is about 0.5-1.0%), namely multi-salt washing water, wherein the low-salt washing water and the multi-salt washing water are treated respectively by adopting different purification modes, 100 tons of salt-containing washing water is treated by adopting a reverse osmosis device 3 as an example, 80 tons of low-salt washing water can obtain at least 95%, namely 76 tons of high-quality permeate water and 4 tons of reverse osmosis concentrated water, and the purification cost (electricity containing cost and membrane assembly consumption cost) of each ton of permeate water is about 3 yuan; then 4 tons of reverse osmosis concentrated water and 20 tons of multi-salt washing water are combined and then evaporated and concentrated through an MVR evaporator 4, at least 21 tons of high-quality distilled water and 3 tons of concentrated brine can be obtained, the purification cost (electricity charge is main) of each ton of distilled water is about 12 yuan, the salt content of the finally obtained concentrated brine is about 20 percent, the sugar content is about 5-8 percent, the protein content is about 3-7 percent, and the total dry matter concentration is about 32 percent.
The purification cost of 76 tons of permeate water and 21 tons of distilled water is about 480 yuan for 97 tons of purified water, and the total cost is less than about 5 yuan per ton (the cost of the prior art is more than 10 yuan per ton), the water yield of the purified water is as high as 97 percent (the water yield of the prior art is less than 60 percent), and the purified water can be repeatedly used for resin regeneration washing in a starch sugar ion exchange system.
While the total dry matter concentration of 3 tons of concentrated brine was 32%, the salt (sodium chloride) was precipitated by continuing the evaporation concentration. In the method, sugar and protein contained in the strong brine are animal excellent nutrients, the salt is also animal nutrients, and the salt cannot be directly fed due to the fact that the salt concentration is too high, so that the effect of the corn steep water evaporator of a starch sugar raw starch workshop is achieved by combining 3 tons of strong brine, the salt concentration can be diluted hundreds of times and enter the proper animal feeding concentration, the problem of the outlet of the strong brine is solved, and meanwhile, the sugar and the protein also increase the feed nutrients of corn steep liquor.
In the embodiment, the method of reverse osmosis and MVR composite purification of the ion exchange salt-containing washing water realizes low-cost recycling of the ion exchange salt-containing washing water in the starch sugar industry, solves the pollution-free comprehensive utilization outlet of purified byproduct strong brine, eliminates the generation of wastewater from a production line source head, is an effective method for realizing zero wastewater discharge in the starch sugar industry, and is beneficial to popularization and application.
The foregoing description of the preferred embodiments of the invention is not intended to be limiting, but rather is intended to cover all modifications, equivalents, and alternatives falling within the spirit and principles of the invention.
Claims (5)
1. The method for recycling the ion exchange salt-containing washing water is characterized by comprising the following steps of:
discharging low-salt washing water generated by each ion exchange column of the starch sugar ion exchange system in a low-salt period into a low-salt washing water tank, and discharging multi-salt washing water generated by each ion exchange column of the starch sugar ion exchange system in a multi-salt period into a multi-salt washing water tank;
treating the low-salt washing water by a reverse osmosis device to obtain permeate water and reverse osmosis concentrated water; wherein the permeate water is returned to the starch sugar ion exchange system for recycling, and the reverse osmosis concentrated water is discharged into the multi-salt washing water tank and mixed with the multi-salt washing water;
evaporating and concentrating the mixed reverse osmosis concentrated water and the multi-salt washing water through an MVR evaporator to obtain distilled water and concentrated brine; the total dry matter concentration of the strong brine is 28-35%, wherein the salt content is 18-22%, the sugar content is 5-8%, and the protein content is 3-7%;
and returning the distilled water to the starch sugar ion exchange system for recycling, and merging the strong brine into a corn soaking water evaporator of a starch raw material starch workshop for recycling.
2. The method for recycling of ion exchange brine wash water according to claim 1, wherein a ratio of the low-salt wash water discharged into the low-salt wash water tank to the multi-salt wash water discharged into the multi-salt wash water tank is four to one.
3. The method for recycling the ion exchange brine is characterized in that the salt content of the low-salt brine is 0.18-0.22%, and the salt content of the multi-salt brine is 1.8-2.2%.
4. A method of recycling the wash water comprising salt of any one of claims 1 to 3, further comprising, prior to the reverse osmosis unit treating the wash water comprising low salt: and carrying out heat exchange cooling on the low-salt washing water through a heat exchanger.
5. A method of recycling the wash water comprising salt of any one of claims 1 to 3, further comprising, prior to the reverse osmosis unit treating the wash water comprising low salt: mixing lye in the low-salt wash water to neutralize the acidity of the low-salt wash water.
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| CN106365251A (en) * | 2016-08-25 | 2017-02-01 | 山东省鲁洲食品集团有限公司 | Recovery method for starch syrup ion exchange material pressing water |
| CN114620877A (en) * | 2022-02-24 | 2022-06-14 | 杭州上拓环境科技股份有限公司 | Treatment system, treatment method and application of ternary material washing water |
| CN218290682U (en) * | 2022-10-20 | 2023-01-13 | 武汉友谊兴泰科技有限公司 | Zero-discharge comprehensive treatment system for starch sugar workshop wastewater |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN106365251A (en) * | 2016-08-25 | 2017-02-01 | 山东省鲁洲食品集团有限公司 | Recovery method for starch syrup ion exchange material pressing water |
| CN114620877A (en) * | 2022-02-24 | 2022-06-14 | 杭州上拓环境科技股份有限公司 | Treatment system, treatment method and application of ternary material washing water |
| CN218290682U (en) * | 2022-10-20 | 2023-01-13 | 武汉友谊兴泰科技有限公司 | Zero-discharge comprehensive treatment system for starch sugar workshop wastewater |
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