WO2022041476A1 - 含盐废水处理装置 - Google Patents

含盐废水处理装置 Download PDF

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Publication number
WO2022041476A1
WO2022041476A1 PCT/CN2020/126204 CN2020126204W WO2022041476A1 WO 2022041476 A1 WO2022041476 A1 WO 2022041476A1 CN 2020126204 W CN2020126204 W CN 2020126204W WO 2022041476 A1 WO2022041476 A1 WO 2022041476A1
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liquid
liquid outlet
inlet
wastewater treatment
outlet
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PCT/CN2020/126204
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English (en)
French (fr)
Inventor
叶伟炳
李琴
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广东闻扬环境科技有限公司
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Publication of WO2022041476A1 publication Critical patent/WO2022041476A1/zh

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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/72—Organic compounds not provided for in groups B01D53/48 - B01D53/70, e.g. hydrocarbons
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/77—Liquid phase processes
    • B01D53/78—Liquid phase processes with gas-liquid contact
    • 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
    • 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

Definitions

  • the present application relates to the technical field of mechanical equipment, and in particular, to a salt-containing wastewater treatment system.
  • thermal oxidizer adopts the "thermal oxidation" process.
  • the waste liquid waste gas pollutants and oxygen undergo an oxidation reaction at a certain temperature.
  • the reaction converts waste liquid exhaust pollutants into harmless substances, such as carbon dioxide and water vapor, which can be safely discharged.
  • solid products will be produced and remain in the thermal oxidizer, and the thermal oxidizer needs to be cleaned with chemical reagent solution, resulting in a large amount of washing wastewater.
  • the washing wastewater of the thermal oxidizer contains a lot of sodium salts, organic substances and other reducing substances, and the chemical oxygen demand (COD) of the wastewater is high, which is much higher than the wastewater discharge standard stipulated by the state.
  • the washing wastewater of the thermal oxidizer is usually mixed with other industrial wastewater, and the pollutants in the wastewater are removed by membrane osmosis treatment, microbial decomposition method and electrochemical method. Among them, a little improper treatment is likely to cause secondary pollution. , generating additional wastewater, damaging the environment, etc., while the purification efficiency is not high.
  • the application provides a salt-containing wastewater treatment device, comprising: a heat exchanger, an exhaust condenser, a crystallization separator, a gas scrubber, a steam compressor, a heater and a forced circulation pump; the first outlet of the heat exchanger
  • the liquid port is connected to the liquid inlet of the exhaust condenser, the first liquid outlet of the exhaust condenser is connected to the liquid inlet of the crystallization separator, and the air outlet of the crystallization separator is connected to the liquid inlet of the crystallization separator.
  • the air inlet of the scrubbing tower is connected, the air outlet of the scrubbing tower is connected to the air inlet of the steam compressor, the air outlet of the steam compressor is connected to the air inlet of the heater, and the The liquid outlet of the scrubbing tower is connected with the liquid inlet of the crystallization separator;
  • the liquid outlet of the crystallization separator is connected with the liquid inlet of the forced circulation pump, and the liquid outlet of the forced circulation pump is connected with the liquid inlet of the heater; the first liquid outlet of the heater The port is connected to the liquid inlet of the crystallization separator.
  • the outlet of the heater is connected to the inlet of the exhaust condenser.
  • the salt-containing wastewater treatment device further includes a first delivery pump, and the first delivery pump is connected between the liquid outlet of the gas scrubber and the liquid inlet of the crystallization separator on the pipeline.
  • the salt-containing wastewater treatment device further includes a washing liquid tank, and the liquid outlet of the washing liquid tank is connected to the liquid inlet of the gas scrubbing tower.
  • the salt-containing wastewater treatment device further includes a concentrate pump, a thickener, a solid-liquid separator, a mother liquor tank and a mother liquor pump;
  • the liquid outlet of the crystallization separator is connected with the liquid inlet of the thickener, the first liquid outlet of the thickener is connected with the liquid inlet of the solid-liquid separator, and the solid-liquid separation
  • the liquid outlet of the device is connected with the liquid outlet of the mother liquor tank, and the liquid outlet of the mother liquor tank is connected with the liquid inlet of the crystallization separator;
  • the concentrated liquid pump is arranged on the connecting pipeline between the liquid outlet of the crystallization separator and the liquid inlet of the thickener; the mother liquor pump is arranged between the liquid outlet of the mother liquor tank and the crystallizer. On the connecting line between the inlets of the separator.
  • the second liquid outlet of the thickener is connected to the liquid inlet of the crystallization separator.
  • the salt-containing wastewater treatment device further includes a mother liquor tank, a second delivery pump, a spray drying tower and a fan; the liquid inlet of the mother liquor tank is connected to the liquid outlet of the mother liquor pump, so The liquid outlet of the mother liquor tank is connected with the liquid inlet of the spray drying tower, and the liquid outlet of the spray dryer is connected with the liquid inlet of the fan; the second delivery pump is located at the bottom of the mother liquor tank.
  • the connecting pipeline between the liquid outlet and the liquid inlet of the spray drying tower.
  • the salt-containing wastewater treatment device further includes a distilled water tank; the second liquid outlet of the heater is connected to the liquid inlet of the distilled water tank, and the liquid outlet of the distilled water tank is connected to the connected to the first liquid inlet of the heat exchanger.
  • the saturated steam inlet of the crystallization separator is connected to the gas outlet of the distilled water tank.
  • the salt-containing wastewater treatment device further includes a chemical tank, and the liquid outlet of the chemical tank is connected to the liquid inlet of the crystallization separator.
  • the salt-containing wastewater treatment device of the present application can be used for the treatment of the salt-containing wastewater to be treated; during operation, the salt-containing wastewater to be treated is first preheated in the heat exchanger, and the preheated salt-containing wastewater enters the exhaust condenser In the process, the steam carried by the preheated salt-containing wastewater is condensed in the exhaust condenser, and the heat generated by the condensation further warms the salt-containing wastewater, and the condensed water is recovered to improve the thermal efficiency; the warmed waste liquid enters Flash evaporation occurs in the crystallization separator to concentrate the salty wastewater and release steam.
  • the steam is scrubbed through the gas scrubber to remove low-boiling fatty acids or other organic substances carried in the steam, thereby reducing the VOC of the steam;
  • the steam after the scrubbing It is pumped out by the steam compressor to increase the temperature and pressure, and the steam after the temperature increase is used as the evaporation heat source of the heater, which improves the thermal efficiency of the device; and the liquid outlet of the scrubbing tower is connected to the liquid inlet of the crystallizer
  • the waste liquid generated in the gas tower can be returned to the crystallization separator to participate in the evaporative crystallization process for solid-liquid separation and recovery of distilled water, so that the gas scrubbing system does not generate additional waste water, so as to achieve the purpose of zero discharge of waste water.
  • the air outlet of the heater is connected to the air inlet of the exhaust condenser, and the non-condensable steam generated during the evaporation and crystallization process of the salty wastewater can be returned to the exhaust condenser, and continues to be used as the heat source of the exhaust condenser, and the The salty wastewater conducts heat exchange, and while increasing the liquid inlet temperature, the atomized water vapor carried in the non-condensable steam is condensed into distilled water, thereby recovering water vapor and heat, thus further improving the thermal efficiency of the device.
  • FIG. 1 is a schematic structural diagram of a salt-containing wastewater treatment device according to an embodiment.
  • an embodiment of the present application provides a salt-containing wastewater treatment device 100, including: a heat exchanger 101, an exhaust condenser 102, a crystallization separator 103, a gas scrubber 104, a steam compressor 105, a heating 106 and forced circulation pump 107.
  • the first liquid outlet of the heat exchanger 101 is connected to the first liquid inlet of the exhaust condenser 102, and the first liquid outlet of the exhaust condenser 102 is connected to the liquid inlet of the crystallization separator 103, and the crystallization separator 103
  • the air outlet of the gas scrubber 104 is connected to the air inlet of the scrubber tower 104, the air outlet of the scrubber tower 104 is connected to the air inlet of the steam compressor 105, and the air outlet of the steam compressor 105 is connected to the air inlet of the heater 106.
  • the liquid outlet of the gas tower 104 is connected to the liquid inlet of the crystallization separator 103 .
  • the liquid outlet of the crystallization separator 103 is connected to the liquid inlet of the forced circulation pump 107 , and the liquid outlet of the forced circulation pump 107 is connected to the liquid inlet of the heater 106 .
  • the first liquid outlet of the heater 106 is connected to the liquid inlet of the above-mentioned crystallization separator 103 .
  • the saline wastewater treatment device 100 can be used for the treatment of saline wastewater to be treated.
  • the salty waste water to be treated is preheated in the heat exchanger 101 first, the preheated salty waste water enters the exhaust condenser 102 , and the steam carried by the preheated salty waste water flows in the exhaust condenser 102 . Condensation occurs in the process, and the heat generated by the condensation further warms the salty wastewater, and the warmed salty wastewater enters the crystallization separator 103 for flash evaporation, so that the salty wastewater is concentrated and steam is released, and the steam is washed by the gas scrubber 104.
  • the washed steam is extracted by the steam compressor 105 for temperature increase and pressure, and the heated steam is used as the evaporation heat source of the heater 106 .
  • the outlet of the heater 106 is connected to the inlet of the exhaust condenser 102 described above.
  • the non-condensable steam produced by the salty waste water in the process of evaporation and crystallization can return to the exhaust condenser 102, and continue to be used as the heat source of the exhaust condenser 102 to exchange heat with the salty waste water entering the exhaust condenser 102, While increasing the temperature of the salty wastewater, the atomized water vapor carried in the non-condensable steam is condensed into distilled water, thereby recovering the water vapor and heat, thus further improving the thermal efficiency of the device.
  • the liquid outlet of the gas scrubbing tower 104 is connected to the liquid inlet of the above-mentioned crystallization separator 103, so that the waste liquid generated in the gas scrubbing tower 104 can be returned to the crystallization separator 103 to participate in the evaporation and crystallization process, so that the gas scrubbing process does not work. Generate additional wastewater.
  • the salty wastewater is continuously heated and crystallized in the heater 106 and the crystallization separator 103, and the heated circulating liquid flows out from the heater 106 to the low-pressure crystallization separator 103. Due to the pressure The abruptly reduced circulating liquid flashes here, is concentrated, and produces secondary steam at the same time.
  • the exhaust condenser 102 is provided with an exhaust port; the treated non-condensable steam is discharged from the exhaust port.
  • the salt-containing wastewater treatment device 100 further includes a first delivery pump 117, and the first delivery pump is located on the pipeline connecting between the liquid outlet of the scrubber tower 104 and the liquid inlet of the crystallization separator 103, In order to provide the power to circulate the waste liquid of the scrubber tower 104 to the crystallization separator 103 .
  • a spray device is provided on the top of the scrubbing tower 104, and the liquid outlet of the first delivery pump 117 is connected to the spray device in the scrubber tower 104; the role of the washing liquid in the first delivery pump 117 down into the spray device in the scrubber 104.
  • the waste liquid generated after the steam is scrubbed enters the crystallization separator 103 through the connecting pipeline between the first conveying pump 117 and the crystallization separator 103 to participate in the crystallization and evaporation, separates the solid, and recovers the distilled water, so that no additional waste water is produced.
  • the salty wastewater treatment device 100 further includes a washing liquid conveying device 118 .
  • the washing liquid conveying device 118 includes a washing liquid pump 1181 and a washing liquid tank 1182.
  • the liquid outlet of the washing liquid tank 1182 is connected with the liquid inlet of the above-mentioned scrubbing tower 104.
  • the washing liquid tank 1182 is used for storing the washing liquid and transmitting it to the washing liquid.
  • Tower 104 is used.
  • the washing liquid conveying device 118 further includes a washing liquid pump 1181 , and the washing liquid pump 1181 is provided on the connecting pipeline between the liquid outlet of the washing liquid tank 1182 and the liquid inlet of the scrubbing tower 104 .
  • the washing liquid stored in the washing liquid tank 1182 is pumped into the washing tower 104 by the washing liquid washing liquid pump 1181 , and the washing liquid enters the spray device in the washing tower 104 through the first conveying pump 117 .
  • the gas-liquid reverse absorption method is adopted in the scrubber tower 104, and the scrubbing liquid is sprayed downward in the form of mist (or small droplets) through the spray device at the top of the scrubber tower 104, while the steam is sprayed down by the scrubber.
  • the bottom of the gas tower 104 is countercurrently flowed upward to achieve the purpose of full gas-liquid contact.
  • top of the scrubber tower 104 is also provided with a demisting system, and the secondary steam after the scrubbing passes through the demisting system to remove the entrained mist water droplets.
  • mist removal system of the scrubber 104 is arranged above the spray system.
  • the above-mentioned crystallization separator 103 adopts a salt leg crystallizer.
  • the top of the above-mentioned salt leg crystallizer is provided with an integrated baffle plate and a wire mesh demister.
  • the integrated baffle and wire mesh mist eliminator is adopted, which has high demisting efficiency.
  • the above salt-containing wastewater treatment device 100 further includes a concentrate pump 108 , a thickener 109 , a solid-liquid separator 110 , a mother liquor tank 111 and a mother liquor pump 112 .
  • the liquid outlet of the crystallization separator 103 is connected to the liquid inlet of the thickener 108, the first liquid outlet of the thickener 108 is connected to the liquid inlet of the solid-liquid separator 110, and the liquid outlet of the solid-liquid separator 110 is connected. It is connected to the liquid outlet of the mother liquor tank 111, and the liquid outlet of the mother liquor tank 111 is connected to the liquid inlet of the crystallization separator 103.
  • the concentrated liquid pump 108 is arranged on the connecting pipeline between the liquid outlet of the crystallization separator 103 and the liquid inlet of the thickener 108; the mother liquor pump 112 is arranged on the liquid outlet of the mother liquor tank 111 and the liquid inlet of the crystallization separator 103 on the connecting line between the ports.
  • solid-liquid separator 110 is provided with a solid outlet D.
  • the salty wastewater is evaporated and crystallized in the centrifugal separator 103 and reaches the concentration ratio required by the process, it enters the thickener 109 for pre-separation, and then passes through the solid-liquid separator 110 to separate the centrifugal mother liquor and the solid, and the solid is separated from the solid.
  • the solid outlet D on the liquid separator 110 is discharged, and the centrifugal mother liquor returns to the crystallization separator 103 through the mother liquor tank 110 and the mother liquor pump 111 to continue the evaporation and concentration process.
  • the thickener 109 is further provided with a second liquid outlet; the second liquid outlet on the thickener 109 is connected to the liquid inlet of the crystallization separator 103 .
  • the salty wastewater When the salty wastewater is concentrated to the concentration ratio required by the process, it enters the thickener 109, the crystals in the concentrated solution grow further, and the preliminary separation of solid and liquid is carried out, and the upper layer liquid flows back through the second liquid outlet in the thickener 109. Enter the crystallization separator 103, continue to participate in the evaporative crystallization, and the lower layer dope enters the solid-liquid separator 110.
  • the salty wastewater treatment device 100 further includes a distilled water tank 113 and a distilled water pump 114 .
  • the second liquid outlet of the heater 104 is connected with the liquid inlet of the distilled water tank 113, the liquid outlet of the distilled water tank 113 is connected with the liquid inlet of the distilled water pump 114, and the liquid outlet of the distilled water pump 114 is connected with the liquid inlet of the heat exchanger 101.
  • the first liquid inlet is connected.
  • the heat exchanger 101 is provided with a second liquid outlet C.
  • the steam generated by the evaporative crystallization of the saline waste water is returned to the heater 104 as an evaporation heat source, and after heat exchange is performed with the circulating liquid entering the heat exchange tube of the heater 104, distilled water is obtained by condensation, and the distilled water is stored in the distilled water tank 113, It is transported by the distilled water pump 114 to the heat exchanger 101 as a heat source, and after heat exchange with the salty wastewater, it is discharged from the system through the second liquid outlet C on the heat exchanger 101, so that a large amount of heat discharged from the distilled water can be recovered and the thermal efficiency can be improved. , and the recovered distilled water meets the discharge standard: COD: 100mg/L.
  • the second liquid outlet of the exhaust condenser 102 is connected to the liquid inlet of the distilled water tank 113 .
  • the distilled water produced in the exhaust condenser 102 is stored in the distilled water tank 113 for further recovery of the distilled water.
  • the distilled water tank 113 is further provided with a gas outlet, and the steam outlet is connected to the saturated steam inlet of the crystallization separator 103 .
  • the saturated steam generated by the condensed water flowing into the distilled water tank 113 is returned to the above-mentioned crystallization separator 103 for forced circulation, which further improves the thermal efficiency of the device, further ensures the overall thermal balance of the device and ensures the stability of operating conditions.
  • the crystallization separator 103 is also provided with a saturated steam inlet E. According to the needs of practical applications, a small amount of additional saturated steam is supplied through the saturated steam inlet E of the crystallization separator 103 to maintain the overall thermal balance of the device and ensure stable operating conditions.
  • the salty wastewater treatment device 100 further includes a feed liquid tank 115 and a feed liquid delivery pump 116 , and the liquid outlet of the feed liquid delivery pump 116 is connected to the second liquid inlet on the heat exchanger 101 .
  • the material liquid tank 115 is provided with a material liquid inlet A and a tap water inlet C.
  • the salty wastewater enters the device through the feed liquid inlet A.
  • the salt-containing wastewater treatment device 10 further includes a cleaning device 119 , the cleaning device 119 includes a chemical tank 1192 , and the liquid outlet of the chemical tank 1192 is connected to the liquid inlet of the crystallization separator 103 .
  • the chemical tank 1192 is used to store the chemical and transmit it to the crystallizer 103 for cleaning the crystallizer 103 .
  • the cleaning device 119 further includes a chemical pump 1191 , and the chemical pump 1191 is arranged on the connecting pipeline between the liquid outlet of the chemical tank 1192 and the liquid inlet of the crystallization separator 103 .
  • the chemicals stored in the chemical tank 1192 are pumped into the crystallization separator 103 through the chemical pump 1191, and a PLC automatic control device is set up to control the cleaning device 119 to regularly clean the crystallization separator 103, which can ensure long-term water treatment and effluent. Water quality is stable.
  • the salt-containing wastewater treatment device 100 further includes a mother liquor tank 120 , a second delivery pump 121 , a spray drying tower 123 and a fan 124 .
  • the liquid inlet of the mother liquor tank 120 is connected with the liquid outlet of the mother liquor pump 121, the liquid outlet of the mother liquor tank 120 is connected with the liquid inlet of the spray drying tower 123, and the liquid outlet of the spray dryer 123 is connected with the liquid inlet of the fan 124. connect.
  • the second delivery pump 121 is located on the connecting pipeline between the liquid outlet of the mother liquor tank 120 and the liquid inlet of the spray drying tower 123 .
  • the centrifugal mother liquor in the mother liquor pump 111 When the centrifugal mother liquor in the mother liquor pump 111 reaches the concentration multiple required by the process, the centrifugal mother liquor enters the spray drying tower 123 through the concentrated liquor tank 120 and the second conveying pump 121, and is dried into a solid in a very short time. Further, the spray drying tower 123 is provided with a cyclone separator. The solids are continuously output from the bottom of the spray drying tower 123 and the cyclone separator, and the exhaust gas is evacuated by the fan 124 .
  • the fan 124 is provided with a cooling water outlet G, a cooling water inlet F and an exhaust port, and the exhaust gas is discharged through the exhaust port.
  • the salt-containing wastewater treatment device of the present application can treat wastewater containing sodium salts.
  • the wastewater containing sodium salts is a washing wastewater of a regenerative thermal oxidizer, and the water quality of the wastewater: pH: 7-8 , COD: 1300 mg/L, NaHCO 3 : 10000 mg/L, NaHSO 3 : 30000 mg/L, Na 2 SO 3 : 70000 mg/L.
  • the salty waste water to be treated is preheated in the heat exchanger 101 first, the preheated salty waste water enters the exhaust condenser 102, and the steam carried by the preheated salty waste water is discharged in the exhaust gas. Condensation occurs in the condenser 102, and the heat generated by the condensation further warms the salty waste water, and the waste liquid after the warming enters the crystallization separator 103 for flash evaporation, concentrating the salty waste water and releasing steam, and the steam passes through the gas scrubber 104.
  • Washing is carried out to remove low-boiling fatty acids or other organic substances carried in the steam, thereby reducing the VOC in the steam; the steam after the washing is extracted by the steam compressor 105 to increase the temperature and pressure, and the warmed steam is used as the heater 106.
  • the evaporation heat source is condensed to obtain distilled water after heat exchange.
  • the distilled water is stored in the distilled water tank 113, and is transported to the heat exchanger 101 by the distilled water pump 114 as a heat source.
  • Outlet C exits the system.
  • the non-condensable steam generated during the evaporation and crystallization process of the salty wastewater can return to the exhaust condenser 102 and continue to be used as the heat source of the exhaust condenser 102 to exchange heat with the salty wastewater.
  • the atomized water vapor carried in the non-condensable steam is condensed into distilled water, thereby recovering water vapor and heat.
  • the liquid outlet of the scrubbing tower 104 is connected to the liquid inlet of the above-mentioned crystallization separator 103, so that the waste liquid generated in the scrubbing tower 104 can be returned to the crystallization separator to participate in the evaporation and crystallization process, so that the scrubbing system does not produce additional waste water.
  • the warmed waste liquid enters the crystallization separator 103 and is mixed with the original circulating liquid, and the resulting mixed liquid is shunted to the heat exchange tube of the heater 106 under the action of the forced circulating pump 107 for heating and evaporation.
  • the heated mixed liquid flows out from the heater to the low-pressure crystallization separator 103. Due to the sudden drop in pressure, the circulating liquid flashes here to obtain a concentrated liquid, and at the same time, secondary steam is generated, and the secondary steam continues to enter the gas scrubbing tower to continuously Heat and distilled water are recovered.
  • the lye is sprayed out from the spray device provided at the top of the scrubber 104 to remove low-boiling fatty acids or other organic substances carried in the steam, thereby reducing the VOC in the steam, improving the quality of the effluent, and making the recovered distilled water reach Emission standard: COD: 100mg/L.
  • the concentrated liquid When the concentrated liquid reaches the concentration ratio required by the process, it enters the thickener 109, the crystals in the concentrated liquid further grow, and the preliminary separation of solid and liquid is performed, and the upper layer liquid flows back into the crystal through the second liquid outlet in the thickener 109.
  • Separator 103 continues to participate in evaporative crystallization, the lower layer concentrated liquid enters solid-liquid separator 110, separates centrifugal mother liquor and solid, solid is discharged from solid outlet D on solid-liquid separator 110, and centrifugal mother liquor passes through mother liquor tank 110, mother liquor pump successively 111 returns to the crystallization separator 103 to continue the evaporative concentration process.
  • the centrifugal mother liquor When the centrifugal mother liquor reaches the concentration multiple required by the process, the centrifugal mother liquor enters the mother liquor tank 120, enters the spray drying tower 123 through the second delivery pump 121, and is dried to obtain a solid, and the solid is continuously output by the bottom of the spray drying tower 123 and the cyclone separator, The exhaust gas is evacuated by fan 124 .
  • the washing liquid in the gas washing system is lye;
  • the forced circulation pump adopts VFD (variable frequency) control, the system is initially started to run, and the frequency is automatically adjusted according to the specific gravity and the automatic detection of the outlet pressure within the range of 0 to 50 Hz, so that the To meet the requirement of circulation flow; the flow rate of each heat exchange tube in the forced circulation pump is controlled at 1.5m/s ⁇ 3.5m/s to reduce the probability of scaling and avoid affecting the heat exchange efficiency.
  • VFD variable frequency

Abstract

一种含盐废水处理装置，包括：换热器（101）、排气冷凝器（102）、结晶分离器（103）、洗气塔（104）、蒸汽压缩机（105）、强制循环泵（107）及加热器（106）；其中，换热器（101）的第一出液口与排气冷凝器（102）的进液口连接，排气冷凝器（102）的第一出液口与结晶分离器（103）的进液口连接，结晶分离器（103）的出气口与洗气塔（104）的进气口连接，洗气塔（104）的出气口与蒸汽压缩机（105）的进气口连接，蒸汽压缩机（105）的出气口与加热器（106）的进气口连接，洗气塔（104）的出液口与结晶分离器（103）的进液口连接；结晶分离器（103）的出液口与强制循环泵（107）的进液口连接，强制循环泵（107）的出液口与加热器（106）的进液口连接，加热器（106）的第一出液口与结晶分离器（103）的进液口连接。

Description

含盐废水处理装置
相关申请的交叉引用
本申请要求于2020年8月31日提交中国专利局、申请号为2020218662888、发明名称为“含盐废水处理装置”的中国专利申请的优先权，其全部内容通过引用结合在本申请中。
技术领域
本申请涉及机械设备技术领域，特别是涉及一种含盐废水处理系统。
技术背景
在生活及各种工生产过程会产生的大量的废液废气，在将废液废气排放到环境中之前，需要用热氧化器对其进行有效的摧毁处理，从而大大减少废液废气污染物的排放。为摧毁废液废气污染物中的有害成分，热氧化器采用了“热氧化”工艺，在热氧化工艺过程中，废液废气污染物与氧气在一定温度条件下发生氧化反应，通过这种化学反应，将废液废气污染物转化为无害的物质，如二氧化碳和水蒸汽，可以安全地排放。在氧化反应过程中，会产生固体产物残留在热氧化器，需要通过化学试剂液对热氧化器进行清洗，从而产生大量的洗涤废水。
热氧化器的洗涤废水含有较多的钠盐、有机物质以及其他还原物质，废水的化学需氧量(COD)高，远高于国家规定的废水排放标准。
传统工艺中，通常将热氧化器的洗涤废水和其他工业废水混合，通过膜渗透处理、微生物分解法以及电化学法等方法除去废水中污染物，其中，稍有处理不当，容易造成二次污染，产生额外的废水，破坏环境等，同时净化效率不高。
因此，现有技术还有待于改进和发展。
发明内容
基于此，有必要提供一种高效且节能、且零排放废水的含盐废水处理装置。
本申请提供一种含盐废水处理装置，包括：换热器、排气冷凝器、结晶分离器、洗气塔、蒸汽压缩机、加热器及强制循环泵；所述换热器的第一出液口与所述排气冷凝器的进液口连接，所述排气冷凝器的第一出液口与所述结晶分离器的进液口连接，所述结晶分离器的出气口与所述洗气塔的进气口连接，所述洗气塔的出气口与所述蒸汽压缩机的进气口连接，所述蒸汽压缩机的出气口与所述加热器的进气口连接，所述洗气塔的出液口与所述结晶分离器的进液口连接；
所述结晶分离器的出液口与所述强制循环泵的进液口连接，所述强制循环泵的出液口与所述加热器的进液口连接；所述加热器的第一出液口与所述结晶分离器的进液口连接。
在其中一些实施例中，所述加热器的出气口与所述排气冷凝器的进气口连接。
在其中一些实施例中，所述含盐废水处理装置还包括第一输送泵，所述第一输送泵位于所述洗气塔的出液口与所述结晶分离器的进液口之间连接的管路上。
在其中一些实施例中，所述含盐废水处理装置还包括洗液罐，所述洗液罐的出液口与所述洗气塔的进液口连接。
在其中一些实施例中，所述含盐废水处理装置还包括浓缩液泵、稠厚器、固液分离器、母液罐及母液泵；
所述结晶分离器的出液口与所述稠厚器的进液口连接，所述稠厚器的第一出液口与所述固液分离器的进液口连接，所述固液分离器的出液口与所述母液罐的出液口连接，所述母液罐的出液口与所述结晶分离器的进液口连接；
所述浓缩液泵的设于结晶分离器的出液口与所述稠厚器的进液口之间的 连接管路上；所述母液泵设于所述母液罐的出液口与所述结晶分离器的进液口之间的连接管路上。
在其中一些实施例中，所述稠厚器的第二出液口与所述结晶分离器的进液口连接。
在其中一些实施例中，所述含盐废水处理装置还包括母液罐、第二输送泵、喷雾干燥塔和风机；所述母液罐的进液口与所述母液泵的出液口连接，所述母液罐的出液口与所述喷雾干燥塔的进液口连接，所述喷雾干燥器的出液口与所述风机的进液口连接；所述第二输送泵位于所述母液罐的出液口与所述喷雾干燥塔的进液口之间的连接管路上。
在其中一些实施例中，所述含盐废水处理装置还包括蒸馏水罐；所述加热器的第二出液口与所述蒸馏水罐的进液口连接，所述蒸馏水罐的出液口与所述换热器的第一进液口连接。
在其中一些实施例中，所述结晶分离器饱和蒸汽入口与所述蒸馏水罐的出气口连接。
在其中一些实施例中，所述含盐废水处理装置还包括化学药剂罐，所述化学药剂罐的出液口与所述结晶分离器的进液口连接。
本申请的含盐废水处理装置，可用于待处理的含盐废水的处理；工作时，待处理的含盐废水先在换热器进行预热，预热后的含盐废水进入排气冷凝器中，预热后的含盐废水携带的蒸汽在排气冷凝器中发生冷凝，冷凝产生的热量对含盐废水进一步提温，且回收了冷凝水，提高了热效率；提温后的废液进入结晶分离器中发生闪蒸，使含盐废水浓缩并释放蒸汽，蒸汽经洗气塔进行洗气，去除蒸汽中携带的低沸点脂肪酸或其他有机物质，从而降低蒸汽的VOC；洗气后的蒸汽被蒸汽压缩机抽出进行升温升压，提温后的蒸汽作为加热器的蒸发热源，提高了装置的热效率；且，洗气塔的出液口与结晶分离器的进液口连接，如此，洗气塔中产生的废液可回到结晶分离器参与蒸发结晶过程，进行固液分离，回收蒸馏水，使洗气系统不产生额外的废水，从而达到零排放废水的目的。
进一步地，加热器的出气口与排气冷凝器的进气口连接，含盐废水在蒸发结晶过程中产生的不凝汽能回到排气冷凝器，继续作为排气冷凝器的热源，与含盐废水进行换热，在提高进液温度的同时，不凝汽中携带的雾化的水蒸汽冷凝成蒸馏水，从而回收水蒸气和热量，如此进一步提高了装置的热效率。
附图说明
图1为一实施例的含盐废水处理装置的结构示意图。
具体实施方式
为了便于理解本申请，下面将参照相关附图对本申请进行更全面的描述。附图中给出了本申请的较佳实施例。但是，本申请可以以许多不同的形式来实现，并不限于本文所描述的实施例。相反地，提供这些实施例的目的是使对本申请的公开内容的理解更加透彻全面。
需要说明的是，当元件被称为“固定于”另一个元件，它可以直接在另一个元件上或者也可以存在居中的元件。当一个元件被认为是“连接”另一个元件，它可以是直接连接到另一个元件或者可能同时存在居中元件。
除非另有定义，本文所使用的所有的技术和科学术语与属于本申请的技术领域的技术人员通常理解的含义相同。本文中在本申请的说明书中所使用的术语只是为了描述具体的实施例的目的，不是旨在于限制本申请。本文所使用的术语“和/或”包括一个或多个相关的所列项目的任意的和所有的组合。
请参阅图1，本申请一实施方式提供了一种含盐废水处理装置100，包括：换热器101、排气冷凝器102、结晶分离器103、洗气塔104、蒸汽压缩机105、加热器106及强制循环泵107。
换热器101的第一出液口与排气冷凝器102的第一进液口连接，排气冷凝器102的第一出液口与结晶分离器103的进液口连接，结晶分离器103的出气口与洗气塔104的进气口连接，洗气塔104的出气口与蒸汽压缩机105 的进气口连接，蒸汽压缩机105的出气口与加热器106的进气口连接，洗气塔104的出液口与结晶分离器103的进液口连接。
结晶分离器103的出液口与强制循环泵107的进液口连接，强制循环泵107的出液口与加热器106的进液口连接。加热器106的第一出液口与上述结晶分离器103的进液口连接。
含盐废水处理装置100可用于待处理的含盐废水的处理。工作时，待处理的含盐废水先在换热器101进行预热，预热后的含盐废水进入排气冷凝器102中，预热后的含盐废水携带的蒸汽在排气冷凝器102中发生冷凝，冷凝产生的热量对含盐废水进一步提温，提温后的含盐废水进入结晶分离器103中发生闪蒸，使含盐废水浓缩并释放蒸汽，蒸汽经洗气塔104进行洗气，去除蒸汽中携带的低沸点脂肪酸或其他有机物质，从而降低蒸汽中的VOC；洗气后的蒸汽被蒸汽压缩机105抽出进行升温升压，升温后的蒸汽作为加热器106的蒸发热源。
在其中一些实施例中，加热器106的出气口与上述排气冷凝器102的进气口连接。
工作时，含盐废水在蒸发结晶过程中产生的不凝汽能回到排气冷凝器102，继续作为排气冷凝器102的热源，与进入排气冷凝器102的含盐废水进行换热，在提高含盐废水温度的同时，不凝汽中携带的雾化的水蒸汽冷凝成蒸馏水，从而回收水蒸气和热量，如此进一步提高了装置的热效率。
同时，洗气塔104的出液口与上述结晶分离器103的进液口连接，如此，洗气塔104中产生的废液可回到结晶分离器103参与蒸发结晶过程，使洗气过程不产生额外的废水。
在强制循环泵105的作用下，含盐废水在加热器106和结晶分离器103中不断进行加热、结晶过程，加热后的循环液从加热器106流出到低压的结晶分离器103中，由于压力骤然降低循环液在此发生闪蒸，得到浓缩，同时产生二次蒸汽。
进一步的，排气冷凝器102上设置有排气口；经处理后的不凝汽由排气 口排出。
在其中一些实施例中，含盐废水处理装置100还包括第一输送泵117，第一输送泵位于洗气塔104的出液口与结晶分离器103的进液口之间连接的管路上，以提供洗气塔104的废液循环至结晶分离器103的动力。
在其中一些实施例中，洗气塔104的顶部设置有喷淋装置，第一输送泵117的出液口与洗气塔104中的喷淋装置连接；洗液在第一输送泵117的作用下进入洗气塔104中的喷淋装置。
蒸汽经洗气后产生的废液经第一输送泵117与结晶分离器103的连接管道进入结晶分离器103参与结晶蒸发，分离出固体，回收蒸馏水，从而不产生额外的废水。
进一步地，含盐废水处理装置100还包括洗液输送装置118。洗液输送装置118包括洗液泵1181和洗液罐1182，洗液罐1182的出液口与上述洗气塔104的进液口连接，洗液罐1182用于储存洗液并传输至洗气塔104使用。进一步地，洗液输送装置118还包括洗液泵1181，洗液泵1181设于洗液罐1182的出液口与洗气塔104的进液口之间的连接管路上。通过洗液洗液泵1181将储存在洗液罐1182中的洗液泵入洗气塔104中，洗液经过第一输送泵117进入洗气塔104中的喷淋装置。
在其中一些实施例中，洗气塔104采用气液逆向吸收方式，洗液通过洗气塔104塔顶的喷淋装置向下雾状(或小液滴)喷洒而下，而蒸汽则由洗气塔104的塔底向上逆流，以达到气液充分接触的目的。
进一步地，洗气塔104的塔顶还设置有除雾系统，洗气后的二次蒸汽经除雾系统，除去携带的雾状水滴。
可理解，洗气塔104的除雾系统设置在喷淋系统的上方。
在其中一些实施例中，上述结晶分离器103采用盐腿结晶器。上述盐腿结晶器的顶部设置有一体式的折流板加丝网除雾器。采用一体式的折流板加丝网除雾器，除雾效率高。
在其中一些实施例中，上述含盐废水处理装置100还包括浓缩液泵108、 稠厚器109、固液分离器110、母液罐111及母液泵112。
结晶分离器103的出液口与稠厚器108的进液口连接，稠厚器108的第一出液口与固液分离器110的进液口连接，固液分离器110的出液口与母液罐111的出液口连接，母液罐111的出液口结晶分离器103的进液口连接。
浓缩液泵108设于结晶分离器103的出液口与稠厚器108的进液口之间的连接管路上；母液泵112设于母液罐111的出液口与结晶分离器103的进液口之间的连接管路上。
进一步地，固液分离器110上设置有固体出口D。
工作时，当含盐废水在离心分离器103中蒸发结晶达到工艺要求的浓缩倍数后，进入稠厚器109进行预分离，再经固液分离器110，分离出离心母液和固体，固体从固液分离器110上的固体出口D排出，离心母液经母液罐110、母液泵111回到结晶分离器103继续进行蒸发浓缩过程。
在其中一些实施例中，稠厚器109上还设有第二出液口；稠厚器109上的第二出液口与上述结晶分离器103的进液口连接。
当含盐废水浓缩达到工艺要求的浓缩倍数后，进入稠厚器109中，浓缩液中的晶体进一步生长，进行固液的初步分离，上层液体通过稠厚器109中的第二出液口回流进结晶分离器103，继续参与蒸发结晶，下层浓液进入固液分离器110。
在其中一些实施例中，含盐废水处理装置100还包括蒸馏水罐113和蒸馏水泵114。
加热器104的第二出液口与蒸馏水罐113的进液口的连接，蒸馏水罐113的出液口与蒸馏水泵114的进液口连接，蒸馏水泵114的出液口与换热器101的第一进液口连接。进一步地，换热器101设有第二出液口C。
含盐废水经蒸发结晶产生的蒸汽回到加热器104的中作为蒸发热源，与进入加热器104的换热管中的循环液进行热交换后，冷凝得到蒸馏水，蒸馏水储存在蒸馏水罐113中，由蒸馏水泵114输送至换热器101作为热源，与含盐废水进行换热后，经换热器101上的第二出液口C排出系统，这样可以 大量回收蒸馏水外排的热量，提高热效率，且回收的蒸馏水达到排放标准：COD:100mg/L。在其中一些实施例中，排气冷凝器102的第二出液口与蒸馏水罐113的进液口的连接。排气冷凝器102中产生的蒸馏水，储存在蒸馏水罐113中，以进一步回收蒸馏水。
在其中一些实施例中，进一步地，蒸馏水罐113还设有出气口，且蒸汽出口与结晶分离器103的饱和蒸汽入口连接。如此，流入蒸馏水罐113的冷凝水产生的饱和蒸汽又回到上述结晶分离器103中，进行强制循环，进一步提高了装置的热效率，进一步保证装置总体的热平衡和保证操作条件的稳定。
进一步地，结晶分离器103还设有饱和蒸汽入口E。根据实际应用的需要，通过上述结晶分离器103的饱和蒸汽入口E，通入少量的额外饱和蒸汽补充，以保持装置总体的热平衡和保证操作条件的稳定。
在其中一些实施例中，含盐废水处理装置100还包括料液罐115和料液输送泵116，料液输送泵116的出液口与换热器101上的第二进液口连接。
进一步地，料液罐115设有料液进口A和自来水进口C。含盐废水经料液进口A进入装置。
进一步地，含盐废水处理装置10还包括清洗装置119，清洗装置119包括化学药剂罐1192，化学药剂罐1192的出液口与结晶分离器103的进液口连接。化学药剂罐1192用于储存化学药剂并传输至结晶分离器103，以清洗结晶分离器103。进一步地，清洗装置119还包括化学药剂泵1191，化学药剂泵1191设于化学药剂罐1192的出液口与结晶分离器103的进液口之间的连接管路上。
储存在化学药剂罐1192中的化学药剂通过化学药剂泵1191泵入结晶分离器103，并设置PLC自动控制装置，控制清洗装置119定期对结晶分离器103进行清洗，可以保证长时期处理水量和出水水质稳定。
在其中一些实施例中，含盐废水处理装置100还包括母液罐120、第二输送泵121、喷雾干燥塔123和风机124。
母液罐120的进液口与母液泵121的出液口连接，母液罐120的出液口 与喷雾干燥塔123的进液口连接，喷雾干燥器123的出液口与风机124的进液口连接。第二输送泵121位于母液罐120的出液口与喷雾干燥塔123的进液口之间的连接管路上。
当母液泵111中的离心母液达到工艺要求的浓缩倍数后，离心母液经浓缩液罐120、第二输送泵121进入喷雾干燥塔123，在极短的时间内被干燥为成固体。进一步地，喷雾干燥塔123中设置有旋风分离器。固体连续地由喷雾干燥塔123的底部和旋风分离器中输出，废气由风机124排空。
在其中一些实施例中，风机124上设置有冷却水出口G、冷却水进口F与排气口，废气经排气口排出。
本申请的含盐废水处理装置可以处理含钠盐的废水，在本申请的具体示例中，含钠盐的废水为一种蓄热式热氧化器的洗涤废水，废水水质：pH:7～8，COD:1300mg/L，NaHCO 3:10000mg/L，NaHSO 3：30000mg/L，Na 2SO 3：70000mg/L。
请继续参考图1，在本申请的具体示例中，含盐废水的处理过程如下：
含盐废水工作时，待处理的含盐废水先在换热器101进行预热，预热后的含盐废水进入排气冷凝器102中，预热后的含盐废水携带的蒸汽在排气冷凝器102中发生冷凝，冷凝产生的热量对含盐废水进一步提温，提温后的废液进入结晶分离器103中发生闪蒸，使含盐废水浓缩并释放蒸汽，蒸汽经洗气塔104进行洗气，去除蒸汽中携带的低沸点脂肪酸或其他有机物质，从而降低蒸汽中的VOC；洗气后的蒸汽被蒸汽压缩机105抽出进行升温升压，提温后的蒸汽作为加热器106的蒸发热源，经热交换后冷凝得到蒸馏水，蒸馏水储存在蒸馏水罐113中，由蒸馏水泵114输送至换热器101作为热源，与含盐废水进行换热后，经换热器101上的第二出液口C排出系统。
与此同时，含盐废水在蒸发结晶过程中产生的不凝汽能回到排气冷凝器102，继续作为排气冷凝器102的热源，与含盐废水进行换热，在提高进液温度的同时，不凝汽中携带的雾化的水蒸汽冷凝成蒸馏水，从而回收水蒸气和热量。同时，洗气塔104的出液口与上述结晶分离器103的进液口连接，如 此，洗气塔104中产生的废液可回到结晶分离器参与蒸发结晶过程，使洗气系统不产生额外的废水。
提温后的废液进入结晶分离器103中与原有的循环液混合后，产生的混合液在强制循环泵107的作用下，分流至加热器106的换热管中，进行加热、蒸发。加热后的混合液从加热器流出到低压的结晶分离器103中，由于压力骤然降低循环液在此发生闪蒸，得到浓缩液，同时产生二次蒸汽，二次蒸汽继续进入洗气塔以不断回收热量和蒸馏水。
具体地，洗气塔104顶部设置的喷淋装置中喷淋出碱液，以去除蒸汽中携带的低沸点脂肪酸或其他有机物质，从而降低蒸汽中的VOC，提高出水水质，使回收的蒸馏水达到排放标准：COD:100mg/L。
当浓缩液达到工艺要求的浓缩倍数后，进入稠厚器109中，浓缩液中的晶体进一步生长，进行固液的初步分离，上层液体通过稠厚器109中的第二出液口回流进结晶分离器103，继续参与蒸发结晶，下层浓液进入固液分离器110，分离出离心母液和固体，固体从固液分离器110上的固体出口D排出，离心母液先后经母液罐110、母液泵111回到结晶分离器103继续进行蒸发浓缩过程。
当离心母液达到工艺要求的浓缩倍数后，离心母液进入母液罐120，经第二输送泵121进入喷雾干燥塔123，干燥得到固体，固体连续地由喷雾干燥塔123的底部和旋风分离器输出，废气由风机124排空。
在上述具体示例中，洗气系统中的洗液为碱液；强制循环泵采用VFD(变频)控制，初始启动系统运行，频率根据比重以及出口压力自动检测保持在0～50Hz范围自动调节，以满足循环流量需求；强制循环泵中每根换热管的流速控制在1.5m/s～3.5m/s，降低结垢概率，以免影响换热效率。
以上所述实施例的各技术特征可以进行任意的组合，为使描述简洁，未对上述实施例中的各个技术特征所有可能的组合都进行描述，然而，只要这些技术特征的组合不存在矛盾，都应当认为是本说明书记载的范围。
以上所述实施例仅表达了本申请的几种实施方式，其描述较为具体和详 细，但并不能因此而理解为对本申请专利范围的限制。应当指出的是，对于本领域的普通技术人员来说，在不脱离本申请构思的前提下，还可以做出若干变形和改进，这些都属于本申请的保护范围。因此，本申请专利的保护范围应以所附权利要求为准。

Claims (10)

  1. 一种含盐废水处理装置，包括：换热器、排气冷凝器、结晶分离器、洗气塔、蒸汽压缩机、加热器及强制循环泵；所述换热器的第一出液口与所述排气冷凝器的进液口连接，所述排气冷凝器的第一出液口与所述结晶分离器的进液口连接，所述结晶分离器的出气口与所述洗气塔的进气口连接，所述洗气塔的出气口与所述蒸汽压缩机的进气口连接，所述蒸汽压缩机的出气口与所述加热器的进气口连接，所述洗气塔的出液口与所述结晶分离器的进液口连接；
    所述结晶分离器的出液口与所述强制循环泵的进液口连接，所述强制循环泵的出液口与所述加热器的进液口连接；所述加热器的第一出液口与所述结晶分离器的进液口连接。
  2. 如权利要求1所述的含盐废水处理装置，其中所述加热器的出气口与所述排气冷凝器的进气口连接。
  3. 如权利要求1所述的含盐废水处理装置，其中所述含盐废水处理装置还包括第一输送泵，所述第一输送泵位于所述洗气塔的出液口与所述结晶分离器的进液口之间连接的管路上。
  4. 如权利要求1所述的含盐废水处理装置，其中所述含盐废水处理装置还包括洗液罐，所述洗液罐的出液口与所述洗气塔的进液口连接。
  5. 如权利要求1所述的含盐废水处理装置，其中所述含盐废水处理装置还包括浓缩液泵、稠厚器、固液分离器、母液罐及母液泵；
    所述结晶分离器的出液口与所述稠厚器的进液口连接，所述稠厚器的第一出液口与所述固液分离器的进液口连接，所述固液分离器的出液口与所述母液罐的出液口连接，所述母液罐的出液口与所述结晶分离器的进液口连接；
    所述浓缩液泵的设于结晶分离器的出液口与所述稠厚器的进液口之间的连接管路上；所述母液泵设于所述母液罐的出液口与所述结晶分离器的进液口之间的连接管路上。
  6. 如权利要求5所述的含盐废水处理装置，其中所述稠厚器的第二出液 口与所述结晶分离器的进液口连接。
  7. 如权利要求6所述的含盐废水处理装置，其中所述含盐废水处理装置还包括母液罐、第二输送泵、喷雾干燥塔和风机；所述母液罐的进液口与所述母液泵的出液口连接，所述母液罐的出液口与所述喷雾干燥塔的进液口连接，所述喷雾干燥器的出液口与所述风机的进液口连接；所述第二输送泵位于所述母液罐的出液口与所述喷雾干燥塔的进液口之间的连接管路上。
  8. 如权利要求1所述的含盐废水处理装置，其中所述含盐废水处理装置还包括蒸馏水罐；所述加热器的第二出液口与所述蒸馏水罐的进液口连接，所述蒸馏水罐的出液口与所述换热器的第一进液口连接。
  9. 如权利要求8所述的含盐废水处理装置，其中所述结晶分离器饱和蒸汽入口与所述蒸馏水罐的出气口连接。
  10. 如权利要求1所述的含盐废水处理装置，其中所述含盐废水处理装置还包括化学药剂罐，所述化学药剂罐的出液口与所述结晶分离器的进液口连接。
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