WO2018045708A1 - 一种间接空冷机组热回收及水处理装置与方法 - Google Patents

一种间接空冷机组热回收及水处理装置与方法 Download PDF

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WO2018045708A1
WO2018045708A1 PCT/CN2017/072019 CN2017072019W WO2018045708A1 WO 2018045708 A1 WO2018045708 A1 WO 2018045708A1 CN 2017072019 W CN2017072019 W CN 2017072019W WO 2018045708 A1 WO2018045708 A1 WO 2018045708A1
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water
membrane distillation
tank
inlet end
condenser
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PCT/CN2017/072019
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English (en)
French (fr)
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刘海洋
齐勇
江澄宇
郭清温
郭永红
夏怀祥
李叶红
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大唐环境产业集团股份有限公司
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Publication of WO2018045708A1 publication Critical patent/WO2018045708A1/zh

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    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
    • C02F1/447—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by membrane distillation
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F22—STEAM GENERATION
    • F22D—PREHEATING, OR ACCUMULATING PREHEATED, FEED-WATER FOR STEAM GENERATION; FEED-WATER SUPPLY FOR STEAM GENERATION; CONTROLLING WATER LEVEL FOR STEAM GENERATION; AUXILIARY DEVICES FOR PROMOTING WATER CIRCULATION WITHIN STEAM BOILERS
    • F22D11/00—Feed-water supply not provided for in other main groups
    • F22D11/02—Arrangements of feed-water pumps
    • F22D11/06—Arrangements of feed-water pumps for returning condensate to boiler

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  • the invention relates to the field of energy saving and environmental protection technologies, in particular to an indirect air cooling unit heat recovery and water treatment device and method.
  • Coal-fired power generation is China's main form of power supply. In China's water-deficient areas, some coal-fired power plants use air-cooled units to generate electricity. Air-cooled units are generally divided into direct air-cooled units and indirect air-cooled units. Indirect air cooling is divided into two types: Heller and Harmon, and the circulating water systems are closed. Indirect air cooling system with surface condenser - also known as Harmon system, consisting of surface condenser, air cooling radiator, circulating water pump and nitrogen filling protection system, circulating water replenishing system, radiator cleaning system and air cooling The tower is composed.
  • the system is basically similar to the conventional wet cooling system, except that the air cooling tower is used instead of the wet cooling tower, and the closed circulating cooling water system is replaced by the closed circulating cooling water system, and the circulating water is demineralized.
  • the process flow of the indirect air cooling system of the surface condenser is: the circulating water enters the water side of the surface condenser through the surface heat exchange, and the steam turbine of the steam turbine side of the condenser is cooled, and the circulating water after being heated is sent to the circulating water pump.
  • the air cooling tower heats the surface with air through an air-cooled radiator, and the circulating water is cooled by air and then returned to the condenser to cool the steam exhaust of the steam turbine to form a closed loop. Therefore, a large amount of heat in the exhausted steam enters the atmosphere through the air cooling system, which not only causes waste of energy, but also causes air pollution problems. Therefore, how to recycle the heat in the spent steam has always been a key research field in the field of energy conservation.
  • Membrane distillation (MD) technology is a highly efficient membrane separation technology.
  • the hydrophobic microporous membrane is used as the separation medium, and the vapor pressure difference between the two sides of the membrane is the mass transfer driving force to realize the wastewater concentration and pure water.
  • the recycling process, MD technology has many advantages compared with the traditional membrane separation technology, such as the high retention efficiency of salt, nearly 100% retention efficiency for most non-volatile substances, and low requirements for influent water quality, operation The conditions are mild (no high-voltage equipment is required), easy operation and maintenance, membrane fouling and energy consumption are lower than conventional evaporation.
  • membrane distillation has a strong adaptability to the change of salt content in wastewater. Theoretically, as long as the solute is not saturated, the membrane module can operate normally. Since membrane distillation requires heating of raw water, the energy consumption is relatively high, which is one of the important factors limiting the large-scale application of the MD process.
  • an object of the present invention is to provide an apparatus and method for heat recovery and water treatment of an indirect air cooling unit, combining the exhaust steam condensation of the indirect air cooling unit with the membrane distillation process, and fully utilizing the residual heat of the steam as a heat source of the membrane distillation system.
  • the invention provides a heat recovery and water treatment device for an indirect air cooling unit, comprising a pretreatment device, a regulating pool, a first water pump, a condenser, an intermediate pool, a boiler, a membrane distillation device, a second water pump, and a production basin;
  • the raw water to be treated enters the water inlet end of the pretreatment device, the water outlet end of the pretreatment device is connected to the water inlet end of the conditioning tank, and the water outlet end of the conditioning pool passes through the first water pump and the The water inlet end of the condenser is connected, and the water outlet end of the condenser is connected to the water inlet end of the intermediate pool;
  • the spent steam enters the condenser, and the condensed water generated after condensation in the condenser is returned to the boiler;
  • the second water pump is located between the intermediate pool and the membrane distillation device, and the water inlet end of the second water pump is connected to the water outlet end of the intermediate water tank, and the water outlet end of the second water pump and the membrane
  • the water inlet end of the distillation apparatus is connected to the water production end of the membrane distillation apparatus; or the water outlet end of the intermediate water tank is connected to the water inlet end of the membrane distillation apparatus, the membrane distillation apparatus
  • the water producing end is connected to the water producing tank, the water inlet end of the second water pump is connected to the water outlet end of the membrane distillation device, and the water outlet end of the second water pump is connected to the water inlet end of the regulating water tank.
  • an auxiliary heating device is further included, the raw water to be treated enters the water inlet end of the pretreatment device, and the water outlet end of the pretreatment device is connected to the water inlet end of the conditioning tank, the adjustment The water outlet end of the pool is connected to the water inlet end of the condenser through the first water pump, and the water outlet end of the condenser is connected to the water inlet end of the intermediate pool, and the water outlet end of the intermediate pool The inlet end of the auxiliary heating device is connected;
  • the spent steam enters the condenser, and the condensed water generated after condensation in the condenser is returned to the boiler;
  • the first water pump is located between the auxiliary heating device and the membrane distillation device, and the water inlet end of the first water pump is connected to the water outlet end of the auxiliary heating device, and the water outlet end of the first water pump
  • the water inlet end of the membrane distillation apparatus is connected, and the water producing end of the membrane distillation apparatus is connected to the water production tank;
  • the water outlet end of the auxiliary heating device is connected to the water inlet end of the membrane distillation device, the water production end of the membrane distillation device is connected to the water production tank, and the water inlet end of the first water pump is At the water outlet end of the distillation apparatus, the water outlet end of the first water pump is connected to the water inlet end of the conditioning tank.
  • the auxiliary heating device is a steam heating device or a flue gas heating device or an electric heating device.
  • a stirring device is provided in the conditioning tank.
  • the pretreatment device is a combination of one or more of a sedimentation tank, a grease trap, an oxidation pond, a softening tank, a filter, and a biochemical tank.
  • the membrane distillation apparatus adopts one or a combination of an air gap type membrane distillation apparatus, an air sweep type membrane distillation apparatus, a vacuum air gap type membrane distillation apparatus, and a direct contact type membrane distillation apparatus.
  • the condenser is provided with a vacuum monitoring and control system and is connected to the standby cooling water system.
  • the invention also provides a heat recovery and water treatment method for an indirect air cooling unit, the method comprising the following steps:
  • Step 1 after the raw water to be treated is pretreated by the pretreatment device, enters the adjustment tank;
  • Step 2 the effluent of the regulating tank enters the condenser through the first water pump, and the exhaust steam from 55 ° C to 65 ° C enters the condenser, and the temperature of the effluent of the regulating tank rises after heat exchange Up to 40 ° C ⁇ 55 ° C, and then enter the intermediate pool, while the condensation water produced in the condenser after condensation is returned to the boiler after regenerative and deoxidation treatment;
  • Step 3 the effluent of the intermediate pool is pumped into the membrane distillation apparatus for membrane distillation concentration treatment under the suction of the second water pump; or the effluent of the intermediate pool is in the second water pump Entering the membrane distillation apparatus under pressure to perform membrane distillation concentration treatment;
  • Step 4 the concentrated water produced by the membrane distillation device is returned to the conditioning tank by the action of the second water pump, and repeat steps 2 and 3;
  • step 5 the distilled water produced by the membrane distillation apparatus enters the water production tank as production water or domestic water.
  • step 3 is replaced by:
  • the effluent of the intermediate pool enters the auxiliary heating device and is heated to 70 ° C to 95 ° C.
  • the effluent heated by the auxiliary heating device is sucked into the membrane distillation device under the suction of the second water pump.
  • the membrane distillation concentration treatment; or the effluent heated by the auxiliary heating device enters the membrane distillation apparatus under the pressure of the second water pump to perform membrane distillation concentration treatment.
  • the method further comprises: opening the stirring device in the adjusting tank to ensure uniform water quality and water temperature in the adjusting tank.
  • the setting of the auxiliary heating system can effectively improve the adaptability and flexibility of the process.
  • FIG. 1 is a schematic structural view of a heat recovery and water treatment device for an indirect air cooling unit according to a first embodiment of the present invention
  • FIG. 2 is a schematic structural view of a heat recovery and water treatment device for an indirect air cooling unit according to a second embodiment of the present invention.
  • Pretreatment device 2. Adjustment tank; 3. First water pump; 4. Condenser; 5. Intermediate pool; 6. Boiler; 7. Auxiliary heating device; 8. Membrane distillation device; 10. Producing pool.
  • Embodiment 1 as shown in FIG. 1, a heat recovery and water treatment device for an indirect air cooling unit according to a first embodiment of the present invention, comprising a pretreatment device 1, a regulating tank 2, a first water pump 3, a condenser 4, and a middle
  • the pool 5, the boiler 6, the membrane distillation unit 8, the second water pump 9, the production tank 10, and the adjustment tank 2 are provided with a stirring device.
  • the raw water to be treated enters the water inlet end of the pretreatment device 1, and the water outlet end of the pretreatment device 1 is connected to the water inlet end of the adjustment tank 2, and the water outlet end of the adjustment tank 2 passes through the water inlet of the first water pump 3 and the condenser 4.
  • the ends are connected, and the water outlet end of the condenser 4 is connected to the water inlet end of the intermediate pool 5.
  • the spent steam enters the condenser 4,
  • the condensed water generated after condensation in the condenser 4 is returned to the boiler 6.
  • the second water pump 9 is located between the intermediate water tank 5 and the membrane distillation unit 8, the water inlet end of the second water pump 9 is connected to the water outlet end of the intermediate water tank 5, and the water outlet end of the second water pump 9 is connected to the water inlet end of the membrane distillation unit 8.
  • the water producing end of the membrane distillation unit 8 is connected to the water producing tank 11; or the water outlet end of the intermediate water tank 5 is connected to the water inlet end of the membrane distillation unit 8, and the water producing end of the membrane distillation unit 8 is connected to the water producing tank 11, second
  • the water inlet end of the water pump 9 is connected to the water outlet end of the membrane distillation unit 8, and the water outlet end of the second water pump 9 is connected to the water inlet end of the conditioning tank 2.
  • the pretreatment device 1 is a combination of one or a combination of a sedimentation tank, a grease trap, an oxidation pond, a softening tank, a filter, and a biochemical pool.
  • the membrane distillation apparatus 8 employs one or a combination of an air gap type membrane distillation apparatus, an air sweep type membrane distillation apparatus, a vacuum air gap type membrane distillation apparatus, and a direct contact type membrane distillation apparatus.
  • a vacuum monitoring and control system is provided in the condenser 4 and is connected to the standby cooling water system.
  • the online cooling pressure monitoring device and the automatic control system in the condenser 4 can automatically open the standby cooling water system to make the power generation of the power plant normal. .
  • the method for producing drinking water by using the brackish water of a river around the power plant as a desalination treatment comprises the following steps:
  • Step 1 After the pretreatment of the pretreatment device 1 by flocculation, softening, filtration, oxidation, etc., the river water is used to remove suspended solids, hardness and COD pollutants in the wastewater to meet the requirements of subsequent membrane distillation water inflow, pretreated seawater. Enter the adjustment tank 2 and open the stirring device in the adjustment tank 2 to ensure uniform water quality and water temperature in the pool.
  • Step 2 the effluent of the adjustment tank 2 enters the condenser 4 through the first water pump 3, and the steam at 60 °C enters the condenser 4, and the temperature of the river water rises to 52 ° C after heat exchange, and then enters the intermediate pool 5, and simultaneously
  • the condensed water generated after condensation in the condenser 4 is returned to the boiler 6 through the heat recovery and oxygen removal treatment.
  • Step 3 the effluent of the intermediate pool 5 is sucked into the membrane distillation unit 8 by the suction of the second water pump 9 for membrane distillation concentration treatment; or, the effluent of the intermediate pool 5 enters the membrane under the pressure of the second water pump 9
  • the distillation apparatus 8 performs a membrane distillation concentration treatment.
  • step 4 the concentrated water produced by the membrane distillation unit 8 is returned to the conditioning tank 2 by the action of the second water pump 9, and steps 2 and 3 are repeated.
  • step 5 the distilled water produced by the membrane distillation unit 8 enters the production tank 10 as production water or domestic water.
  • the suction water inlet method is beneficial to reduce the seawater pressure in the membrane module and avoid the penetration of the hydrophobic membrane. At the same time, the vapor pressure difference between the membranes can be increased under the same operating conditions, which is beneficial to increase the water production of the membrane. the amount.
  • the on-line pressure monitoring device and the automatic control system in the condenser 4 automatically turn on the standby cooling water system to ensure that the power generation of the power plant is normal.
  • Embodiment 2 as shown in FIG. 2, a heat recovery and water treatment device for an indirect air cooling unit according to a second embodiment of the present invention is different from Embodiment 1 in that it further includes an auxiliary heating device 7, and the raw water to be treated enters
  • the water inlet end of the pretreatment device 1 is connected to the water inlet end of the conditioning tank 2, and the water outlet end of the conditioning tank 2 is connected to the water inlet end of the condenser 4 through the first water pump 3, and the condensing steam
  • the water outlet end of the tank 4 is connected to the water inlet end of the intermediate water tank 5, and the water outlet end of the intermediate water tank 5 is connected to the water inlet end of the auxiliary heating device 7.
  • the first water pump 9 is located between the auxiliary heating device 7 and the membrane distillation device 8, and the water inlet end of the first water pump 9 is connected to the water outlet end of the auxiliary heating device 7, and the water outlet end of the first water pump 9 and the water inlet of the membrane distillation device 8 Connected to the end, the water producing end of the membrane distillation unit 8 is connected to the production tank 11; or, the water outlet end of the auxiliary heating unit 7 is connected to the water inlet end of the membrane distillation unit 8, and the water producing end of the membrane distillation unit 8 is connected to the water producing tank 11
  • the water outlet end of the water inlet end membrane distillation device 8 of the first water pump 9 is connected to the water inlet end of the conditioning tank 2 at the water outlet end of the first water pump 9.
  • the auxiliary heating device 7 is a steam heating device or a flue gas heating device or an electric heating device.
  • the brackish water of a river around the power plant is desalinated, and the method for producing drinking water by using the indirect air cooling unit heat recovery and water treatment device comprises the following steps:
  • Step 1 After the pretreatment of the pretreatment device 1 by flocculation, softening, filtration, oxidation, etc., the river water is used to remove suspended solids, hardness and COD pollutants in the wastewater to meet the requirements of subsequent membrane distillation water inflow.
  • the pre-treated seawater enters the adjustment tank 2, and the stirring device in the adjustment tank 2 is opened to ensure uniform water quality and water temperature in the pool.
  • Step 2 the effluent of the adjustment tank 2 enters the condenser 4 through the first water pump 3, and the steam at 60 °C enters the condenser 4, and the temperature of the river water rises to 52 ° C after heat exchange, and then enters the intermediate pool 5, and simultaneously
  • the condensed water generated after condensation in the condenser 4 is returned to the boiler 6 through the heat recovery and oxygen removal treatment.
  • Step 3 in order to achieve a higher membrane distillation water production flux, the outlet water of the intermediate pool 5 enters the auxiliary heating device, and the river water temperature is heated to 80 ° C by the high temperature steam, and the heated river water is pumped by the second water pump 9 It is sucked into the membrane distillation apparatus 8 to perform membrane distillation concentration treatment; or, the heated river water enters the membrane distillation apparatus 8 under the pressure of the second water pump 9 to perform membrane distillation concentration treatment.
  • Step 4 after the membrane distillation apparatus 8 is treated, the produced concentrated water temperature is lowered to about 42 ° C while being refluxed into the conditioning tank 2 by the action of the second water pump 9, and steps 2 and 3 are repeated.
  • step 5 the distilled water produced by the membrane distillation unit 8 enters the production tank 10 as production water or domestic water.
  • the suction water inlet method is beneficial to reduce the seawater pressure in the membrane module and avoid the penetration of the hydrophobic membrane. At the same time, the vapor pressure difference between the membranes can be increased under the same operating conditions, which is beneficial to increase the water production of the membrane. the amount.
  • the area of the construction land can be limited.
  • the salt content of the concentrated water produced by the membrane distillation apparatus 8 reaches 18% or more, the concentrated water discharge system is further processed.
  • the third embodiment differs from the first embodiment in that the seawater is treated as a treatment object, and the method for performing seawater desalination treatment by the indirect air cooling unit heat recovery and water treatment device includes the following steps:
  • Step 1 After the seawater is pretreated by softening, flocculation, sedimentation, filtration, etc. of the pretreatment device 1, the suspended solids and hardness and the like are removed from the wastewater to meet the requirements of the subsequent membrane distillation water inlet, and the pretreated seawater enters the regulating tank.
  • the stirring device in the adjusting tank 2 is opened to ensure uniform water quality and water temperature in the pool.
  • Step 2 the effluent of the adjustment tank 2 enters the condenser 4 through the first water pump 3, and the exhaust gas at 63 ° C enters Condenser 4, after the heat exchange of the river water, the temperature rises to 50 ° C, and then enters the intermediate pool 5, and at the same time, the condensed water generated after condensation in the condenser 4 is returned to the boiler 6 through the heat recovery and oxygen removal treatment.
  • Step 3 the effluent of the intermediate pool 5 is sucked into the membrane distillation unit 8 by the suction of the second water pump 9 for membrane distillation concentration treatment; or, the effluent of the intermediate pool 5 enters the membrane under the pressure of the second water pump 9
  • the distillation apparatus 8 performs a membrane distillation concentration treatment.
  • step 4 the concentrated water produced by the membrane distillation unit 8 is returned to the conditioning tank 2 by the action of the second water pump 9, and steps 2 and 3 are repeated.
  • step 5 the distilled water produced by the membrane distillation unit 8 enters the production tank 10 as production water or domestic water.
  • the suction water inlet method is beneficial to reduce the seawater pressure in the membrane module and avoid the penetration of the hydrophobic membrane. At the same time, the vapor pressure difference between the membranes can be increased under the same operating conditions, which is beneficial to increase the water production of the membrane. the amount.
  • Step 1 After the seawater is pretreated by softening, flocculation, sedimentation, filtration, etc. of the pretreatment device 1, the suspended solids and hardness and the like are removed from the wastewater to meet the requirements of the subsequent membrane distillation water inlet, and the pretreated seawater enters the regulating tank.
  • the stirring device in the adjusting tank 2 is opened to ensure uniform water quality and water temperature in the pool.
  • Step 2 the effluent of the adjustment tank 2 enters the condenser 4 through the first water pump 3, and the exhaust gas at 63 °C enters the condenser 4, and the temperature of the river water rises to 50 ° C after heat exchange, and then enters the intermediate pool 5, and simultaneously
  • the condensed water generated after condensation in the condenser 4 is returned to the boiler 6 through the heat recovery and oxygen removal treatment.
  • Step 3 in order to achieve a higher membrane distillation water production flux, the outlet water of the intermediate pool 5 enters the auxiliary heating device, and the river water temperature is heated to 70 ° C by the high temperature steam, and the heated river water is pumped by the second water pump 9 It is sucked into the membrane distillation apparatus 8 to perform membrane distillation concentration treatment; or, the heated river water enters the membrane distillation apparatus 8 under the pressure of the second water pump 9 to perform membrane distillation concentration treatment.
  • step 4 after the membrane distillation apparatus 8 is treated, the produced concentrated water temperature is lowered to about 40 ° C while being refluxed into the conditioning tank 2 by the action of the second water pump 9, and steps 2 and 3 are repeated.
  • step 5 the distilled water produced by the membrane distillation unit 8 enters the production tank 10 as production water or domestic water.
  • the suction water inlet method is beneficial to reduce the seawater pressure in the membrane module and avoid the penetration of the hydrophobic membrane. At the same time, the vapor pressure difference between the membranes can be increased under the same operating conditions, which is beneficial to increase the water production of the membrane. the amount.
  • the invention aims at the disadvantages of large energy consumption and serious heat loss of the air cooling system in the direct air cooling unit power plant, combining the exhaust steam condensation of the indirect air cooling unit with the membrane distillation process, replacing the direct air cooling system by the membrane distillation system, and utilizing the residual steam heat as the membrane.
  • the heat source of the distillation system, the aqueous solution to be treated replaces the cooling water circulation of the air-cooling unit, and the exhaust steam is condensed in the condenser, and at the same time, the self-heating process is realized, and the aqueous solution to be treated is heated to enter the membrane distillation system to complete the water-making process and the aqueous solution to be treated.
  • the cooling process is suitable for the treatment of pure water or desalting of wastewater such as wastewater and seawater desalination.
  • the pretreatment process may be one or more of chemical bottoming, chemical oxidation, biological treatment, filtration, and adsorption.
  • the raw water used for treatment is power plant wastewater or domestic sewage or sea water or surface water or ground water.

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Abstract

一种间接空冷机组热回收及水处理装置，原水进入预处理装置（1），预处理装置（1）出水端与调节池（2）进水端相连，调节池（2）出水端通过第一水泵（3）与凝汽器（4）进水端相连，凝汽器（4）出水端与中间水池（5）进水端相连；乏汽进入凝汽器（4），冷凝水回流到锅炉（6）；第二水泵（9）进水端与中间水池（5）出水端相连，第二水泵（9）出水端与膜蒸馏装置（8）进水端相连，膜蒸馏装置（8）出水端与产水池（10）相连；或，中间水池（5）出水端与膜蒸馏装置（8）进水端相连，膜蒸馏装置（8）出水端与产水池（10）相连，第二水泵（9）进水端与膜蒸馏装置（8）出水端相连，第二水泵（9）出水端与调节池（2）进水端相连。还公开了一种间接空冷机组热回收及水处理方法。

Description

一种间接空冷机组热回收及水处理装置与方法 技术领域
本发明涉及节能环保技术领域，具体而言，涉及一种间接空冷机组热回收及水处理装置与方法。
背景技术
燃煤发电是我国主要的电力供给形式，在我国缺水地区，一些燃煤电厂采用空冷机组发电，空冷机组一般分为直接空冷机组和间接空冷机组。间接空冷分为海勒式和哈蒙式两种，其循环水系统都是闭式的。带表面式凝汽器的间接空冷系统——亦称哈蒙系统，由表面式凝汽器、空冷散热器、循环水泵以及充氮保护系统、循环水补充水系统、散热器清洗等系统与空冷塔构成。该系统与常规的湿冷系统基本相仿，不同之处是用空冷塔代替湿冷塔，用密闭式循环冷却水系统代替敞开式循环冷却水系统，循环水采用除盐水。表面式凝汽器间接空冷系统的工艺流程为：循环水进入表面式凝汽器的水侧通过表面换热，冷却凝汽器汽侧的汽轮机排汽，受热后的循环水由循环水泵送至空冷塔，通过空冷散热器与空气进行表面换热，循环水被空气冷却后再返回凝汽器去冷却汽轮机排汽，构成了密闭循环。因此，乏汽中大量热量通过空冷系统进入大气中，这不仅造成了能源浪费，同时还会引起大气污染问题，因此，如何回收利用乏汽中的热量，一直是节能领域重点研究领域。
膜蒸馏(MD)技术是一种高效的膜分离技术，是通过控制废水温度，以疏水性微孔膜为分离介质，以膜两侧蒸汽压差为传质推动力，实现废水浓缩和纯水回收的过程，MD技术与传统膜分离技术相比具有众多优点，如对盐的截留效率极高，对绝大多数非挥发性物质具有近100％截留效率，以及对进水水质要求低、操作条件温和(不需要高压设备)、运行维护方便、不容易发生膜污染和能耗比传统蒸发低等。此外，膜蒸馏对废水中含盐量变化适应性强，理论上只要溶质不饱和析出，膜组件都可以正常运行。由于膜蒸馏需要对原水进行加热，因此能耗相对较高，这也是限制MD工艺大规模应用的重要因素之一。
因此，为了减少甚至避免间接空冷机组中乏汽热量浪费，回收能源，将膜蒸馏技术与间接空冷机组冷却系统相结合，开发经济高效的热能回收和水处理工艺具有重要意义。
发明内容
为解决上述问题，本发明的目的在于提供一种间接空冷机组热回收及水处理装置与方法，将间接空冷机组乏汽冷凝与膜蒸馏工艺相结合，充分利用乏汽余热作为膜蒸馏系统的热源。
本发明提供了一种间接空冷机组热回收及水处理装置，包括预处理装置、调节池、第一水泵、凝汽器、中间水池、锅炉、膜蒸馏装置、第二水泵、产水池；
其中，
待处理的原水进入所述预处理装置的进水端，所述预处理装置的出水端与所述调节池的进水端相连，所述调节池的出水端通过所述第一水泵与所述凝汽器的进水端相连，所述凝汽器的出水端与所述中间水池的进水端相连；
乏汽进入所述凝汽器，所述凝汽器内冷凝后产生的冷凝水回流到所述锅炉；
所述第二水泵位于所述中间水池和所述膜蒸馏装置之间，所述第二水泵的进水端与所述中间水池的出水端相连，所述第二水泵的出水端与所述膜蒸馏装置的进水端相连，所述膜蒸馏装置的产水端与所述产水池相连；或，所述中间水池的出水端与所述膜蒸馏装置的进水端相连，所述膜蒸馏装置的产水端与所述产水池相连，所述第二水泵的进水端与所述膜蒸馏装置的出水端相连，所述第二水泵的出水端与所述调节池的进水端相连。
作为本发明进一步的改进，还包括辅助加热装置，待处理的原水进入所述预处理装置的进水端，所述预处理装置的出水端与所述调节池的进水端相连，所述调节池的出水端通过所述第一水泵与所述凝汽器的进水端相连，所述凝汽器的出水端与所述中间水池的进水端相连，所述中间水池的出水端与所述辅助加热装置的进水端相连；
乏汽进入所述凝汽器，所述凝汽器内冷凝后产生的冷凝水回流到所述锅炉中；
所述第一水泵位于所述辅助加热装置和所述膜蒸馏装置之间，所述第一水泵的进水端与所述辅助加热装置的出水端相连，所述第一水泵的出水端与所述膜蒸馏装置的进水端相连，所述膜蒸馏装置的产水端与所述产水池相连； 或，所述辅助加热装置的出水端与所述膜蒸馏装置的进水端相连，所述膜蒸馏装置的产水端与所述产水池相连，所述第一水泵的进水端所述膜蒸馏装置的出水端，所述第一水泵的出水端与所述调节池的进水端相连。
作为本发明进一步的改进，所述辅助加热装置为蒸汽加热装置或烟气加热装置或电加热装置。
作为本发明进一步的改进，所述调节池中设有搅拌装置。
作为本发明进一步的改进，所述预处理装置为沉淀池、隔油池、氧化池、软化池、过滤器和生化池中的一种或几种的组合。
作为本发明进一步的改进，所述膜蒸馏装置采用气隙式膜蒸馏装置、气扫式膜蒸馏装置、真空气隙式膜蒸馏装置和直接接触式膜蒸馏装置中的一种或几种的组合。
作为本发明进一步的改进，所述凝汽器中设有真空监测和控制系统，并与备用冷却水系统相连。
本发明还提供了一种间接空冷机组热回收及水处理方法，该方法包括以下步骤：
步骤1，待处理的原水经过所述预处理装置的预处理后，进入所述调节池中；
步骤2，所述调节池的出水经所述第一水泵进入所述凝汽器中，55℃～65℃的乏汽进入所述凝汽器，所述调节池的出水经换热后温度升高至40℃～55℃，然后进入所述中间水池，同时，所述凝汽器内冷凝后产生的冷凝水经过回热和除氧处理后回流到所述锅炉中；
步骤3，所述中间水池的出水在所述第二水泵的抽吸作用下被抽吸进入所述膜蒸馏装置进行膜蒸馏浓缩处理；或，所述中间水池的出水在所述第二水泵的压力作用下进入所述膜蒸馏装置进行膜蒸馏浓缩处理；
步骤4，所述膜蒸馏装置产生的浓水通过所述第二水泵的作用下回流至所述调节池中，并重复步骤2和步骤3；
步骤5，所述膜蒸馏装置产生的蒸馏水进入所述产水池，作为生产用水或生活用水。
作为本发明进一步的改进，步骤3替换为：
所述中间水池的出水进入所述辅助加热装置加热至70℃～95℃，所述辅助加热装置加热后的出水在所述第二水泵的抽吸作用下被抽吸进入所述膜蒸馏装置进行膜蒸馏浓缩处理；或，所述辅助加热装置加热后的出水在所述第二水泵的压力作用下进入所述膜蒸馏装置进行膜蒸馏浓缩处理。
作为本发明进一步的改进，步骤2之前还包括：开启所述调节池中的搅拌装置，保证所述调节池内的水质和水温均匀。
本发明的有益效果为：
1、将电厂乏汽为作为膜蒸馏系统的热源，充分利用乏汽余热，有效避免大部分热量进入大气而造成能源浪费，同时大幅降低膜蒸馏处理的运行成本，可以利用乏汽余热进行废水处理或生产高品质的水资源，提高整个电厂的热利用效率；
2、辅助加热系统的设置，可以有效提高该工艺的适应性和灵活性。
附图说明
图1为本发明第一实施例所述的一种间接空冷机组热回收及水处理装置的结构示意图；
图2为本发明第二实施例所述的一种间接空冷机组热回收及水处理装置的结构示意图。
图中，
1、预处理装置；2、调节池；3、第一水泵；4、凝汽器；5、中间水池；6、锅炉；7、辅助加热装置；8、膜蒸馏装置；9、第二水泵；10、产水池。
具体实施方式
下面通过具体的实施例并结合附图对本发明做进一步的详细描述。
实施例1，如图1所示，本发明第一实施例的一种间接空冷机组热回收及水处理装置，包括预处理装置1、调节池2、第一水泵3、凝汽器4、中间水池5、锅炉6、膜蒸馏装置8、第二水泵9、产水池10，调节池2中设有搅拌装置。待处理的原水进入预处理装置1的进水端，预处理装置1的出水端与调节池2的进水端相连，调节池2的出水端通过第一水泵3与凝汽器4的进水端相连，凝汽器4的出水端与中间水池5的进水端相连。乏汽进入凝汽器4， 凝汽器4内冷凝后产生的冷凝水回流到锅炉6。第二水泵9位于中间水池5和膜蒸馏装置8之间，第二水泵9的进水端与中间水池5的出水端相连，第二水泵9的出水端与膜蒸馏装置8的进水端相连，膜蒸馏装置8的产水端与产水池11相连；或，中间水池5的出水端与膜蒸馏装置8的进水端相连，膜蒸馏装置8的产水端与产水池11相连，第二水泵9的进水端与膜蒸馏装置8的出水端相连，第二水泵9的出水端与调节池2的进水端相连。
其中，预处理装置1为沉淀池、隔油池、氧化池、软化池、过滤器和生化池中的一种或几种的组合。
膜蒸馏装置8采用气隙式膜蒸馏装置、气扫式膜蒸馏装置、真空气隙式膜蒸馏装置和直接接触式膜蒸馏装置中的一种或几种的组合。
凝汽器4中设有真空监测和控制系统，并与备用冷却水系统相连。当由于系统运行故障或膜蒸馏系统维护等原因，造成凝汽器4内真空度不足时，通过凝汽器4内在线压力监测装置和自控系统，可自动开启备用冷却水系统，使电厂发电正常。
以电厂周边某河流苦咸水为淡化处理对象，利用该间接空冷机组热回收及水处理装置生产饮用水的方法包括以下步骤：
步骤1，河水经过预处理装置1的絮凝沉淀、软化、过滤、氧化等预处理后，去除废水中悬浮物、硬度和COD等污染物，以满足后续膜蒸馏进水要求，预处理后的海水进入调节池2中，开启调节池2中搅拌装置，以保证池内水质和水温均匀。
步骤2，调节池2的出水经第一水泵3进入凝汽器4中，60℃的乏汽进入凝汽器4，河水经换热后温度升高至52℃，然后进入中间水池5，同时，凝汽器4内冷凝后产生的冷凝水经过回热和除氧处理后回流到锅炉6中。
步骤3，中间水池5的出水在第二水泵9的抽吸作用下被抽吸进入膜蒸馏装置8进行膜蒸馏浓缩处理；或，中间水池5的出水在第二水泵9的压力作用下进入膜蒸馏装置8进行膜蒸馏浓缩处理。
步骤4，膜蒸馏装置8产生的浓水通过第二水泵9的作用下回流至调节池2中，并重复步骤2和步骤3。
步骤5，膜蒸馏装置8产生的蒸馏水进入产水池10，作为生产用水或生活用水。
采用抽吸的进水方式，有利于降低膜组件内的海水压力，避免疏水膜发生穿透，同时，可以在同等操作条件下增大膜两侧蒸汽压差，有利于提高膜的产水通量。
本实施例中由于电厂厂内空地充足，有足够空间用于建设膜蒸馏系统，为了不影响主机发电效率，因此取消辅助加热装置的设置。当膜蒸馏装置8产生的浓水含盐量达到20％时，浓水排出系统进一步处理。
当由于系统运行故障或膜蒸馏系统维护等原因，造成凝汽器4内真空度不足时，通过凝汽器4内在线压力监测装置和自控系统，自动开启备用冷却水系统，保证电厂发电正常。
实施例2，如图2所示，本发明第二实施例的一种间接空冷机组热回收及水处理装置，与实施例1不同之处在于，还包括辅助加热装置7，待处理的原水进入预处理装置1的进水端，预处理装置1的出水端与调节池2的进水端相连，调节池2的出水端通过第一水泵3与凝汽器4的进水端相连，凝汽器4的出水端与中间水池5的进水端相连，中间水池5的出水端与辅助加热装置7的进水端相连。乏汽进入凝汽器4，凝汽器4内冷凝后产生的冷凝水回流到锅炉6中。第一水泵9位于辅助加热装置7和膜蒸馏装置8之间，第一水泵9的进水端与辅助加热装置7的出水端相连，第一水泵9的出水端与膜蒸馏装置8的进水端相连，膜蒸馏装置8的产水端与产水池11相连；或，辅助加热装置7的出水端与膜蒸馏装置8的进水端相连，膜蒸馏装置8的产水端与产水池11相连，第一水泵9的进水端膜蒸馏装置8的出水端，第一水泵9的出水端与调节池2的进水端相连。
其中，辅助加热装置7为蒸汽加热装置或烟气加热装置或电加热装置。
同样以电厂周边某河流苦咸水为淡化处理对象，利用该间接空冷机组热回收及水处理装置生产饮用水的方法包括以下步骤：
步骤1，河水经过预处理装置1的絮凝沉淀、软化、过滤、氧化等预处理后，去除废水中悬浮物、硬度和COD等污染物，以满足后续膜蒸馏进水要求， 预处理后的海水进入调节池2中，开启调节池2中搅拌装置，以保证池内水质和水温均匀。
步骤2，调节池2的出水经第一水泵3进入凝汽器4中，60℃的乏汽进入凝汽器4，河水经换热后温度升高至52℃，然后进入中间水池5，同时，凝汽器4内冷凝后产生的冷凝水经过回热和除氧处理后回流到锅炉6中。
步骤3，为了实现较高的膜蒸馏产水通量，中间水池5的出水进入辅助加热装置，通过高温蒸汽将河水温度加热至80℃，加热后的河水在第二水泵9的抽吸作用下被抽吸进入膜蒸馏装置8进行膜蒸馏浓缩处理；或，加热后的河水在第二水泵9的压力作用下进入膜蒸馏装置8进行膜蒸馏浓缩处理。
步骤4，膜蒸馏装置8处理后，产生的浓水温度降至约42℃，同时通过第二水泵9的作用下回流至调节池2中，并重复步骤2和步骤3。
步骤5，膜蒸馏装置8产生的蒸馏水进入产水池10，作为生产用水或生活用水。
采用抽吸的进水方式，有利于降低膜组件内的海水压力，避免疏水膜发生穿透，同时，可以在同等操作条件下增大膜两侧蒸汽压差，有利于提高膜的产水通量。
本实施例中由于布置紧凑，可建设用地面积有限，为了减少膜蒸馏系统占地面积，需要尽可能提高膜蒸馏系统的单位膜面积产水通量，以便减少膜组件用量，最终节约站点面积，因此需控制膜蒸馏进水处于较高温度，增加辅助加热装置。当膜蒸馏装置8产生的浓水含盐量达到18％以上时，浓水排出系统进一步处理。
实施例3，与实施例1不同之处在于，以海水为处理对象，利用该间接空冷机组热回收及水处理装置进行海水淡化处理的方法包括以下步骤：
步骤1，海水经过预处理装置1的软化、絮凝沉淀、过滤等预处理后，去除废水中的悬浮物和硬度等污染物，以满足后续膜蒸馏进水要求，预处理后的海水进入调节池2中，开启调节池2中搅拌装置，以保证池内水质和水温均匀。
步骤2，调节池2的出水经第一水泵3进入凝汽器4中，63℃的乏汽进入 凝汽器4，河水经换热后温度升高至50℃，然后进入中间水池5，同时，凝汽器4内冷凝后产生的冷凝水经过回热和除氧处理后回流到锅炉6中。
步骤3，中间水池5的出水在第二水泵9的抽吸作用下被抽吸进入膜蒸馏装置8进行膜蒸馏浓缩处理；或，中间水池5的出水在第二水泵9的压力作用下进入膜蒸馏装置8进行膜蒸馏浓缩处理。
步骤4，膜蒸馏装置8产生的浓水通过第二水泵9的作用下回流至调节池2中，并重复步骤2和步骤3。
步骤5，膜蒸馏装置8产生的蒸馏水进入产水池10，作为生产用水或生活用水。
采用抽吸的进水方式，有利于降低膜组件内的海水压力，避免疏水膜发生穿透，同时，可以在同等操作条件下增大膜两侧蒸汽压差，有利于提高膜的产水通量。
实施例4，与实施例2不同之处在于，以海水为处理对象，利用该间接空冷机组热回收及水处理装置进行海水淡化处理的方法包括以下步骤：
步骤1，海水经过预处理装置1的软化、絮凝沉淀、过滤等预处理后，去除废水中的悬浮物和硬度等污染物，以满足后续膜蒸馏进水要求，预处理后的海水进入调节池2中，开启调节池2中搅拌装置，以保证池内水质和水温均匀。
步骤2，调节池2的出水经第一水泵3进入凝汽器4中，63℃的乏汽进入凝汽器4，河水经换热后温度升高至50℃，然后进入中间水池5，同时，凝汽器4内冷凝后产生的冷凝水经过回热和除氧处理后回流到锅炉6中。
步骤3，为了实现较高的膜蒸馏产水通量，中间水池5的出水进入辅助加热装置，通过高温蒸汽将河水温度加热至70℃，加热后的河水在第二水泵9的抽吸作用下被抽吸进入膜蒸馏装置8进行膜蒸馏浓缩处理；或，加热后的河水在第二水泵9的压力作用下进入膜蒸馏装置8进行膜蒸馏浓缩处理。
步骤4，膜蒸馏装置8处理后，产生的浓水温度降至约40℃，同时通过第二水泵9的作用下回流至调节池2中，并重复步骤2和步骤3。
步骤5，膜蒸馏装置8产生的蒸馏水进入产水池10，作为生产用水或生活用水。
采用抽吸的进水方式，有利于降低膜组件内的海水压力，避免疏水膜发生穿透，同时，可以在同等操作条件下增大膜两侧蒸汽压差，有利于提高膜的产水通量。
本发明针对直接空冷机组发电厂中，空冷系统能耗大和热量损失严重的缺点，将间接空冷机组乏汽冷凝与膜蒸馏工艺相结合，通过膜蒸馏系统取代直接空冷系统，利用乏汽余热作为膜蒸馏系统的热源，待处理水溶液取代空冷机组的冷却水循环，在凝汽器内将乏汽冷凝，同时实现自身加热过程，待处理水溶液经过加热后进入膜蒸馏系统，完成制水过程和待处理水溶液的降温过程，适用于处理废水和海水淡化等纯水生产或溶液脱盐处理。其中的预处理过程可以为化学沉底、化学氧化、生物处理、过滤和吸附中的一种或几种。其中，用于处理的原水为电厂废水或生活污水或海水或地表水或地下水。
以上所述仅为本发明的优选实施例而已，并不用于限制本发明，对于本领域的技术人员来说，本发明可以有各种更改和变化。凡在本发明的精神和原则之内，所作的任何修改、等同替换、改进等，均应包含在本发明的保护范围之内。

Claims (10)

  1. 一种间接空冷机组热回收及水处理装置，其特征在于，包括预处理装置(1)、调节池(2)、第一水泵(3)、凝汽器(4)、中间水池(5)、锅炉(6)、膜蒸馏装置(8)、第二水泵(9)、产水池(10)；
    其中，
    待处理的原水进入所述预处理装置(1)的进水端，所述预处理装置(1)的出水端与所述调节池(2)的进水端相连，所述调节池(2)的出水端通过所述第一水泵(3)与所述凝汽器(4)的进水端相连，所述凝汽器(4)的出水端与所述中间水池(5)的进水端相连；
    乏汽进入所述凝汽器(4)，所述凝汽器(4)内冷凝后产生的冷凝水回流到所述锅炉(6)；
    所述第二水泵(9)位于所述中间水池(5)和所述膜蒸馏装置(8)之间，所述第二水泵(9)的进水端与所述中间水池(5)的出水端相连，所述第二水泵(9)的出水端与所述膜蒸馏装置(8)的进水端相连，所述膜蒸馏装置(8)的产水端与所述产水池(11)相连；或，所述中间水池(5)的出水端与所述膜蒸馏装置(8)的进水端相连，所述膜蒸馏装置(8)的产水端与所述产水池(11)相连，所述第二水泵(9)的进水端与所述膜蒸馏装置(8)的出水端相连，所述第二水泵(9)的出水端与所述调节池(2)的进水端相连。
  2. 根据权利要求1所述的间接空冷机组热回收及水处理装置，其特征在于，还包括辅助加热装置(7)，待处理的原水进入所述预处理装置(1)的进水端，所述预处理装置(1)的出水端与所述调节池(2)的进水端相连，所述调节池(2)的出水端通过所述第一水泵(3)与所述凝汽器(4)的进水端相连，所述凝汽器(4)的出水端与所述中间水池(5)的进水端相连，所述中间水池(5)的出水端与所述辅助加热装置(7)的进水端相连；
    乏汽进入所述凝汽器(4)，所述凝汽器(4)内冷凝后产生的冷凝水回流到所述锅炉(6)中；
    所述第一水泵(9)位于所述辅助加热装置(7)和所述膜蒸馏装置(8)之间，所述第一水泵(9)的进水端与所述辅助加热装置(7)的出水端相连， 所述第一水泵(9)的出水端与所述膜蒸馏装置(8)的进水端相连，所述膜蒸馏装置(8)的产水端与所述产水池(11)相连；或，所述辅助加热装置(7)的出水端与所述膜蒸馏装置(8)的进水端相连，所述膜蒸馏装置(8)的产水端与所述产水池(11)相连，所述第一水泵(9)的进水端所述膜蒸馏装置(8)的出水端，所述第一水泵(9)的出水端与所述调节池(2)的进水端相连。
  3. 根据权利要求2所述的间接空冷机组热回收及水处理装置，其特征在于，所述辅助加热装置(7)为蒸汽加热装置或烟气加热装置或电加热装置。
  4. 根据权利要求1所述的间接空冷机组热回收及水处理装置，其特征在于，所述调节池(2)中设有搅拌装置。
  5. 根据权利要求1或2所述的间接空冷机组热回收及水处理装置，其特征在于，所述预处理装置(1)为沉淀池、隔油池、氧化池、软化池、过滤器和生化池中的一种或几种的组合。
  6. 根据权利要求1或2所述的间接空冷机组热回收及水处理装置，其特征在于，所述膜蒸馏装置(8)采用气隙式膜蒸馏装置、气扫式膜蒸馏装置、真空气隙式膜蒸馏装置和直接接触式膜蒸馏装置中的一种或几种的组合。
  7. 根据权利要求1或2所述的间接空冷机组热回收及水处理装置，其特征在于，所述凝汽器(4)中设有真空监测和控制系统，并与备用冷却水系统相连。
  8. 一种利用权利要求1所述的一种间接空冷机组热回收及水处理装置的热回收及水处理方法，其特征在于，该方法包括以下步骤：
    步骤1，待处理的原水经过所述预处理装置(1)的预处理后，进入所述调节池(2)中，其中，预处理为化学沉底、化学氧化、生物处理、过滤和吸附中的一种或几种；
    步骤2，所述调节池(2)的出水经所述第一水泵(3)进入所述凝汽器(4)中，55℃～65℃的乏汽进入所述凝汽器(4)，所述调节池(2)的出水经换热后温度升高至40℃～55℃，然后进入所述中间水池(5)，同时，所述凝汽器(4)内冷凝后产生的冷凝水经过回热和除氧处理后回流到所述锅炉(6)中；
    步骤3，所述中间水池(5)的出水在所述第二水泵(9)的抽吸作用下被抽吸进入所述膜蒸馏装置(8)进行膜蒸馏浓缩处理；或，所述中间水池(5)的出水在所述第二水泵(9)的压力作用下进入所述膜蒸馏装置(8)进行膜蒸馏浓缩处理；
    步骤4，所述膜蒸馏装置(8)产生的浓水通过所述第二水泵(9)的作用下回流至所述调节池(2)中，并重复步骤2和步骤3；
    步骤5，所述膜蒸馏装置(8)产生的蒸馏水进入所述产水池(10)，作为生产用水或生活用水。
  9. 根据权利要求8所述的热回收及水处理方法，其特征在于，步骤3替换为：
    所述中间水池(5)的出水进入所述辅助加热装置(7)加热至70℃～95℃，所述辅助加热装置(7)加热后的出水在所述第二水泵(9)的抽吸作用下被抽吸进入所述膜蒸馏装置(8)进行膜蒸馏浓缩处理；或，所述辅助加热装置(7)加热后的出水在所述第二水泵(9)的压力作用下进入所述膜蒸馏装置(8)进行膜蒸馏浓缩处理。
  10. 根据权利要求8或9所述的热回收及水处理方法，其特征在于，步骤2之前还包括：开启所述调节池(2)中的搅拌装置，保证所述调节池(2)内的水质和水温均匀。
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