CN104724873A - Method for realizing zero discharge and resource utilization of production waste water of white carbon black - Google Patents
Method for realizing zero discharge and resource utilization of production waste water of white carbon black Download PDFInfo
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- CN104724873A CN104724873A CN201510095862.1A CN201510095862A CN104724873A CN 104724873 A CN104724873 A CN 104724873A CN 201510095862 A CN201510095862 A CN 201510095862A CN 104724873 A CN104724873 A CN 104724873A
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- carbon black
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- 238000000034 method Methods 0.000 title claims abstract description 39
- 239000002351 wastewater Substances 0.000 title claims abstract description 30
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 title claims abstract description 24
- 239000006229 carbon black Substances 0.000 title claims abstract description 24
- 238000004519 manufacturing process Methods 0.000 title abstract 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 66
- AMXOYNBUYSYVKV-UHFFFAOYSA-M lithium bromide Chemical compound [Li+].[Br-] AMXOYNBUYSYVKV-UHFFFAOYSA-M 0.000 claims abstract description 60
- 238000001728 nano-filtration Methods 0.000 claims abstract description 32
- 238000001704 evaporation Methods 0.000 claims abstract description 28
- 230000008020 evaporation Effects 0.000 claims abstract description 27
- 238000001223 reverse osmosis Methods 0.000 claims abstract description 20
- 239000007788 liquid Substances 0.000 claims abstract description 17
- 239000012452 mother liquor Substances 0.000 claims abstract description 15
- 238000000108 ultra-filtration Methods 0.000 claims abstract description 13
- 238000001556 precipitation Methods 0.000 claims abstract description 4
- 239000000243 solution Substances 0.000 claims description 54
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 claims description 27
- 229940059936 lithium bromide Drugs 0.000 claims description 27
- WHXSMMKQMYFTQS-UHFFFAOYSA-N Lithium Chemical compound [Li] WHXSMMKQMYFTQS-UHFFFAOYSA-N 0.000 claims description 26
- 229910052744 lithium Inorganic materials 0.000 claims description 26
- 239000010842 industrial wastewater Substances 0.000 claims description 20
- 238000004064 recycling Methods 0.000 claims description 18
- 229910052938 sodium sulfate Inorganic materials 0.000 claims description 17
- 235000011152 sodium sulphate Nutrition 0.000 claims description 17
- 239000006200 vaporizer Substances 0.000 claims description 14
- 239000013505 freshwater Substances 0.000 claims description 12
- 238000005189 flocculation Methods 0.000 claims description 11
- 230000016615 flocculation Effects 0.000 claims description 11
- 238000001914 filtration Methods 0.000 claims description 10
- 239000012141 concentrate Substances 0.000 claims description 9
- 239000013049 sediment Substances 0.000 claims description 8
- 239000000126 substance Substances 0.000 claims description 8
- 238000009833 condensation Methods 0.000 claims description 7
- 230000005494 condensation Effects 0.000 claims description 7
- 239000000047 product Substances 0.000 claims description 7
- 238000005119 centrifugation Methods 0.000 claims description 6
- 239000000706 filtrate Substances 0.000 claims description 6
- 239000007789 gas Substances 0.000 claims description 6
- JEGUKCSWCFPDGT-UHFFFAOYSA-N h2o hydrate Chemical compound O.O JEGUKCSWCFPDGT-UHFFFAOYSA-N 0.000 claims description 6
- 238000010438 heat treatment Methods 0.000 claims description 6
- 238000002203 pretreatment Methods 0.000 claims description 6
- 238000010521 absorption reaction Methods 0.000 claims description 3
- 238000010790 dilution Methods 0.000 claims description 3
- 239000012895 dilution Substances 0.000 claims description 3
- 239000002440 industrial waste Substances 0.000 claims description 3
- 238000002425 crystallisation Methods 0.000 abstract description 16
- 230000008025 crystallization Effects 0.000 abstract description 8
- 239000013078 crystal Substances 0.000 abstract description 4
- 238000005265 energy consumption Methods 0.000 abstract description 4
- 239000006096 absorbing agent Substances 0.000 abstract 3
- 238000013327 media filtration Methods 0.000 abstract 1
- 239000002244 precipitate Substances 0.000 abstract 1
- 239000004576 sand Substances 0.000 abstract 1
- 238000001816 cooling Methods 0.000 description 12
- 238000005516 engineering process Methods 0.000 description 4
- 230000008014 freezing Effects 0.000 description 4
- 238000007710 freezing Methods 0.000 description 4
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- 238000007906 compression Methods 0.000 description 2
- LCPVQAHEFVXVKT-UHFFFAOYSA-N 2-(2,4-difluorophenoxy)pyridin-3-amine Chemical compound NC1=CC=CN=C1OC1=CC=C(F)C=C1F LCPVQAHEFVXVKT-UHFFFAOYSA-N 0.000 description 1
- 210000000746 body region Anatomy 0.000 description 1
- 239000012267 brine Substances 0.000 description 1
- 235000011389 fruit/vegetable juice Nutrition 0.000 description 1
- 239000008235 industrial water Substances 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 239000010413 mother solution Substances 0.000 description 1
- 238000005192 partition Methods 0.000 description 1
- 238000011020 pilot scale process Methods 0.000 description 1
- 238000005057 refrigeration Methods 0.000 description 1
- 239000011734 sodium Substances 0.000 description 1
- 239000011780 sodium chloride Substances 0.000 description 1
- CHQMHPLRPQMAMX-UHFFFAOYSA-L sodium persulfate Substances [Na+].[Na+].[O-]S(=O)(=O)OOS([O-])(=O)=O CHQMHPLRPQMAMX-UHFFFAOYSA-L 0.000 description 1
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 description 1
- 230000005068 transpiration Effects 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
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- Separation Using Semi-Permeable Membranes (AREA)
- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
Abstract
The invention discloses a method for realizing zero discharge and resource utilization of production waste water of white carbon black. The waste water is pretreated to adjust the pH value, sand clear liquid and a flocculent precipitate turbidity solution are obtained through flocculent precipitation, the clear liquid is subjected to porous media filtration, ultrafiltration and nanofiltration to obtain concentrated water, the concentrated water is precooled after entering a heat exchanger, and plain water obtained after nanofiltration is further diluted through reverse osmosis. The precooled concentrated water is subjected to evaporative crystallization after entering a crystallizer, and evaporated water steam flows into an absorber so as to be absorbed by a lithium bromide solution; mother liquor separated from a magma enters the heat exchanger so as to be subjected to heat exchange with the concentrated water subjected to nanofiltration, and then is subjected to nanofiltration and concentration. The lithium bromide diluted solution in the absorber is transferred into an evaporator, and the lithium bromide concentrated solution obtained after evaporation and concentration is returned into the absorber again, and the water steam is condensed and recycled. According to the method disclosed by the invention, no cold source is needed, the energy consumption is reduced, meanwhile crystal attachment in septate heat transfer is avoided, and the recycle of the plain water is realized through reverse osmosis; the whole process is closed and cyclical, so that the purposes of zero discharge and resource utilization of the production waste water of the white carbon black are realized.
Description
Technical field
The present invention relates to wastewater treatment and application technology as the second resource, be specifically related to a kind of method of white carbon black industrial wastewater zero release and recycling, belong to technical field of waste water processing.
Background technology
Utilize producing white carbon black using settling method usually can discharge the trade effluent of a large amount of contains sodium sulfate, its concentration is up to 20000mg/L-30000mg/L.If these waste water directly outer row not only destroy ecotope, and waste resource, if process this waste water; realize sodium sulfate to be separated with fresh water, fresh water reuse, sodium sulfate is as Product recycling; not only protect environment, also make it obtain recycling, realize considerable economic benefit.
" flocculation sediment+filtration+ultrafiltration+reverse osmosis " technique that process for white carbon black industrial wastewater adopts usually and " after reverse osmosis concentration+freezing and crystallizing or MVR thermo-compression evaporation or multiple-effect evaporation crystallization " technique.
" flocculation sediment+filtration+ultrafiltration+reverse osmosis " technological operation is simple, and energy consumption is lower, produce fresh water reuse, but the dense water after reverse osmosis concentrate is arranged outward, therefore can not realize the zero release of waste water.
" after reverse osmosis concentration+freezing and crystallizing or MVR thermo-compression evaporation or multiple-effect evaporation crystallization " technique is by after Waste water concentrating by reverse osmosis, fresh water reuse, dense water realizes being separated of sodium sulfate and water after freezing and crystallizing or evaporation technique process, but because these technology need to provide low-temperature receiver (usually adopting chilled brine), or consume the supercharging intensification that electric energy realizes secondary steam, or adopting raw steam to provide thermal source, treatment process energy consumption is high.Especially freezing and crystallizing, owing to adopting the partition type of cooling to realize refrigeration crystallization process, near crystallizer internal cold wall face, comparatively body region is low for temperature, makes crystal easily appear at cold near wall, and then causes the attached wall phenomenon of crystallization.
Summary of the invention
For prior art above shortcomings, the object of this invention is to provide that a kind of energy consumption is low, easy handling, the method for white carbon black industrial wastewater zero release and recycling can be realized.
Technical scheme of the present invention is achieved in that
A method for white carbon black industrial wastewater zero release and recycling, step is as follows:
1) normal temperature white carbon black industrial wastewater is after pre-treatment adjust ph to 6-9, then clear liquid and the turbid liquid of flocculation sediment is obtained through flocculation, precipitation process, wherein clear liquid enters porous medium filtration, the turbid liquid of flocculation sediment obtains mud cake and filtrate after press filtration, mud cake is transported outward, and filtrate is back to described pre-treatment link adjust ph together with the white carbon black industrial wastewater newly entered;
2) clear liquid after porous medium filters, again successively through ultrafiltration and nanofiltration, the mass concentration of sodium sulfate in waste water is increased to 15%-20%, dense water after nanofiltration enters in heat exchanger I, the fresh water obtained after nanofiltration is desalinated further through reverse osmosis, the fresh water reuse that reverse osmosis appears, the dense water that reverse osmosis appears turns back to circular treatment in ultrafiltration;
3) the dense water after nanofiltration enters heat exchanger I precooling, and the dense water temp after precooling can not lower than its temperature of saturation, to prevent at heat exchanger I intercrystalline;
4) the dense water after precooling enters crystallizer, crystallizer is communicated with resorber gas-phase space, temperature is had lower than 30 DEG C in resorber, concentration higher than 53% lithium-bromide solution, non-condensable gas in all gas-phase spaces that removal present method relates to, makes the chemical potential of lithium-bromide solution in resorber lower than the chemical potential of water dense in crystallizer, under this promotes, realize the evaporation of dense water surface moisture, bottom decrease temperature crystalline obtains magma, the flow of water vapor of evaporation is absorbed to lithium-bromide solution surface by lithium-bromide solution; The sensible heat that latent heat needed for dense water evaporation is discharged by self provides;
5) magma of crystallizer bottom is drawn also centrifugation and go out saltcake and mother liquor, saltcake utilizes as Product recycling; Mother liquor enters the 3rd) in the heat exchanger I of step with nanofiltration after dense water carry out heat exchange, mother liquor temperature is raised, and the dense water after nanofiltration is down to and is needed temperature; Mother liquor after heat exchange reenters nanofiltration and concentrates together with the waste water after ultrafiltration;
6) the lithium-bromide solution dilution after absorbing waste water water vapour in resorber forms bromize lithium dilute solution, bromize lithium dilute solution is delivered in vaporizer, forming bromize lithium concentrated solution after concentrated by heating evaporation returns in resorber, to maintain the process of continuous absorption, the water of condensation obtained after the water vapor condensation that in vaporizer, evaporation produces directly is recycled; The water vapour that bromize lithium dilute solution evaporation produces and lithium-bromide solution absorb waste water water vapour and maintain and balance.
Further, between resorber and vaporizer, be provided with heat exchanger II, bromizate lithium dilute solution and bromize lithium concentrated solution heat exchange by heat exchanger II, by heat exchange, preheating before bromize lithium dilute solution is concentrated, is cooled before bromize lithium concentrated solution returns.
The thermal source of vaporizer heating is temperature higher than the industrial waste heat of 80 DEG C.
Compared to existing technology, the present invention has the following advantages:
1) the present invention proposes a kind of method of white carbon black industrial wastewater zero release and recycling, by nanofiltration by further for the waste water of contains sodium sulfate lower concentration concentrate, realize fresh water reuse by reverse osmosis.
2) the present invention utilizes the strong water absorbability of lithium-bromide solution to realize sodium sulfate wastewater transpiration cooling crystallization, and without the need to low-temperature receiver, energy efficient, avoids the attached wall of crystallization in septate heat transfer simultaneously.
3) magma in crystallizer is passed through centrifugation by the present invention, realize saltcake Product recycling, lower concentration crystalline mother solution returns to nanofiltration system after reclaiming cold by interchanger and concentrates, and makes whole process closed circulation, realizes the object of white carbon black industrial wastewater zero release and recycling.
Accompanying drawing explanation
Fig. 1-white carbon black industrial wastewater processing flow chart of the present invention.
Embodiment
The present invention realizes the thinking of white carbon black industrial wastewater zero release and recycling: first the process of white carbon black industrial wastewater concentrate is obtained to the concentration needed, then carry out crystallisation by cooling, crystallisate is recycled.During concrete crystallisation by cooling, the strong water absorbability of lithium-bromide solution is utilized to realize contains sodium sulfate high-salt wastewater low-temperature evaporation condensing crystal, sodium sulfate wastewater moisture evaporation in crystallizer, the moisture of evaporation is absorbed by lithium-bromide solution in resorber and forms bromize lithium dilute solution, and the impellent needed for evaporative process is the chemical potential of chemical potential lower than water dense in crystallizer of lithium-bromide solution in resorber.The water vapour that bromize lithium dilute solution is obtained by vaporizer carries out condensed recycling condensing water, and strong solution returns resorber again.The present invention enters sodium sulfate concentration in the waste water of crystallizer and is not less than 150g/L, and temperature is not less than 15 DEG C; Lithium-bromide solution massfraction is higher than 53%, and temperature is no more than 30 DEG C, and under aforementioned impellent, can realize sodium sulfate wastewater evaporating, concentrating and crystallizing, magma goes out saltcake and mother liquor by centrifugation.Saltcake is as Product recycling, and mother liquor reclaims cold through interchanger, and juice circulation.
Below in conjunction with Fig. 1, the present invention is described in further details.
1) normal temperature white carbon black industrial wastewater (25-30 DEG C) is after pre-treatment adjust ph to 6-9, then clear liquid and the turbid liquid of flocculation sediment is obtained through flocculation, precipitation process, wherein clear liquid enters porous medium filtration, the turbid liquid of flocculation sediment obtains mud cake and filtrate after press filtration, mud cake is transported outward, and filtrate is back to described pre-treatment link adjust ph together with the white carbon black industrial wastewater newly entered.
2) clear liquid after porous medium filters, again successively through ultrafiltration and nanofiltration, the mass concentration of sodium sulfate in waste water is increased to 15%-20%, dense water after nanofiltration enters in heat exchanger I, the fresh water obtained after nanofiltration is desalinated further through reverse osmosis, the fresh water reuse that reverse osmosis appears, the dense water that reverse osmosis appears turns back to circular treatment in ultrafiltration.
3) the dense water after nanofiltration enters heat exchanger I precooling, and the dense water temp after precooling can not lower than its temperature of saturation, to prevent at heat exchanger I intercrystalline.The variation relation of sodium sulfate solubility with temperature is in table 1, and because in present method, the mass concentration of sodium sulfate is not less than 15%, the temperature of saturation of its correspondence is approximately 15 DEG C, so dense water temp during actual treatment after precooling is not less than 15 DEG C.
The variation relation of table 1 sodium sulfate solubility with temperature
| Temperature/DEG C | 0 | 10 | 20 | 30 | 40 |
| Solubleness g/L | 49 | 91 | 195 | 408 | 488 |
4) the dense water after precooling enters crystallizer, crystallizer is communicated with resorber gas-phase space, temperature is had lower than 30 DEG C in resorber, concentration higher than 53% lithium-bromide solution, remove the non-condensable gas in all gas-phase spaces of relating to of present method in advance, reality removes non-condensable gas by vacuum pump evacuation mode, to start present method; Because of the strong water absorbability of lithium-bromide solution, make the chemical potential of lithium-bromide solution in resorber lower than the chemical potential of water dense in crystallizer, under this promotes, realize the evaporation of dense water surface moisture, bottom decrease temperature crystalline obtains magma, the flow of water vapor of evaporation is absorbed to lithium-bromide solution surface by lithium-bromide solution; The sensible heat that latent heat needed for dense water evaporation is discharged by self provides.Because of the stopping property problem that crystallization cooling system may exist, when the non-condensable gas be mixed with affects crystallisation by cooling system cloud gray model, discharge non-condensable gas by going vacuum system.
5) magma of crystallizer bottom is drawn also centrifugation and go out saltcake and mother liquor, saltcake utilizes as Product recycling; Lower concentration mother liquor enters the 3rd) in the heat exchanger I of step with nanofiltration after dense water carry out after heat exchange reclaims cold, mother liquor temperature is raised, and the dense water after nanofiltration is down to and is needed temperature; Before mother liquor after heat exchange is back to nano-filtration unit, reenters nano-filtration unit and concentrate together with the waste water after ultrafiltration.
6) the lithium-bromide solution dilution after absorbing waste water water vapour in resorber forms bromize lithium dilute solution, bromize lithium dilute solution is delivered in vaporizer, forming bromize lithium concentrated solution after concentrated by heating evaporation returns in resorber, to maintain the process of continuous absorption, actual when implementing, the thermal source of vaporizer heating is temperature higher than the industrial waste heat (as industrial water of condensation) of 80 DEG C.The water of condensation obtained after the water vapor condensation that in vaporizer, evaporation produces directly is recycled; The water vapour that bromize lithium dilute solution evaporation produces and lithium-bromide solution absorb waste water water vapour and maintain and balance.
For maintenance heat balance, be provided with heat exchanger II, bromizate lithium dilute solution and bromize lithium concentrated solution heat exchange by heat exchanger II between resorber and vaporizer, by heat exchange, preheating before bromize lithium dilute solution is concentrated, is cooled before bromize lithium concentrated solution returns.
As can be seen from Figure 1, the present invention includes waste water concentrate and the large process of crystallisation by cooling two; Wherein waste water concentrate comprises pretreatment unit (for pH value is adjusted to 6.0-9.0), press filtration unit, porous medium filtering unit, ultra filtration unit, nano-filtration unit and reverse osmosis units, crystallisation by cooling is carried out in nano-filtration unit water outlet, and the concentration going out the dense aqueous sodium persulfate of nano-filtration unit is concentrated into 15%-20%.Crystallisation by cooling mainly comprises dense water pre-cooling unit (heat exchanger I), crystalline element (crystallizer and centrifugation) and lithium-bromide solution absorptive unit (resorber, heat exchanger II, vaporizer and condenser).Wherein enter the dense water of crystallisation by cooling system after pre-cooled, temperature is not less than 15 DEG C.The present invention utilizes the strong water absorbability of lithium-bromide solution, realizes the sodium chloride crystal in dense water in crystallizer.
Embodiment: white carbon black industrial wastewater process pilot scale project, waste water quality: pH:5.0-6.0, Na
2sO
4: 26000mg/L, SS:2000mg/L.Process flow is 15m
3/ d, the sodium sulfate concentration of the dense water after nanofiltration is 180g/L, produces reuse fresh water conductance lower than 150mS/cm through reverse osmosis.In crystallisation by cooling system, the lithium-bromide solution temperature in resorber is lower than 30 DEG C, and massfraction, higher than under the condition of 53%, obtains crystalline product saltcake.
The above embodiment of the present invention is only for example of the present invention is described, and is not the restriction to embodiments of the present invention.For those of ordinary skill in the field, other multi-form change and variations can also be made on the basis of the above description.Here cannot give exhaustive to all embodiments.Every belong to technical scheme of the present invention the apparent change of amplifying out or variation be still in the row of protection scope of the present invention.
Claims (3)
1. a method for white carbon black industrial wastewater zero release and recycling, is characterized in that: step is as follows:
1) normal temperature white carbon black industrial wastewater is after pre-treatment adjust ph to 6-9, then clear liquid and the turbid liquid of flocculation sediment is obtained through flocculation, precipitation process, wherein clear liquid enters porous medium filtration, the turbid liquid of flocculation sediment obtains mud cake and filtrate after press filtration, mud cake is transported outward, and filtrate is back to described pre-treatment link adjust ph together with the white carbon black industrial wastewater newly entered;
2) clear liquid after porous medium filters, again successively through ultrafiltration and nanofiltration, the mass concentration of sodium sulfate in waste water is increased to 15%-20%, dense water after nanofiltration enters in heat exchanger I, the fresh water obtained after nanofiltration is desalinated further through reverse osmosis, the fresh water reuse that reverse osmosis appears, the dense water that reverse osmosis appears turns back to circular treatment in ultrafiltration;
3) the dense water after nanofiltration enters heat exchanger I precooling, and the dense water temp after precooling can not lower than its temperature of saturation, to prevent at heat exchanger I intercrystalline;
4) the dense water after precooling enters crystallizer, crystallizer is communicated with resorber gas-phase space, temperature is had lower than 30 DEG C in resorber, concentration higher than 53% lithium-bromide solution, non-condensable gas in all gas-phase spaces that removal present method relates to, makes the chemical potential of lithium-bromide solution in resorber lower than the chemical potential of water dense in crystallizer, under this promotes, realize the evaporation of dense water surface moisture, bottom decrease temperature crystalline obtains magma, the flow of water vapor of evaporation is absorbed to lithium-bromide solution surface by lithium-bromide solution; The sensible heat that latent heat needed for dense water evaporation is discharged by self provides;
5) magma of crystallizer bottom is drawn also centrifugation and go out saltcake and mother liquor, saltcake utilizes as Product recycling; Mother liquor enters the 3rd) in the heat exchanger I of step with nanofiltration after dense water carry out heat exchange, mother liquor temperature is raised, and the dense water after nanofiltration is down to and is needed temperature; Mother liquor after heat exchange reenters nanofiltration and concentrates together with the waste water after ultrafiltration;
6) the lithium-bromide solution dilution after absorbing waste water water vapour in resorber forms bromize lithium dilute solution, bromize lithium dilute solution is delivered in vaporizer, forming bromize lithium concentrated solution after concentrated by heating evaporation returns in resorber, to maintain the process of continuous absorption, the water of condensation obtained after the water vapor condensation that in vaporizer, evaporation produces directly is recycled; The water vapour that bromize lithium dilute solution evaporation produces and lithium-bromide solution absorb waste water water vapour and maintain and balance.
2. the method for white carbon black industrial wastewater zero release according to claim 1 and recycling, it is characterized in that: between resorber and vaporizer, be provided with heat exchanger II, lithium dilute solution and bromize lithium concentrated solution heat exchange is bromizated by heat exchanger II, pass through heat exchange, preheating before bromize lithium dilute solution is concentrated, is cooled before bromize lithium concentrated solution returns.
3. the method for white carbon black industrial wastewater zero release according to claim 1 and recycling, is characterized in that: the thermal source of vaporizer heating is temperature higher than the industrial waste heat of 80 DEG C.
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN106854004A (en) * | 2016-12-05 | 2017-06-16 | 益凯新材料有限公司 | A kind of apparatus and method of the evaporative crystallization of white carbon black industrial wastewater |
| CN108394947A (en) * | 2018-01-16 | 2018-08-14 | 安徽至臻环保科技有限公司 | A kind of white carbon washings Zero discharge treatment method |
| CN110745832A (en) * | 2019-11-29 | 2020-02-04 | 河南骏化发展股份有限公司 | Water-saving device and process for producing white carbon black by precipitation method |
| CN112723567A (en) * | 2020-12-28 | 2021-04-30 | 中昊黑元化工研究设计院有限公司 | Rapid clarification device and method for white carbon black production wastewater by precipitation method |
| CN113044859A (en) * | 2021-02-23 | 2021-06-29 | 四川思达能环保科技有限公司 | Method for recovering sodium sulfate from white carbon black feed liquid |
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| CN106854004A (en) * | 2016-12-05 | 2017-06-16 | 益凯新材料有限公司 | A kind of apparatus and method of the evaporative crystallization of white carbon black industrial wastewater |
| CN106854004B (en) * | 2016-12-05 | 2022-11-11 | 益凯新材料有限公司 | Device and method for evaporative crystallization of white carbon black production wastewater |
| CN108394947A (en) * | 2018-01-16 | 2018-08-14 | 安徽至臻环保科技有限公司 | A kind of white carbon washings Zero discharge treatment method |
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| CN113044859A (en) * | 2021-02-23 | 2021-06-29 | 四川思达能环保科技有限公司 | Method for recovering sodium sulfate from white carbon black feed liquid |
| CN113044859B (en) * | 2021-02-23 | 2022-10-14 | 四川思达能环保科技有限公司 | Method for recovering sodium sulfate from white carbon black feed liquid |
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| CN104724873B (en) | 2017-03-08 |
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