CN105016553A - High-salinity wastewater treatment method - Google Patents

High-salinity wastewater treatment method Download PDF

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Publication number
CN105016553A
CN105016553A CN201510321161.5A CN201510321161A CN105016553A CN 105016553 A CN105016553 A CN 105016553A CN 201510321161 A CN201510321161 A CN 201510321161A CN 105016553 A CN105016553 A CN 105016553A
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China
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effect
evaporation
pump
evaporating
salt wastewater
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CN201510321161.5A
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Chinese (zh)
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朱卫
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朱卫
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Priority to CN201510321161.5A priority Critical patent/CN105016553A/en
Publication of CN105016553A publication Critical patent/CN105016553A/en

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Abstract

The present invention discloses a high-salinity wastewater treatment method. The method comprises steps of feeding, evaporating and solid-gas separating. Innovating points of the high-salinity wastewater treatment method are: in the evaporating step, triple effect circulation evaporation is performed by using a triple effect circulation evaporation process, and the triple effect circulation evaporation process comprises in sequence a first effect circulation evaporation step, a second effect circulation evaporation step, and a third effect circulation evaporation step; and the first effect, the second effect and the third effect circulation evaporation steps each comprise a preheating step of a preheater and an evaporation step of a flash evaporator. The high-salinity wastewater treatment method of the invention is highly automated and good in wastewater purification effect, causes no pollution by discharging wastewater, is small in energy consumption and investment, and is unlikely to cause equipment to be corroded. For the high-salinity wastewater treated by the method of the present invention, the recovery rate of obtained salt crystal is greater than 99.5%, and the contained chemical oxygen demand decreases to less than 68 mg/L, which meets the national discharge standards.

Description

The treatment process of high-salt wastewater

Technical field

The present invention relates to the treatment process of high-salt wastewater, particularly relate to a kind for the treatment of process of high salt agricultural chemicals waste water, belong to industrial waste water purifying field.

Background technology

The organism of high-salt-content organic wastewater is different according to production process, and contained organic kind and chemical property differ greatly, but contained salts substances mostly is Cl -, SO4 2-, Na +, Ca 2+deng salts substances.

The waste water of total saliferous massfraction at least 1% of high-salt wastewater. it is mainly from the collection processing etc. of chemical plant and oil and natural gas. and this waste water contains many kinds of substance (comprising salt, oil, organic heavy metal and radioactive substance).The way of production of brine waste is extensive, and the water yield also increases year by year.The impact that organic pollutant in removal saline sewage causes environment is most important.Adopt biological process to process, the salts substances of high density is inhibited to microorganism, adopts physico-chemical process process, and general investment is large, and working cost is high, and is difficult to the decontamination effect improving reaching expection.As the technical finesse for high density height saliferous trade effluent, what research was both at home and abroad more at present mainly contains wet-air oxidation law technology (WAO), Wet Catalytic Oxidation Method technology (CWO), evaporation recovery etc.These technology need to carry out under high-temperature and high-pressure conditions, and equipment and working condition require high, and energy consumption is high, and investment is large, and equipment is perishable.

Research finds: multiple-effect evaporation can allow the salt solution after heating evaporate in the vaporizer of multiple series connection, and previous evaporator evaporation steam is out as the thermal source of next vaporizer, and condensation becomes fresh water.Wherein low temperature multiple-effect distillation is one of method the most energy-conservation in distillation method.Low temperature multiple-effect distillation technology is due to energy-conservation factor, and developed recently is rapid, the scale expanding day of device, cost reduces day by day, and Main Trends of The Development makes outlet capacity for improving device unit, adopts cheap material to reduce construction costs, improve service temperature, improve heat transfer efficiency; The simultaneously multistage flash evaporation flashing chamber that hot salt brine can be made to flow through several pressure successively reduce gradually, stepped evaporation is lowered the temperature, simultaneously salt solution also enrichment step by step, have that equipment is simple and reliable, safety in operation is high, anti-scaling property is good, turndown ratio is large and can utilize the advantage such as Lowlevel thermal energy and used heat, be suitable for large-scale and ultra-large type desalting equipment.

Summary of the invention

The object of this invention is to provide the treatment process of high-salt wastewater, the method level of automation is high, purifies liquid waste effective, and waste water is discharged pollution-free, and energy consumption is less, invests little, and equipment is not perishable.

The technical solution used in the present invention is: the treatment process of high-salt wastewater, comprise reinforced, evaporation and solid and gas separating step, it is characterized in that: described evaporation step carries out triple effect cycle evaporation for adopting triple effect cycle evaporation flow process, and described triple effect cycle evaporation flow process comprises an effect circulating and evaporating step, two effect circulating and evaporating step and triple effect cycle evaporation steps successively; Preheater preheating steps and flasher evaporation step is comprised respectively in a described effect, two effects, triple effect cycle evaporation step.

Further, in a described effect circulating and evaporating step, preheater preheating steps is the effect preheater pumped into by pump by high-salt wastewater in an effect evaporation flow process, and preheated by condensation hot water, make full use of heat energy, arranging pre-heating temperature is 76 ~ 78 DEG C; Described flasher evaporation step evaporates for pre-warmed high-salt wastewater is pumped into an effect flasher by pump, and arranging vaporization temperature is 122 ~ 125 DEG C; By an effect forced circulation pump circulating and evaporating; The salt concn of the high-salt wastewater after one effect evaporation reaches 26 ~ 28%, carries out two effect circulating and evaporating steps.

Further, in described two effect circulating and evaporating steps preheater preheating steps be by concentration be 26 ~ 28% high-salt wastewater pump into two effect flashers by pump and evaporate, arranging vaporization temperature is 100 ~ 105 DEG C; By two effect recycle pump circulating and evaporating, partial material sends into triple-effect evaporation plant simultaneously, and partial material sends into two effect enrichment tanks, pumps into slurry flash tank by pump.

Further, two effect flash tanks material is out sent into three grades of flashers and evaporates, arranging vaporization temperature is 70 ~ 76 DEG C; By triple effect cycle pump circulating and evaporating, triple effect enrichment tank sent into by material, and component loops evaporates, and part pumps into slurry flash tank by pump.

Further, described separating step for gas phase fraction is pumped into separating tank by pump, then enters container for storing liquid after condenser condenses, finally gets rid of; Gu material pumps into whizzer by discharging pump and carries out centrifugation, supernatant liquid is mother liquor, and it is salt crystal that solid is separated out by lower floor; Described mother liquor is returned triple effect cycle evaporation flow process and carry out the evaporation of secondary triple effect cycle, the secondary mother liquid be again separated carries out burning disposal, and it is salt crystal that solid is separated out by lower floor.

Further, the initial saltiness of described high-salt wastewater is 14 ~ 25%.

Beneficial effect: the treatment process of this high-salt wastewater of the present invention, level of automation is high, purifies liquid waste effective, and waste water is discharged pollution-free, and energy consumption is less, invests little, and equipment is not perishable; Through the high-salt wastewater of method process of the present invention, the rate of recovery obtaining salt crystal can reach more than 99.5%, and the chemical oxygen demand (COD) contained drops to below 68mg/L, reaches discharging standards.

Embodiment

Implementation column below can make those skilled in the art more fully understand the present invention, but does not therefore limit the present invention among described scope of embodiments.

Embodiment 1

By saltiness be 14% agricultural chemicals waste water by feedstock pump pump into one effect evaporation flow process in preheater, preheated by saturated steam, arranging pre-heating temperature is 76 DEG C, pre-warmed high-salt wastewater is pumped into primary flash device by pump evaporate, arranging vaporization temperature is 122 DEG C,, the salt concn of the high-salt wastewater after an effect evaporation is 26%;

By concentration be 26% high-salt wastewater by pump pump into two effects evaporation flow processs in secondary preheater, preheated by secondary saturated steam, arranging pre-heating temperature is 100 DEG C; Described flasher evaporation step evaporates for pre-warmed high-salt wastewater is pumped into two-stage flash device by pump, and arranging vaporization temperature is 115 DEG C, and the salt concn of the high-salt wastewater after two effect evaporations is 88%;

By concentration be 88% high-salt wastewater pumped into three grades of preheaters in triple effect evaporation flow process by pump, preheated by three saturated steams, arranging pre-heating temperature is 70 DEG C, by triple effect cycle pump circulating and evaporating, triple effect enrichment tank sent into by material, 16% circulating and evaporating, 84% pumps into slurry flash tank by pump.

Gas phase fraction is pumped into separating tank by pump, then enter container for storing liquid after condenser condenses, finally get rid of; Gu material pumps into whizzer by discharging pump and carries out centrifugation, supernatant liquid is mother liquor, and it is salt crystal that solid is separated out by lower floor.

Through the high-salt wastewater of the present embodiment method process, the rate of recovery obtaining salt crystal can reach 99.5%, and the chemical oxygen demand (COD) contained drops to 65mg/L, reaches discharging standards.

Embodiment 2

By saltiness be 25% agricultural chemicals waste water by feedstock pump pump into one effect evaporation flow process in preheater, preheated by saturated steam, arranging pre-heating temperature is 78 DEG C, pre-warmed high-salt wastewater is pumped into primary flash device by pump evaporate, arranging vaporization temperature is 125 DEG C, and the salt concn of the high-salt wastewater after an effect evaporation is 28%;

By concentration be 28% high-salt wastewater by pump pump into two effects evaporation flow processs in secondary preheater, preheated by secondary saturated steam, arranging pre-heating temperature is 105 DEG C; Described flasher evaporation step evaporates for pre-warmed high-salt wastewater is pumped into two-stage flash device by pump, and arranging vaporization temperature is 115 DEG C, and the salt concn of the high-salt wastewater after two effect evaporations is 90%;

By concentration be 90% high-salt wastewater pumped into three grades of preheaters in triple effect evaporation flow process by pump, preheated by three saturated steams, arranging pre-heating temperature is 76 DEG C, by triple effect cycle pump circulating and evaporating, triple effect enrichment tank sent into by material, 12% circulating and evaporating, 88% pumps into slurry flash tank by pump.

Gas phase fraction is pumped into separating tank by pump, then enter container for storing liquid after condenser condenses, finally get rid of; Gu material pumps into whizzer by discharging pump and carries out centrifugation, supernatant liquid is mother liquor, and it is salt crystal that solid is separated out by lower floor; Described mother liquor is returned triple effect cycle evaporation flow process and carry out the evaporation of secondary triple effect cycle, the secondary mother liquid be again separated carries out burning disposal, and it is salt crystal that solid is separated out by lower floor.

Through the high-salt wastewater of the present embodiment method process, the rate of recovery obtaining salt crystal can reach 99.8%, and the chemical oxygen demand (COD) contained drops to 68mg/L, reaches discharging standards.

Claims (6)

1. the treatment process of high-salt wastewater, comprise reinforced, evaporation and solid and gas separating step, it is characterized in that: described evaporation step carries out triple effect cycle evaporation for adopting triple effect cycle evaporation flow process, and described triple effect cycle evaporation flow process comprises an effect circulating and evaporating step, two effect circulating and evaporating step and triple effect cycle evaporation steps successively; Preheater preheating steps and flasher evaporation step is comprised respectively in a described effect, two effects, triple effect cycle evaporation step.
2. the treatment process of high-salt wastewater according to claim 1, it is characterized in that: in a described effect circulating and evaporating step, preheater preheating steps is the effect preheater pumped into by pump by high-salt wastewater in an effect evaporation flow process, preheated by condensation hot water, arranging pre-heating temperature is 76 ~ 78 DEG C; Described flasher evaporation step evaporates for pre-warmed high-salt wastewater is pumped into an effect flasher by pump, and arranging vaporization temperature is 122 ~ 125 DEG C; By an effect forced circulation pump circulating and evaporating; The salt concn of the high-salt wastewater after one effect evaporation reaches 26 ~ 28%, carries out two effect circulating and evaporating steps.
3. the treatment process of high-salt wastewater according to claim 1, it is characterized in that: in described two effect circulating and evaporating steps preheater preheating steps be by concentration be 26 ~ 28% high-salt wastewater pump into two effect flashers by pump and evaporate, arranging vaporization temperature is 100 ~ 105 DEG C; By two effect recycle pump circulating and evaporating, triple-effect evaporation plant sent into by 78 ~ 84% materials simultaneously, and two effect enrichment tanks sent into by 14 ~ 20% materials, pump into slurry flash tank by pump.
4. the treatment process of high-salt wastewater according to claim 1, is characterized in that: two effect flash tanks material is out sent into three grades of flashers and evaporates, arranging vaporization temperature is 70 ~ 76 DEG C; By triple effect cycle pump circulating and evaporating, triple effect enrichment tank sent into by material, and 10 ~ 15% circulating and evaporating, 90 ~ 85% pump into slurry flash tank by pump.
5. the treatment process of high-salt wastewater according to claim 1, is characterized in that: described separating step for gas phase fraction is pumped into separating tank by pump, then enters container for storing liquid after condenser condenses, finally gets rid of; Gu material pumps into whizzer by discharging pump and carries out centrifugation, supernatant liquid is mother liquor, and it is salt crystal that solid is separated out by lower floor; Described mother liquor is returned triple effect cycle evaporation flow process and carry out the evaporation of secondary triple effect cycle, the secondary mother liquid be again separated carries out burning disposal, and it is salt crystal that solid is separated out by lower floor.
6. the treatment process of high-salt wastewater according to claim 1, is characterized in that: the initial saltiness of described high-salt wastewater is 14 ~ 25%.
CN201510321161.5A 2015-06-05 2015-06-05 High-salinity wastewater treatment method CN105016553A (en)

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Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4330373A (en) * 1980-07-25 1982-05-18 Aqua-Chem, Inc. Solar desalting plant
CN103833094A (en) * 2014-03-18 2014-06-04 江苏星瑞化工工程科技有限公司 Method for treating high-salinity wastewater
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

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4330373A (en) * 1980-07-25 1982-05-18 Aqua-Chem, Inc. Solar desalting plant
CN103833094A (en) * 2014-03-18 2014-06-04 江苏星瑞化工工程科技有限公司 Method for treating high-salinity wastewater
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

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
张绍坤: "三效蒸发器在高含盐废水处理中的应用", 《中国环保产业》 *

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