CN105236651A - Technology for evaporating and crystallizing high concentration salt-containing wastewater in pulping and papermaking industries - Google Patents
Technology for evaporating and crystallizing high concentration salt-containing wastewater in pulping and papermaking industries Download PDFInfo
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- CN105236651A CN105236651A CN201510637003.0A CN201510637003A CN105236651A CN 105236651 A CN105236651 A CN 105236651A CN 201510637003 A CN201510637003 A CN 201510637003A CN 105236651 A CN105236651 A CN 105236651A
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Abstract
The invention discloses a technology for evaporating and crystallizing high concentration salt-containing wastewater in the pulping and papermaking industries. The technology comprises the following steps: preheating high concentration salt-containing wastewater by a preheating system; introducing the preheated wastewater into an evaporator, introducing the secondary steam into a steam compressor, compressing the steam by the steam compressor, returning the compressed steam to the heating chamber of the evaporator to heat the compressed steam; transferring the evaporated condensed liquid to a crystallizer; discharging the precipitated crystallized salts in the crystallizer to a salt slurry barrel through a salt pipe, pumping the salt slurry to a thickening device, transferring the thickened slurry to a centrifuge to carry out dehydration; returning the supernate mother liquor and centrifugal mother liquor to the raw material barrel, and drying the wet solids from the centrifuge in a drying bed so as to obtain the finished product of crystallized salt. The pollution caused by high concentration brine is solved, recyclable condensed water and crystallized salts are obtained, and the zero discharge of high concentration slat containing wastewater is achieved.
Description
Technical field
The invention belongs to evaporative crystallization technique, relate to the treatment process of pulping and paper-making high-concentration salt-containing wastewater.
Background technology
In the whole production process of pulping and paper-making, all need a large amount of water to carry out to carry from the processing etc. of the recovery of papermaking of getting the raw materials ready, chemical, paper, wash, dispersed material and cooling apparatus etc.Although also there is the part reuse of water in process of production, still a large amount of brine wastes can be produced.After prior art adopts pre-treatment, membrane treatment appts, still there is the high dense brine waste of part.Generally following three kinds of modes are mainly contained to the process of this effluent part:
A () arranges method outward.Directly outer row not only causes the pollution of local environment, also brings the significant wastage of resource simultaneously.
(b) evaporation pond method.This method is not only very large by region, the impact in season, and brings the trouble of post-processed.
(c) multiple-effect evaporation method.Technical process is multiple-effect evaporation tank successively after preheating, evaporating pot slurry out by centrifuge dehydration, the solid obtained outward transport or landfill.This technique floor space is comparatively large, Controlling System relative complex, the solid salt that obtains can not recyclings, can only as fixed-end forces, and secondary pollution is serious.
Summary of the invention
The object of the present invention is to provide a kind of pulping and paper-making high-concentration salt-containing wastewater evaporative crystallization technique, adopting this technique to obtain can the water of condensation of reuse and the crystal salt product sold outward.Have that floor space is little, technique be simple, feature that energy consumption is lower, the object of wastewater zero discharge can be realized.
The technical scheme of invention:
Pulp and paper making wastewater zero discharge system high-concentration salt-containing wastewater evaporative crystallization technique, comprises the following steps:
(a) concentration be 8% ~ 12% brine waste be 90 ~ 110 DEG C by the temperature after preheater preheats, thermal source is vapo(u)rization system water of condensation out.
B the waste water after () preheating enters evaporating pot, controlling temperature in evaporating pot is 100 ~ 110 DEG C, and the inlet steam temperature of vapour compressor is 100 ~ 105 DEG C, and outlet steam temperature is 105 ~ 110 DEG C, and feed liquid is concentrated in evaporating pot, obtains the concentrated solution of 20% ~ 24%.
C () concentrated solution enters crystallizer, in crystallization control tank, temperature is 105 ~ 115 DEG C, and the inlet steam temperature of vapour compressor is 100 ~ 105 DEG C, and outlet steam temperature is 110 ~ 116 DEG C, and feed liquid concentrates crystallization salt further in crystallizer; Controlled circulation materials in the tube solid and liquid ratio is 15% ~ 25%.
D () salt leg salt slurry is out by pump to thickener, the solid-to-liquid ratio controlling thickener is 40% ~ 60%.
E () thickener salt slurry out enters whizzer, whizzer wet feed water ratio 3% ~ 5% out.
F the wet feed after () dehydration enters drying bed, obtain crystal salt product after drying.
The temperature controlled in described (a) step after preheater preheats is preferably 100 ~ 105 DEG C.
Control temperature in evaporating pot in described (b) step and be preferably 102 ~ 107 DEG C.
In described (c) step, in crystallization control tank, temperature is preferably 108 ~ 113 DEG C.
The present invention has following beneficial effect: the combination adopting mechanical thermal compress technique and first evaporation concentration recrystallize technique, by vapour compressor, the secondary steam of evaporation is pushed back again the heating chamber of evaporating pot, so recycle, make that whole system floor space is little, running cost is low, achieve zero emission requirement.Meanwhile, the water of condensation of evaporation process meets reuse requirement, may be used for dyeing by the crystal salt after drying bed process.
Accompanying drawing explanation
Accompanying drawing is process flow diagram.
Embodiment
Embodiment 1
30 DEG C, concentration be 10% brine waste be 102 DEG C by the temperature after preheater preheats, thermal source is vapo(u)rization system water of condensation out; Waste water after preheating enters evaporating pot, and controlling temperature in evaporating pot is 104.5 DEG C, and the inlet steam temperature of vapour compressor is 100 DEG C, and outlet steam temperature is 108 DEG C, and feed liquid is concentrated in evaporating pot, obtains the concentrated solution of 22%; Concentrated solution enters crystallizer, and in crystallization control tank, temperature is 111 DEG C, and the inlet steam temperature of vapour compressor is 100 DEG C, and outlet steam temperature is 115 DEG C, and feed liquid concentrates crystallization salt further in crystallizer; Controlled circulation materials in the tube solid and liquid ratio is 20%; Salt slurry is expelled to salt slurry bucket by salt leg, and pump is to thickener, and the solid-to-liquid ratio controlling thickener is 50%; Thickener salt slurry out enters whizzer, whizzer wet feed water ratio 5% out; Wet feed after dehydration enters drying bed, obtains crystal salt product after drying.
Embodiment 2
25 DEG C, concentration be 12% brine waste be 103 DEG C by the temperature after preheater preheats, thermal source is vapo(u)rization system water of condensation out; Waste water after preheating enters evaporating pot, and controlling temperature in evaporating pot is 105 DEG C, and the inlet steam temperature of vapour compressor is 100.5 DEG C, and outlet steam temperature is 108.5 DEG C, and feed liquid is concentrated in evaporating pot, obtains the concentrated solution of 24%; Concentrated solution enters crystallizer, and in crystallization control tank, temperature is 111 DEG C, and the inlet steam temperature of vapour compressor is 100.5 DEG C, and outlet steam temperature is 115.5 DEG C, and feed liquid concentrates crystallization salt further in crystallizer; Controlled circulation materials in the tube solid and liquid ratio is 15%; Salt slurry is expelled to salt slurry bucket by salt leg, and pump is to thickener, and the solid-to-liquid ratio controlling thickener is 50%; Thickener salt slurry out enters whizzer, whizzer wet feed water ratio 4% out; Wet feed after dehydration enters drying bed, obtains crystal salt product after drying.
Embodiment 3
25 DEG C, concentration be 8% brine waste be 90 DEG C by the temperature after preheater preheats, thermal source is vapo(u)rization system water of condensation out; Waste water after preheating enters evaporating pot, and controlling temperature in evaporating pot is 91 DEG C, and the inlet steam temperature of vapour compressor is 86 DEG C, and outlet steam temperature is 94 DEG C, and feed liquid is concentrated in evaporating pot, obtains the concentrated solution of 20%; Concentrated solution enters crystallizer, and in crystallization control tank, temperature is 96 DEG C, and the inlet steam temperature of vapour compressor is 86 DEG C, and outlet steam temperature is 102 DEG C, and feed liquid concentrates crystallization salt further in crystallizer; Controlled circulation materials in the tube solid and liquid ratio is 25%; Salt slurry is expelled to salt slurry bucket by salt leg, and pump is to thickener, and the solid-to-liquid ratio controlling thickener is 50%; Thickener salt slurry out enters whizzer, whizzer wet feed water ratio 5% out; Wet feed after dehydration enters drying bed, obtains crystal salt product after drying.
Claims (4)
1. pulping and paper-making high-concentration salt-containing wastewater evaporative crystallization technique, is characterized in that comprising the following steps:
(a) concentration be 8% ~ 12% brine waste be 90 ~ 110 DEG C by the temperature after preheater preheats, thermal source is vapo(u)rization system water of condensation out;
B the waste water after () preheating enters evaporating pot, controlling temperature in evaporating pot is 100 ~ 110 DEG C, and the inlet steam temperature of vapour compressor is 100 ~ 105 DEG C, and outlet steam temperature is 105 ~ 110 DEG C, and feed liquid is concentrated in evaporating pot, obtains the concentrated solution of 20% ~ 24%;
C () concentrated solution enters crystallizer, in crystallization control tank, temperature is 105 ~ 115 DEG C, and the inlet steam temperature of vapour compressor is 100 ~ 105 DEG C, and outlet steam temperature is 110 ~ 116 DEG C, and feed liquid concentrates crystallization salt further in crystallizer; Controlled circulation materials in the tube solid and liquid ratio is 15% ~ 25%;
D () salt leg salt slurry is out by pump to thickener, the solid-to-liquid ratio controlling thickener is 40% ~ 60%;
E () thickener salt slurry out enters whizzer, whizzer wet feed water ratio 3% ~ 5% out;
F the wet feed after () dehydration enters drying bed, obtain crystal salt product after drying.
2. pulping and paper-making high-concentration salt-containing wastewater evaporative crystallization technique according to claim 1, is characterized in that: controlling the temperature after preheater preheats in (a) step is 100 ~ 105 DEG C.
3. pulping and paper-making high-concentration salt-containing wastewater evaporative crystallization technique according to claim 1, is characterized in that: controlling temperature in evaporating pot in (b) step is 102 ~ 107 DEG C.
4. pulping and paper-making high-concentration salt-containing wastewater evaporative crystallization technique according to claim 1, is characterized in that: in (c) step, in crystallization control tank, temperature is 108 ~ 113 DEG C.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
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| CN201510637003.0A CN105236651A (en) | 2015-10-03 | 2015-10-03 | Technology for evaporating and crystallizing high concentration salt-containing wastewater in pulping and papermaking industries |
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| CN201510637003.0A CN105236651A (en) | 2015-10-03 | 2015-10-03 | Technology for evaporating and crystallizing high concentration salt-containing wastewater in pulping and papermaking industries |
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Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106379920A (en) * | 2016-11-17 | 2017-02-08 | 河北言明化工设备有限公司 | Device and method of preparing pure lithium chloride solution by precipitating sodium through evaporation of mixed aqueous solution of lithium chloride and sodium chloride |
| CN106698493A (en) * | 2017-01-05 | 2017-05-24 | 四川理工学院 | Evaporative crystallization technology of barium chloride |
| CN107265737A (en) * | 2017-08-14 | 2017-10-20 | 东莞东元环境科技股份有限公司 | A kind of industrial high-salt wastewater evaporative crystallization Zero discharging system and method |
| CN108249668A (en) * | 2016-12-28 | 2018-07-06 | 麦王环境技术股份有限公司 | Slurrying yellow liquor concentrate and dry Processes and apparatus |
| CN110563236A (en) * | 2019-09-10 | 2019-12-13 | 南通能达水务有限公司 | High-concentration brine inorganic salt recovery system and recovery method |
| CN110606613A (en) * | 2019-10-09 | 2019-12-24 | 北京国电富通科技发展有限责任公司 | Wave energy crystallization method and device for high-salinity wastewater |
| CN112408528A (en) * | 2020-10-29 | 2021-02-26 | 武汉凯迪水务有限公司 | Anti-fouling blocking and self-cleaning MVR evaporation concentration system |
| CN112939364A (en) * | 2021-02-07 | 2021-06-11 | 浙江晶立捷环境科技有限公司 | Landfill leachate concentrated solution treatment system and treatment process |
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| EP0473329A1 (en) * | 1990-08-13 | 1992-03-04 | Kamyr, Inc. | Dimple plate horizontal evaporator effects |
| CN202625969U (en) * | 2012-04-17 | 2012-12-26 | 常州光辉生物科技有限公司 | High-salinity organic wastewater treatment device |
| CN103819041A (en) * | 2014-03-18 | 2014-05-28 | 江苏星瑞化工工程科技有限公司 | Method for concentrating high-salinity wastewater at low temperature |
| CN103936220A (en) * | 2014-05-06 | 2014-07-23 | 田晓良 | Zero discharge treatment process of saline sewage produced by refining |
| CN204310909U (en) * | 2014-12-04 | 2015-05-06 | 石家庄鼎威化工设备工程有限公司 | Coal Chemical Industry produces brine waste evaporated crystallization device in ethylene glycol |
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2015
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Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
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| EP0473329A1 (en) * | 1990-08-13 | 1992-03-04 | Kamyr, Inc. | Dimple plate horizontal evaporator effects |
| CN202625969U (en) * | 2012-04-17 | 2012-12-26 | 常州光辉生物科技有限公司 | High-salinity organic wastewater treatment device |
| CN103819041A (en) * | 2014-03-18 | 2014-05-28 | 江苏星瑞化工工程科技有限公司 | Method for concentrating high-salinity wastewater at low temperature |
| CN103936220A (en) * | 2014-05-06 | 2014-07-23 | 田晓良 | Zero discharge treatment process of saline sewage produced by refining |
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Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106379920A (en) * | 2016-11-17 | 2017-02-08 | 河北言明化工设备有限公司 | Device and method of preparing pure lithium chloride solution by precipitating sodium through evaporation of mixed aqueous solution of lithium chloride and sodium chloride |
| CN106379920B (en) * | 2016-11-17 | 2018-02-06 | 河北言明化工设备有限公司 | Lithium chloride sodium chloride mixed aqueous solution evaporation analysis sodium produces the device and method of pure lithium chloride solution |
| CN108249668A (en) * | 2016-12-28 | 2018-07-06 | 麦王环境技术股份有限公司 | Slurrying yellow liquor concentrate and dry Processes and apparatus |
| CN106698493A (en) * | 2017-01-05 | 2017-05-24 | 四川理工学院 | Evaporative crystallization technology of barium chloride |
| CN107265737A (en) * | 2017-08-14 | 2017-10-20 | 东莞东元环境科技股份有限公司 | A kind of industrial high-salt wastewater evaporative crystallization Zero discharging system and method |
| CN110563236A (en) * | 2019-09-10 | 2019-12-13 | 南通能达水务有限公司 | High-concentration brine inorganic salt recovery system and recovery method |
| CN110606613A (en) * | 2019-10-09 | 2019-12-24 | 北京国电富通科技发展有限责任公司 | Wave energy crystallization method and device for high-salinity wastewater |
| CN112408528A (en) * | 2020-10-29 | 2021-02-26 | 武汉凯迪水务有限公司 | Anti-fouling blocking and self-cleaning MVR evaporation concentration system |
| CN112939364A (en) * | 2021-02-07 | 2021-06-11 | 浙江晶立捷环境科技有限公司 | Landfill leachate concentrated solution treatment system and treatment process |
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Application publication date: 20160113 |