CN113694553B - A kind of printing and dyeing light lye absorption heat pump multi-effect distillation system and its working method - Google Patents

A kind of printing and dyeing light lye absorption heat pump multi-effect distillation system and its working method Download PDF

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CN113694553B
CN113694553B CN202110948187.8A CN202110948187A CN113694553B CN 113694553 B CN113694553 B CN 113694553B CN 202110948187 A CN202110948187 A CN 202110948187A CN 113694553 B CN113694553 B CN 113694553B
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evaporator
outlet
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inlet
preheater
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沈九兵
谭牛高
骆礼梅
周子晗
王炳东
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Jiangsu University of Science and Technology
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/14—Fractional distillation or use of a fractionation or rectification column
    • B01D3/143—Fractional distillation or use of a fractionation or rectification column by two or more of a fractionation, separation or rectification step
    • B01D3/146—Multiple effect distillation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/14—Fractional distillation or use of a fractionation or rectification column
    • B01D3/32—Other features of fractionating columns ; Constructional details of fractionating columns not provided for in groups B01D3/16 - B01D3/30
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B15/00—Sorption machines, plants or systems, operating continuously, e.g. absorption type
    • F25B15/02—Sorption machines, plants or systems, operating continuously, e.g. absorption type without inert gas
    • F25B15/06—Sorption machines, plants or systems, operating continuously, e.g. absorption type without inert gas the refrigerant being water vapour evaporated from a salt solution, e.g. lithium bromide
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    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02B—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO BUILDINGS, e.g. HOUSING, HOUSE APPLIANCES OR RELATED END-USER APPLICATIONS
    • Y02B30/00—Energy efficient heating, ventilation or air conditioning [HVAC]
    • Y02B30/52—Heat recovery pumps, i.e. heat pump based systems or units able to transfer the thermal energy from one area of the premises or part of the facilities to a different one, improving the overall efficiency
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P70/00—Climate change mitigation technologies in the production process for final industrial or consumer products
    • Y02P70/10—Greenhouse gas [GHG] capture, material saving, heat recovery or other energy efficient measures, e.g. motor control, characterised by manufacturing processes, e.g. for rolling metal or metal working

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Abstract

本发明公开了一种印染淡碱液吸收式热泵多效蒸馏系统及其工作方法，所述系统包括第二类溴化锂吸收式热泵系统和多效蒸馏系统。所述方法是：利用中温废水余热驱动吸收式热泵，并由吸收式热泵的蒸发器回收多效蒸馏系统末效蒸汽的冷凝热，通过吸收器出来的高温溴化锂溶液使冷凝水再蒸发得到高温蒸汽驱动多效蒸馏系统。通过设置储能器，可在无水处理需求时将吸收式热泵回收的热能蓄存，再在无中温废水时放热驱动多效蒸馏系统，实现错峰使用。本发明回收中温废水的热量，既能极大限度地降低印染淡碱蒸发过程的能耗，又能有效降低废水排放到环境中造成的能量浪费和环境影响。

Figure 202110948187

The invention discloses a printing and dyeing light alkali liquor absorption heat pump multi-effect distillation system and a working method thereof. The system comprises a second-type lithium bromide absorption heat pump system and a multi-effect distillation system. The method is as follows: using the waste heat of medium-temperature waste water to drive the absorption heat pump, recovering the condensation heat of the end effect steam of the multi-effect distillation system by the evaporator of the absorption heat pump, and re-evaporating the condensed water through the high-temperature lithium bromide solution from the absorber to obtain the high-temperature steam Drives a multi-effect distillation system. By setting the accumulator, the heat energy recovered by the absorption heat pump can be stored when there is no need for water treatment, and then the multi-effect distillation system can be driven by exothermic heat when there is no intermediate-temperature wastewater, so as to realize off-peak use. The invention recovers the heat of the medium-temperature wastewater, which can not only greatly reduce the energy consumption of the light alkali evaporation process of printing and dyeing, but also effectively reduce the energy waste and environmental impact caused by the discharge of the wastewater into the environment.

Figure 202110948187

Description

一种印染淡碱液吸收式热泵多效蒸馏系统及其工作方法A kind of printing and dyeing light lye absorption heat pump multi-effect distillation system and its working method

技术领域technical field

本发明涉及一种印染淡碱液吸收式热泵多效蒸馏系统及其工作方法，尤其涉及利用第二类吸收式热泵系统回收中温废水余热，用来驱动二效蒸馏系统对淡碱液进行蒸馏浓缩。The invention relates to an absorption heat pump multi-effect distillation system for printing and dyeing light lye and a working method thereof, in particular to the use of a second type of absorption heat pump system to recover the waste heat of medium-temperature wastewater, which is used to drive a two-effect distillation system to distill and concentrate light lye .

背景技术Background technique

我国是纺织印染工业的第一大国，纺织印染行业是废水排放大户，约占整个工业废水排放量的35％，印染废水排放量约为每天3×106m3～4×106m3。印染工业不同工艺流程用水温度不一样，退浆工艺用水温度98℃，废水排放温度95℃，清洗工艺用水温度80℃～90℃，废水排放温度75℃～85℃，这些中温废水含有大量的余热。能源在被利用的过程中，有很大一部分没有被有效利用，而这部分没有被利用的能量往往以热的形式释放到大气或水体中，对环境造成了热污染。充分利用印染工业废水的余热，是减少印染行业热污染的最主要措施。印染工业中染色工艺淡碱液的回收和利用，历来是印染行业和环境保护的一个重要科技攻关课题，常规的方法是将淡碱液加热浓缩回用。传统单效蒸馏的浓缩方法，蒸汽消耗量大，设备投资成本大，经济性较差。China is the largest country in the textile printing and dyeing industry. The textile printing and dyeing industry is a large waste water discharger, accounting for about 35% of the entire industrial waste water discharge. The temperature of water in different processes in the printing and dyeing industry is different. The temperature of water in desizing process is 98°C, the temperature of waste water discharge is 95°C, the temperature of water in cleaning process is 80°C to 90°C, and the temperature of waste water discharge is 75°C to 85°C. These medium-temperature waste water contains a lot of waste heat. . In the process of energy utilization, a large part of the energy is not used effectively, and this part of the unused energy is often released into the atmosphere or water in the form of heat, causing thermal pollution to the environment. Making full use of the waste heat of the printing and dyeing industry wastewater is the most important measure to reduce thermal pollution in the printing and dyeing industry. The recovery and utilization of the light lye in the dyeing process in the printing and dyeing industry has always been an important scientific and technological research topic in the printing and dyeing industry and environmental protection. The conventional method is to heat and concentrate the light lye for reuse. The traditional single-effect distillation concentration method has large steam consumption, large equipment investment cost and poor economy.

发明内容SUMMARY OF THE INVENTION

本发明是针对上述问题，提出一种印染淡碱液吸收式热泵多效蒸馏系统。In view of the above problems, the present invention proposes a printing and dyeing light lye absorption heat pump multi-effect distillation system.

为实现本发明的目的，本发明采用的技术方案是：For realizing the purpose of the present invention, the technical scheme adopted in the present invention is:

一种印染淡碱液吸收式热泵多效蒸馏系统，包括多效蒸馏循环系统和吸收式热泵循环系统，所述多效蒸馏循环系统包括：第一离心泵101、第一预热器102、第二预热器103、第三预热器104、第一蒸发器105和第二蒸发器106，印染淡碱液通过管路连通第一离心泵101入口，第一离心泵101出口通过管路连接第一预热器102入口a1，第一预热器102出口a2通过管路连接第二预热器103入口b1，第二预热器103出口b2通过管路连接第三预热器104入口c1，第三预热器104出口c2通过管路连接第一蒸发器105的溶液入口d1，所述第一蒸发器105溶液出口d2通过管路经第一减压阀107接至第二蒸发器106溶液入口e1，第一蒸发器105的凝结水d4出口通过管路接至第三预热器104入口c3，第一蒸发器105蒸汽出口d5 通过管路接至第二蒸发器106的蒸汽入口e3；第二蒸发器106溶液出口e2通过管路接至第一预热器102入口a3，第二蒸发器106的凝结水出口e4通过管路接至第二预热器103入口b3；A printing and dyeing light lye absorption heat pump multi-effect distillation system, including a multi-effect distillation cycle system and an absorption heat pump cycle system, the multi-effect distillation cycle system includes: a first centrifugal pump 101, a first preheater 102, a first The second preheater 103, the third preheater 104, the first evaporator 105 and the second evaporator 106, the printing and dyeing light lye is connected to the inlet of the first centrifugal pump 101 through pipelines, and the outlet of the first centrifugal pump 101 is connected through pipelines The inlet a1 of the first preheater 102, the outlet a2 of the first preheater 102 are connected to the inlet b1 of the second preheater 103 through a pipeline, and the outlet b2 of the second preheater 103 is connected to the inlet c1 of the third preheater 104 through a pipeline , the outlet c2 of the third preheater 104 is connected to the solution inlet d1 of the first evaporator 105 through a pipeline, and the solution outlet d2 of the first evaporator 105 is connected to the second evaporator 106 through a pipeline through the first pressure reducing valve 107 The solution inlet e1, the condensed water d4 outlet of the first evaporator 105 is connected to the inlet c3 of the third preheater 104 through a pipeline, and the steam outlet d5 of the first evaporator 105 is connected to the steam inlet e3 of the second evaporator 106 through a pipeline ; The solution outlet e2 of the second evaporator 106 is connected to the inlet a3 of the first preheater 102 through a pipeline, and the condensed water outlet e4 of the second evaporator 106 is connected to the inlet b3 of the second preheater 103 through a pipeline;

所述吸收式热泵循环系统包括：发生器201、冷凝器202、第二离心泵203、第三蒸发器 204、第四蒸发器205、吸收器206、第五蒸发器207、储能器208、第四预热器209和第三离心泵210；中温废水通过管路连接发生器201入口o1，发生器201出口o2通过管路接至第一蒸发器204的入口j4，第一蒸发器204的出口j3接排放管路，所述发生器201的蒸汽出口o4 通过管路连接冷凝器202入口k1，冷凝器202出口k2通过管路经第二离心泵203接至第一蒸发器204入口j6，第一蒸发器204的出口j5通过管路接至第二蒸发器205的入口f5，第二蒸发器205的出口f6通过管路连接至吸收器206的蒸汽入口m2；所述发生器201的浓溴化锂溶液出口o5通过管路经第三离心泵210连接至第四预热器209入口i4，第四预热器209出口i3通过管路连接至吸收器206的浓溶液入口m1；所述吸收器206的溴化锂稀溶液出口m3 通过管路连接至第三蒸发器207的入口h3，第三蒸发器207的出口h4通过管路连接至储能器208的蓄热管路入口n1，储能器208的出口n2通过管路接至第四预热器209的入口i1，第四蒸发器209的出口i2通过管路经第二减压阀211接至发生器201的溴化锂稀溶液入口o3；The absorption heat pump circulation system includes: a generator 201, a condenser 202, a second centrifugal pump 203, a third evaporator 204, a fourth evaporator 205, an absorber 206, a fifth evaporator 207, an accumulator 208, The fourth preheater 209 and the third centrifugal pump 210; the medium temperature wastewater is connected to the inlet o1 of the generator 201 through a pipeline, and the outlet o2 of the generator 201 is connected to the inlet j4 of the first evaporator 204 through a pipeline. The outlet j3 is connected to the discharge pipeline, the steam outlet o4 of the generator 201 is connected to the inlet k1 of the condenser 202 through the pipeline, and the outlet k2 of the condenser 202 is connected to the inlet j6 of the first evaporator 204 through the pipeline through the second centrifugal pump 203, The outlet j5 of the first evaporator 204 is connected to the inlet f5 of the second evaporator 205 through a pipeline, and the outlet f6 of the second evaporator 205 is connected to the steam inlet m2 of the absorber 206 through a pipeline; The lithium bromide solution outlet o5 is connected to the inlet i4 of the fourth preheater 209 through a pipeline through the third centrifugal pump 210, and the outlet i3 of the fourth preheater 209 is connected to the concentrated solution inlet m1 of the absorber 206 through a pipeline; the absorber The lithium bromide dilute solution outlet m3 of 206 is connected to the inlet h3 of the third evaporator 207 through a pipeline, and the outlet h4 of the third evaporator 207 is connected to the heat storage pipeline inlet n1 of the accumulator 208 through a pipeline. The outlet n2 is connected to the inlet i1 of the fourth preheater 209 through the pipeline, and the outlet i2 of the fourth evaporator 209 is connected to the inlet o3 of the dilute lithium bromide solution of the generator 201 through the second pressure reducing valve 211;

所述第二蒸发器106顶部二次蒸汽出口e5通过管路连接至第四蒸发器205入口f1，第四蒸发器205出口f2通过管路连接至第四离心泵301入口，所述第四离心泵301出口通过管路经第一截止阀303接至第五蒸发器207的入口h1，第五蒸发器207的出口h2通过管路经第二截止阀304连接至气液分离器302入口g1，所述气液分离器302蒸汽出口g2通过管路连接至第一蒸发器105的蒸汽入口d3，所述气液分离器302的水出口g3通过管路经第三截止阀305连接至第四离心泵301的入口管路；The secondary steam outlet e5 at the top of the second evaporator 106 is connected to the inlet f1 of the fourth evaporator 205 through a pipeline, and the outlet f2 of the fourth evaporator 205 is connected to the inlet of the fourth centrifugal pump 301 through a pipeline. The outlet of the pump 301 is connected to the inlet h1 of the fifth evaporator 207 through the first stop valve 303 through the pipeline, and the outlet h2 of the fifth evaporator 207 is connected to the inlet g1 of the gas-liquid separator 302 through the pipeline through the second stop valve 304. The steam outlet g2 of the gas-liquid separator 302 is connected to the steam inlet d3 of the first evaporator 105 through a pipeline, and the water outlet g3 of the gas-liquid separator 302 is connected to the fourth centrifugal pump through a pipeline through the third stop valve 305 the inlet line of the pump 301;

系统补给水通过管路依次经电动调节阀401和第五离心泵402连接至第三蒸发器204的入口j1，第三蒸发器204的出口j2通过管路连接至第二蒸发器205的入口f3，第二蒸发器205 的出口f4通过管路连接至第四离心泵301的入口管路；The system make-up water is connected to the inlet j1 of the third evaporator 204 through the electric regulating valve 401 and the fifth centrifugal pump 402 in sequence through the pipeline, and the outlet j2 of the third evaporator 204 is connected to the inlet f3 of the second evaporator 205 through the pipeline. , the outlet f4 of the second evaporator 205 is connected to the inlet pipeline of the fourth centrifugal pump 301 through a pipeline;

进一步，所述第四离心泵301出口还通过管路经第四截止阀306连接至储能器208的入口n3，所述储能器208的出口n4通过管路经第五截止阀307连接至气液分离器302的入口 g1；Further, the outlet of the fourth centrifugal pump 301 is also connected to the inlet n3 of the accumulator 208 through the fourth stop valve 306 through the pipeline, and the outlet n4 of the accumulator 208 is connected to the inlet n4 of the accumulator 208 through the pipeline through the fifth stop valve 307 the inlet g1 of the gas-liquid separator 302;

进一步，所述气液分离器302内设有液位控制器308，所述气液分离器302出口管路上设置有温度控制器309，所述液位控制器308和温度控制器309通过信号线连接电动调节阀 401；Further, the gas-liquid separator 302 is provided with a liquid level controller 308, the outlet pipeline of the gas-liquid separator 302 is provided with a temperature controller 309, and the liquid level controller 308 and the temperature controller 309 pass through a signal line Connect the electric regulating valve 401;

进一步，所述储能器208使用的储能相变材料为Mg(NO3)2 ·2H2O或NaNO3─LiNO3/石墨复合储能材料；Further, the energy storage phase change material used in the energy storage device 208 is Mg(NO 3 ) 2 ·2H 2 O or NaNO 3 ─LiNO 3 /graphite composite energy storage material;

进一步，所述多效蒸馏循环系统根据淡碱液浓度设置为二效蒸馏循环系统、三效蒸馏循环系统或四效蒸馏循环系统；Further, the multi-effect distillation circulating system is set as a two-effect distillation circulating system, a three-effect distillation circulating system or a four-effect distillation circulating system according to the concentration of the light lye;

进一步，所述第一预热器102还设置有浓溶液出口a4；所述第二预热器103还设置有冷凝水出口b4；所述第三预热器104还设置有冷凝水出口c4；所述冷凝器202还设置有冷却水出口k3和低温冷却水入口k4；Further, the first preheater 102 is further provided with a concentrated solution outlet a4; the second preheater 103 is further provided with a condensed water outlet b4; the third preheater 104 is further provided with a condensed water outlet c4; The condenser 202 is also provided with a cooling water outlet k3 and a low temperature cooling water inlet k4;

本发明的一种印染淡碱液吸收式热泵多效蒸馏系统的工作方法，包括联合运行模式、储能模式和蒸馏处理模式；The working method of a printing and dyeing light lye absorption heat pump multi-effect distillation system of the present invention includes a combined operation mode, an energy storage mode and a distillation treatment mode;

一、联合运行模式：1. Joint operation mode:

当印染厂存在中温废水且需要处理淡碱液时，则启动联合运行模式，具体方法步骤是：打开第一截止阀303、第二截止阀304、第三截止阀305和电动调节阀401，关闭第四截止阀 306、第五截止阀307，淡碱稀溶液进入第一离心泵101内加压，再依次经过第一预热器102、第二预热器103和第三预热器104预热后进入第一蒸发器105内，第一蒸发器105内的淡碱稀溶液被加热后产生的蒸汽由第一蒸发器105顶部出口d5流入第二蒸发器106内，淡碱溶液由第一蒸发器105出口d2流出，经第一减压阀107降压后继续进入第二蒸发器106进行热交换，冷凝水由第一蒸发器105出口d4流入第三预热器104内换热；第二蒸发器106内的淡碱浓溶液由第二蒸发器106出口e2进口流入第一预热器102内换热，冷凝水由第二蒸发器106出口e4流入第二预热器103内换热，二次蒸汽由第二蒸发器106出口e5流入第四蒸发器205内换热，液化后的凝结水进入第二离心泵301内升压，然后进入第五蒸发器207内吸热汽化为饱和蒸汽，通过第二截止阀304进入气液分离器302，水蒸气由气液分离器302出口g2流入第一蒸发器105内继续下一循环；重新升温后的二次蒸汽不能满足二效蒸馏循环系统的运行，需要对蒸汽进行补充，补充水经过电动调节阀401进入第五离心泵402，升压后依次经第三蒸发器204和第四蒸发器205进行预热，与第四蒸发器205出口f2流出的冷凝水混合，进入第二离心泵301内加压。When the printing and dyeing factory has medium-temperature wastewater and needs to treat light lye, the joint operation mode is started. The specific method steps are: open the first stop valve 303, the second stop valve 304, the third stop valve 305 and the electric regulating valve 401, close the The fourth cut-off valve 306 and the fifth cut-off valve 307, the diluted alkaline solution enters the first centrifugal pump 101 to be pressurized, and then passes through the first preheater 102, the second preheater 103 and the third preheater 104 for preheating. After being heated, it enters the first evaporator 105, and the steam generated after the light alkali dilute solution in the first evaporator 105 is heated flows into the second evaporator 106 from the top outlet d5 of the first evaporator 105, and the light alkali solution flows from the first evaporator 105 to the second evaporator 106. The outlet d2 of the evaporator 105 flows out, and after being depressurized by the first pressure reducing valve 107, it continues to enter the second evaporator 106 for heat exchange, and the condensed water flows into the third preheater 104 from the outlet d4 of the first evaporator 105 for heat exchange; The light alkali concentrated solution in the second evaporator 106 flows into the first preheater 102 through the inlet e2 of the second evaporator 106 for heat exchange, and the condensed water flows into the second preheater 103 from the outlet e4 of the second evaporator 106 for heat exchange , the secondary steam flows from the outlet e5 of the second evaporator 106 into the fourth evaporator 205 for heat exchange, the liquefied condensed water enters the second centrifugal pump 301 to boost pressure, and then enters the fifth evaporator 207 to absorb heat and vaporize to saturation The steam enters the gas-liquid separator 302 through the second shut-off valve 304, and the water vapor flows into the first evaporator 105 from the outlet g2 of the gas-liquid separator 302 to continue the next cycle; the reheated secondary steam cannot meet the two-effect distillation cycle The operation of the system needs to supplement the steam. The supplementary water enters the fifth centrifugal pump 402 through the electric regulating valve 401. After boosting, it is preheated by the third evaporator 204 and the fourth evaporator 205 in turn. The condensed water flowing out of the outlet f2 is mixed and enters the second centrifugal pump 301 to be pressurized.

中温废水进入发生器201内换热，然后进入第三蒸发器204内继续换热，然后由第三蒸发器204出口j3排出；发生器201内的稀溴化锂溶液被加热，产生低压工质水蒸汽，水蒸汽由发生器201出口o4流入冷凝器202内，与低温冷却水换热后冷凝成饱和水，饱和水经过第四离心泵203升压后进入第三蒸发器204与中温废水换热，然后进入第四蒸发器205与二次蒸汽换热，温度升高后进入吸收器206内进行热质交换；浓溴化锂溶液由发生器201出口o5 流入第三离心泵210内升压，然后进入第四预热器209内换热，温度升高后进入吸收器206 内进行热质交换；在吸收器206内，高压工质蒸汽被浓溶液吸收产生大量的吸收热，使得吸收器206内的溴化锂溶液温度急剧增高；升温后的稀溴化锂溶液进入第五蒸发器207进行热交换，温度降低后的稀溴化锂溶液进入储能器208与储能相变材料换热，随后稀溴化锂溶液进入第四预热器209内换热，最后稀溴化锂溶液经过第二减压阀211降压后进入发生器201 内进行下一步循环。The medium-temperature wastewater enters the generator 201 for heat exchange, then enters the third evaporator 204 to continue heat exchange, and is then discharged from the outlet j3 of the third evaporator 204; the dilute lithium bromide solution in the generator 201 is heated to generate low-pressure working medium water vapor , the water vapor flows into the condenser 202 from the outlet o4 of the generator 201, and is condensed into saturated water after exchanging heat with the low-temperature cooling water. Then it enters the fourth evaporator 205 to exchange heat with the secondary steam, and after the temperature rises, it enters the absorber 206 for heat and mass exchange; the concentrated lithium bromide solution flows into the third centrifugal pump 210 from the outlet o5 of the generator 201 for boosting, and then enters the first The four preheaters 209 exchange heat, and after the temperature rises, they enter the absorber 206 for heat and mass exchange; in the absorber 206, the high-pressure working fluid vapor is absorbed by the concentrated solution to generate a large amount of absorption heat, so that the lithium bromide in the absorber 206 The temperature of the solution increases sharply; the diluted lithium bromide solution after the temperature rise enters the fifth evaporator 207 for heat exchange, and the diluted lithium bromide solution after the temperature reduction enters the energy storage device 208 to exchange heat with the energy storage phase change material, and then the diluted lithium bromide solution enters the fourth preheating device. Heat is exchanged in the heater 209, and finally the dilute lithium bromide solution is depressurized through the second pressure reducing valve 211 and then enters the generator 201 for the next cycle.

二、储能模式2. Energy storage mode

当印染厂存在中温废水但没有淡碱液处理需求时，则启动储能模式，具体方法步骤是：关闭第一截止阀303、第二截止阀304、第三截止阀305、第四截止阀306、第五截止阀307 和电动调节阀401，二效蒸馏循环系统不运行，单独运行吸收式热泵循环系统，其过程与上述联合运行模式相同，利用储能器208将高温热量储存起来备用。When there is medium-temperature wastewater in the printing and dyeing factory but there is no need for light lye treatment, the energy storage mode is activated. The specific method steps are: closing the first cut-off valve 303, the second cut-off valve 304, the third cut-off valve 305, and the fourth cut-off valve 306 , the fifth shut-off valve 307 and the electric regulating valve 401, the two-effect distillation cycle system does not operate, and the absorption heat pump cycle system is operated alone. The process is the same as the above-mentioned combined operation mode.

三、蒸馏处理模式3. Distillation treatment mode

当印染厂无中温废水排放，但需要进行淡碱液处理时，则启动蒸馏处理模式，具体方法步骤是：打开第三截止阀305、第四截止阀306、第五截止阀307和电动调节阀401，关闭第一截止阀303和第二截止阀304，吸收式热泵循环系统不运行，单独运行二效蒸馏循环系统，淡碱溶液和补充水的处理过程与上述联合运行模式相同，不同的是，第二蒸发器106内产生的二次蒸气进入第四蒸发器205换热，之后与第四蒸发器205出口f4流出的补充水混合进入第四离心泵301内加压，之后经第四截止阀306流入储能器208内与储能相变材料换热，温度升高后经第五截止阀307流入气液分离器302，分离后的液态水经第三截止阀305与二次蒸汽、补充水进行混合，水蒸气由气液分离器302出口g2流入第一蒸发器105内换热，产生的水蒸汽流入第二蒸发器106进行下一次循环。When the printing and dyeing factory has no medium-temperature wastewater discharge, but needs to carry out light lye treatment, the distillation treatment mode is activated. The specific method steps are: open the third stop valve 305, the fourth stop valve 306, the fifth stop valve 307 and the electric regulating valve. 401, close the first shut-off valve 303 and the second shut-off valve 304, the absorption heat pump circulation system does not operate, and the two-effect distillation circulation system is operated alone. , the secondary steam generated in the second evaporator 106 enters the fourth evaporator 205 for heat exchange, and then mixes with the supplementary water flowing out of the outlet f4 of the fourth evaporator 205 and enters the fourth centrifugal pump 301 for pressure, and then passes through the fourth cut-off The valve 306 flows into the accumulator 208 to exchange heat with the energy storage phase change material. After the temperature rises, it flows into the gas-liquid separator 302 through the fifth cut-off valve 307. The separated liquid water passes through the third cut-off valve 305 and the secondary steam, The supplementary water is mixed, the water vapor flows into the first evaporator 105 from the outlet g2 of the gas-liquid separator 302 for heat exchange, and the generated water vapor flows into the second evaporator 106 for the next cycle.

进一步，所述电动调节阀401的开度与气液分离器302内的液位高度成反比例调节关系，所述电动调节阀401的开度与气液分离器302出口蒸汽温度成正比例调节关系；Further, the opening of the electric control valve 401 is in an inversely proportional adjustment relationship with the liquid level in the gas-liquid separator 302, and the opening of the electric control valve 401 is in a proportional adjustment relationship with the outlet steam temperature of the gas-liquid separator 302;

第二类吸收式热泵属于“升温型”热泵，输出热的温度比驱动热源的温度高，但是输出的热量比驱动热源的热量少。多效蒸馏系统利用蒸发器压差回收自身系统的蒸汽潜热实现多次蒸发和冷凝，结合第二类吸收式热泵系统对多效蒸馏系统末级蒸发器产生的二次蒸汽进行升温再利用，既能极大限度地降低蒸发过程的能耗，又能有效回收印染过程产生的大量低温废水的热量，提高系统能源效率。The second type of absorption heat pump belongs to the "heating type" heat pump, which outputs heat at a higher temperature than the driving heat source, but outputs less heat than the driving heat source. The multi-effect distillation system uses the evaporator pressure difference to recover the steam latent heat of its own system to realize multiple evaporation and condensation. Combined with the second type of absorption heat pump system, the secondary steam generated by the last-stage evaporator of the multi-effect distillation system is heated and reused. It can greatly reduce the energy consumption of the evaporation process, and can effectively recover the heat of a large amount of low-temperature wastewater generated in the printing and dyeing process, and improve the energy efficiency of the system.

附图说明Description of drawings

图1为本发明流程系统图。Fig. 1 is a flow chart of the present invention.

图中：101为第一离心泵、102为第一预热器、103为第二预热器、104为第三预热器、105为第一蒸发器、106为第二蒸发器、107为第一减压阀、201为发生器、202为冷凝器、 203为第二离心泵、204为第三蒸发器、205为第四蒸发器、206为吸收器、207为第五蒸发器、208为储能器、209为第四预热器、210为第三离心泵、301为第四离心泵、302为气液分离器、303为第一截止阀、304为第二截止阀、305为第三截止阀、306为第四截止阀、307 为第五截止阀、308为液位控制器、309为温度控制器、401为电动调节阀、402为第五离心泵In the figure: 101 is the first centrifugal pump, 102 is the first preheater, 103 is the second preheater, 104 is the third preheater, 105 is the first evaporator, 106 is the second evaporator, 107 is the second evaporator The first pressure reducing valve, 201 is the generator, 202 is the condenser, 203 is the second centrifugal pump, 204 is the third evaporator, 205 is the fourth evaporator, 206 is the absorber, 207 is the fifth evaporator, 208 is the accumulator, 209 is the fourth preheater, 210 is the third centrifugal pump, 301 is the fourth centrifugal pump, 302 is the gas-liquid separator, 303 is the first shut-off valve, 304 is the second shut-off valve, and 305 is the The third stop valve, 306 is the fourth stop valve, 307 is the fifth stop valve, 308 is the liquid level controller, 309 is the temperature controller, 401 is the electric regulating valve, 402 is the fifth centrifugal pump

具体实施方式Detailed ways

为使本发明的上述目的、特征和优点能够更为明显易懂，下面结合附图和实施例对本发明做进一步的详细说明。In order to make the above objects, features and advantages of the present invention more clearly understood, the present invention will be further described in detail below with reference to the accompanying drawings and embodiments.

一种印染淡碱液吸收式热泵多效蒸馏系统，包括多效蒸馏循环系统和吸收式热泵循环系统，所述多效蒸馏循环系统包括：第一离心泵101、第一预热器102、第二预热器103、第三预热器104、第一蒸发器105和第二蒸发器106，印染淡碱液通过管路连通第一离心泵101入口，第一离心泵101出口通过管路连接第一预热器102入口a1，第一预热器102出口a2通过管路连接第二预热器103入口b1，第二预热器103出口b2通过管路连接第三预热器104入口c1，第三预热器104出口c2通过管路连接第一蒸发器105的溶液入口d1，所述第一蒸发器105溶液出口d2经第一减压阀107接至第二蒸发器106溶液入口e1，第一蒸发器105的凝结水d4出口通过管路接至第三预热器104入口c3，第一蒸发器105蒸汽出口d5通过管路接至第二蒸发器106的蒸汽入口e3；第二蒸发器106溶液出口e2通过管路接至第一预热器 102入口a3，第二蒸发器106的凝结水出口e4通过管路接至第二预热器103入口b3；A printing and dyeing light lye absorption heat pump multi-effect distillation system, including a multi-effect distillation cycle system and an absorption heat pump cycle system, the multi-effect distillation cycle system includes: a first centrifugal pump 101, a first preheater 102, a first The second preheater 103, the third preheater 104, the first evaporator 105 and the second evaporator 106, the printing and dyeing light lye is connected to the inlet of the first centrifugal pump 101 through pipelines, and the outlet of the first centrifugal pump 101 is connected through pipelines The inlet a1 of the first preheater 102, the outlet a2 of the first preheater 102 are connected to the inlet b1 of the second preheater 103 through a pipeline, and the outlet b2 of the second preheater 103 is connected to the inlet c1 of the third preheater 104 through a pipeline , the outlet c2 of the third preheater 104 is connected to the solution inlet d1 of the first evaporator 105 through a pipeline, and the solution outlet d2 of the first evaporator 105 is connected to the solution inlet e1 of the second evaporator 106 through the first pressure reducing valve 107 , the outlet of condensed water d4 of the first evaporator 105 is connected to the inlet c3 of the third preheater 104 through a pipeline, and the steam outlet d5 of the first evaporator 105 is connected to the steam inlet e3 of the second evaporator 106 through a pipeline; The solution outlet e2 of the evaporator 106 is connected to the inlet a3 of the first preheater 102 through a pipeline, and the condensed water outlet e4 of the second evaporator 106 is connected to the inlet b3 of the second preheater 103 through a pipeline;

所述吸收式热泵循环系统包括：发生器201、冷凝器202、第二离心泵203、第三蒸发器 204、第四蒸发器205、吸收器206、第五蒸发器207、储能器208、第四预热器209和第三离心泵210；中温废水通过管路连接发生器201入口o1，发生器201出口o2通过管路接至第一蒸发器204的入口j4，第一蒸发器204的出口j3接排放管路，所述发生器201的蒸汽出口o4 通过管路连接冷凝器202入口k1，冷凝器202出口k2通过管路经第二离心泵203接至第一蒸发器204入口j6，第一蒸发器204的出口j5通过管路接至第二蒸发器205的入口f5，第二蒸发器205的出口f6通过管路连接至吸收器206的蒸汽入口m2；所述发生器201的浓溴化锂溶液出口o5通过管路经第三离心泵210连接至第四预热器209入口i4，第四预热器209出口i3通过管路连接至吸收器206的浓溶液入口m1；所述吸收器206的溴化锂稀溶液出口m3 通过管路连接至第三蒸发器207的入口h3，第三蒸发器207的出口h4通过管路连接至储能器208的蓄热管路入口n1，储能器208的出口n2通过管路接至第四预热器209的入口i1，第四预热器209的出口i2通过管路经第二减压阀211接至发生器201的溴化锂稀溶液入口o3；The absorption heat pump circulation system includes: a generator 201, a condenser 202, a second centrifugal pump 203, a third evaporator 204, a fourth evaporator 205, an absorber 206, a fifth evaporator 207, an accumulator 208, The fourth preheater 209 and the third centrifugal pump 210; the medium temperature wastewater is connected to the inlet o1 of the generator 201 through a pipeline, and the outlet o2 of the generator 201 is connected to the inlet j4 of the first evaporator 204 through a pipeline. The outlet j3 is connected to the discharge pipeline, the steam outlet o4 of the generator 201 is connected to the inlet k1 of the condenser 202 through the pipeline, and the outlet k2 of the condenser 202 is connected to the inlet j6 of the first evaporator 204 through the pipeline through the second centrifugal pump 203, The outlet j5 of the first evaporator 204 is connected to the inlet f5 of the second evaporator 205 through a pipeline, and the outlet f6 of the second evaporator 205 is connected to the steam inlet m2 of the absorber 206 through a pipeline; The lithium bromide solution outlet o5 is connected to the inlet i4 of the fourth preheater 209 through a pipeline through the third centrifugal pump 210, and the outlet i3 of the fourth preheater 209 is connected to the concentrated solution inlet m1 of the absorber 206 through a pipeline; the absorber The lithium bromide dilute solution outlet m3 of 206 is connected to the inlet h3 of the third evaporator 207 through a pipeline, and the outlet h4 of the third evaporator 207 is connected to the heat storage pipeline inlet n1 of the accumulator 208 through a pipeline. The outlet n2 is connected to the inlet i1 of the fourth preheater 209 through the pipeline, and the outlet i2 of the fourth preheater 209 is connected to the inlet o3 of the dilute lithium bromide solution of the generator 201 through the second pressure reducing valve 211;

所述第二蒸发器106顶部二次蒸汽出口e5通过管路连接至第四蒸发器205入口f1，第四蒸发器205出口f2通过管路连接至第四离心泵301入口，所述第四离心泵301出口通过管路经第一截止阀303接至第五蒸发器207的入口h1，第五蒸发器207的出口h2通过管路经第二截止阀304连接至气液分离器302入口g1，所述气液分离器302蒸汽出口g2通过管路连接至第一蒸发器105的蒸汽入口d3，所述气液分离器302的水出口g3通过管路经第三截止阀305连接至第四离心泵301的入口管路；The secondary steam outlet e5 at the top of the second evaporator 106 is connected to the inlet f1 of the fourth evaporator 205 through a pipeline, and the outlet f2 of the fourth evaporator 205 is connected to the inlet of the fourth centrifugal pump 301 through a pipeline. The outlet of the pump 301 is connected to the inlet h1 of the fifth evaporator 207 through the first stop valve 303 through the pipeline, and the outlet h2 of the fifth evaporator 207 is connected to the inlet g1 of the gas-liquid separator 302 through the pipeline through the second stop valve 304. The steam outlet g2 of the gas-liquid separator 302 is connected to the steam inlet d3 of the first evaporator 105 through a pipeline, and the water outlet g3 of the gas-liquid separator 302 is connected to the fourth centrifugal pump through a pipeline through the third stop valve 305 the inlet line of the pump 301;

系统补给水通过管路依次经电动调节阀401和第五离心泵402连接至第三蒸发器204的入口j1，第三蒸发器204的出口j2通过管路连接至第二蒸发器205的入口f3，第二蒸发器205 的出口f4通过管路连接至第四离心泵301的入口管路；The system make-up water is connected to the inlet j1 of the third evaporator 204 through the electric regulating valve 401 and the fifth centrifugal pump 402 in sequence through the pipeline, and the outlet j2 of the third evaporator 204 is connected to the inlet f3 of the second evaporator 205 through the pipeline. , the outlet f4 of the second evaporator 205 is connected to the inlet pipeline of the fourth centrifugal pump 301 through a pipeline;

所述第四离心泵301出口还通过管路经第四截止阀306连接至储能器208的入口n3，所述储能器208的出口n4通过管路经第五截止阀307连接至气液分离器302的入口g1，当无中温废水可利用时，可利用储能器208内储能相变材料提供热量；The outlet of the fourth centrifugal pump 301 is also connected to the inlet n3 of the accumulator 208 through the fourth cut-off valve 306 through the pipeline, and the outlet n4 of the accumulator 208 is connected to the gas-liquid through the fifth cut-off valve 307 through the pipeline. At the inlet g1 of the separator 302, when there is no intermediate-temperature wastewater available, the energy storage phase change material in the energy storage device 208 can be used to provide heat;

所述气液分离器302内设有液位控制器308，所述气液分离器302出口管路上设置有温度控制器309，所述液位控制器308和温度控制器309通过信号线连接电动调节阀401；The gas-liquid separator 302 is provided with a liquid level controller 308, the outlet pipeline of the gas-liquid separator 302 is provided with a temperature controller 309, and the liquid level controller 308 and the temperature controller 309 are connected to an electric motor through a signal line. regulating valve 401;

所述储能器208使用的储能相变材料为Mg(NO3)2 ·2H2O或NaNO3─LiNO3/石墨复合储能材料，可以储存吸收式热泵系统产生的富余热量；The energy storage phase change material used in the energy storage device 208 is Mg(NO 3 ) 2 ·2H 2 O or NaNO 3 ─ LiNO 3 /graphite composite energy storage material, which can store excess heat generated by the absorption heat pump system;

所述多效蒸馏循环系统根据淡碱液浓度设置为二效蒸馏循环系统、三效蒸馏循环系统或四效蒸馏循环系统；The multi-effect distillation circulating system is set as a two-effect distillation circulating system, a three-effect distillation circulating system or a four-effect distillation circulating system according to the concentration of the light lye;

所述第一预热器102还设置有浓溶液出口a4；所述第二预热器103还设置有冷凝水出口 b4；所述第三预热器104还设置有冷凝水出口c4；所述冷凝器202还设置有冷却水出口k3 和低温冷却水入口k4；The first preheater 102 is also provided with a concentrated solution outlet a4; the second preheater 103 is also provided with a condensed water outlet b4; the third preheater 104 is also provided with a condensed water outlet c4; The condenser 202 is also provided with a cooling water outlet k3 and a low temperature cooling water inlet k4;

一种印染淡碱液吸收式热泵多效蒸馏系统的工作方法，包括联合运行模式、储能模式和蒸馏处理模式；A working method of a light lye absorption heat pump multi-effect distillation system for printing and dyeing, comprising a combined operation mode, an energy storage mode and a distillation treatment mode;

一、联合运行模式：1. Joint operation mode:

当印染厂存在中温废水且需要处理淡碱液时，则启动联合运行模式，具体方法步骤是：打开第一截止阀303、第二截止阀304、第三截止阀305和电动调节阀401，关闭第四截止阀306、第五截止阀307，淡碱稀溶液进入第一离心泵101内加压，然后进入第一预热器102被浓溶液预热，进入第二预热器103和第三预热器104被冷凝水预热，进入第一蒸发器105内的淡碱稀溶液与高温蒸汽换热，产生的二次蒸汽由第一蒸发器105顶部出口d5流入第二蒸发器106内，淡碱溶液由第一蒸发器105出口d2流出，经第一减压阀107降压后继续进入第二蒸发器106内换热，冷凝水由第一蒸发器105出口d4流入第三预热器104内换热；第二蒸发器106内的淡碱浓溶液由第二蒸发器106出口e2流入第一预热器102内与淡碱稀溶液换热，冷凝水由第二蒸发器106出口e4流入第二预热器103内换热，二次蒸汽由第二蒸发器106出口e5流入第四蒸发器205内释放热量，液化后的凝结水进入第二离心泵301内升压，然后进入第五蒸发器207内吸收热量汽化为饱和蒸汽，通过第二截止阀304进入气液分离器302，水蒸气由气液分离器302出口g2流入第一蒸发器105内继续下一循环；重新升温后的二次蒸汽不能满足二效蒸馏循环系统的运行，需要对蒸汽进行补充，补充水经过电动调节阀401进入第五离心泵402，升压后依次经第三蒸发器204和第四蒸发器205进行预热，与第四蒸发器205出口f2流出的冷凝水混合，进入第二离心泵301内加压；When the printing and dyeing factory has medium-temperature wastewater and needs to treat light lye, the joint operation mode is started. The specific method steps are: open the first stop valve 303, the second stop valve 304, the third stop valve 305 and the electric regulating valve 401, close the The fourth cut-off valve 306 and the fifth cut-off valve 307, the diluted alkaline solution enters the first centrifugal pump 101 for pressure, then enters the first preheater 102 to be preheated by the concentrated solution, enters the second preheater 103 and the third The preheater 104 is preheated by the condensed water, and the diluted alkaline solution entering the first evaporator 105 exchanges heat with the high temperature steam, and the generated secondary steam flows into the second evaporator 106 from the top outlet d5 of the first evaporator 105, The light alkali solution flows out from the outlet d2 of the first evaporator 105, and after being depressurized by the first pressure reducing valve 107, it continues to enter the second evaporator 106 for heat exchange, and the condensed water flows into the third preheater from the outlet d4 of the first evaporator 105. Heat exchange in 104; the light alkali concentrated solution in the second evaporator 106 flows into the first preheater 102 from the outlet e2 of the second evaporator 106 to exchange heat with the light alkali dilute solution, and the condensed water flows from the second evaporator 106 outlet e4 It flows into the second preheater 103 for heat exchange, the secondary steam flows into the fourth evaporator 205 from the outlet e5 of the second evaporator 106 to release heat, and the liquefied condensed water enters the second centrifugal pump 301 for boosting, and then enters the second evaporator 301. The heat absorbed in the fifth evaporator 207 is vaporized into saturated steam, which enters the gas-liquid separator 302 through the second shut-off valve 304, and the water vapor flows into the first evaporator 105 from the outlet g2 of the gas-liquid separator 302 to continue the next cycle; The secondary steam cannot meet the operation of the two-effect distillation cycle system, and it is necessary to supplement the steam. The supplementary water enters the fifth centrifugal pump 402 through the electric regulating valve 401, and then passes through the third evaporator 204 and the fourth evaporator 205 after being boosted. Carry out preheating, mix with the condensed water flowing out of the outlet f2 of the fourth evaporator 205, and enter the second centrifugal pump 301 to pressurize;

中温废水进入发生器201内与溴化锂溶液换热，然后进入第三蒸发器204内与饱和水和补充水换热，然后由第三蒸发器204出口j3排出；发生器201内的稀溴化锂溶液与中温废水换热，产生了低压工质水蒸汽，水蒸汽由发生器201出口o4流入冷凝器202内，与低温冷却水换热后冷凝成饱和水，饱和水经过第四离心泵203升压后进入第三蒸发器204与中温废水换热成湿饱和蒸汽，然后进入第四蒸发器205与二次蒸汽换热变成干饱和蒸汽，温度升高后进入吸收器206内进行热质交换；发生器(201)中稀溴化锂溶液被中温废水加热蒸发部分水后变成浓溴化锂溶液，浓溴化锂溶液由发生器201出口o5流入第三离心泵210内升压，然后进入第四预热器209内与稀溶液换热，温度升高后进入吸收器206内进行热质交换；在吸收器206内，高压工质蒸汽被浓溶液吸收产生大量的吸收热，使得吸收器206内的溴化锂溶液温度急剧增高；升温后的稀溴化锂溶液进入第五蒸发器207进行热交换，温度降低后的稀溴化锂溶液进入储能器208与储能相变材料换热，部分热量被储存再相变材料中，在其他工作模式中提供热量，随后稀溴化锂溶液进入第四预热器209内与浓溴化锂溶液换热，最后稀溴化锂溶液经过第二减压阀211降压后进入发生器201内进行下一步循环；The medium-temperature waste water enters the generator 201 to exchange heat with the lithium bromide solution, then enters the third evaporator 204 to exchange heat with saturated water and supplemental water, and is then discharged from the outlet j3 of the third evaporator 204; the dilute lithium bromide solution in the generator 201 and The medium-temperature wastewater exchanges heat to generate low-pressure working fluid water vapor, which flows into the condenser 202 from the outlet o4 of the generator 201, and condenses into saturated water after exchanging heat with the low-temperature cooling water. The saturated water is boosted by the fourth centrifugal pump 203. Enter the third evaporator 204 to exchange heat with the medium-temperature waste water to form wet saturated steam, then enter the fourth evaporator 205 to exchange heat with the secondary steam to become dry saturated steam, and enter the absorber 206 for heat and mass exchange after the temperature rises; In the device (201), the dilute lithium bromide solution is heated by the medium-temperature waste water to evaporate part of the water and becomes a concentrated lithium bromide solution, and the concentrated lithium bromide solution flows into the third centrifugal pump 210 from the outlet o5 of the generator 201 to boost pressure, and then enters the fourth preheater 209. Exchange heat with the dilute solution, and enter the absorber 206 for heat and mass exchange after the temperature rises; in the absorber 206, the high-pressure working fluid vapor is absorbed by the concentrated solution to generate a large amount of heat of absorption, so that the temperature of the lithium bromide solution in the absorber 206 is sharp. increased; the dilute lithium bromide solution after the temperature rise enters the fifth evaporator 207 for heat exchange, the dilute lithium bromide solution after the temperature reduction enters the accumulator 208 and exchanges heat with the energy storage phase change material, and part of the heat is stored in the phase change material, in the In other working modes, heat is provided, and then the dilute lithium bromide solution enters the fourth preheater 209 to exchange heat with the concentrated lithium bromide solution, and finally the dilute lithium bromide solution enters the generator 201 after being depressurized by the second pressure reducing valve 211 to carry out the next cycle;

二、储能模式2. Energy storage mode

当印染厂存在中温废水但没有淡碱液处理需求时，则启动储能模式，具体方法步骤是：关闭第一截止阀303、第二截止阀304、第三截止阀305、第四截止阀306、第五截止阀307 和电动调节阀401，二效蒸馏循环系统不运行，单独运行吸收式热泵循环系统，其过程与上述联合运行模式相同，目的是利用Mg(NO3)2 ·2H2O做成的储能器将吸收器产生的高温热量存储起来备用，Mg(NO3)2 ·2H2O的相变温度为130℃，能够满足二效蒸馏系统第一蒸发器蒸汽温度为127℃的需求；When there is medium-temperature wastewater in the printing and dyeing factory but there is no need for light lye treatment, the energy storage mode is activated. The specific method steps are: closing the first cut-off valve 303, the second cut-off valve 304, the third cut-off valve 305, and the fourth cut-off valve 306 , the fifth cut-off valve 307 and the electric regulating valve 401, the two-effect distillation cycle system is not operated, and the absorption heat pump cycle system is operated alone, the process is the same as the above-mentioned combined operation mode, the purpose is to use Mg(NO 3 ) 2 ·2H 2 O The built-in energy storage device stores the high temperature heat generated by the absorber for standby use. The phase transition temperature of Mg(NO 3 ) 2 ·2H 2 O is 130℃, which can satisfy the steam temperature of the first evaporator of the two-effect distillation system of 127℃. needs;

三、蒸馏处理模式3. Distillation treatment mode

当印染厂无中温废水排放，但需要进行淡碱液处理时，则启动蒸馏处理模式，具体方法步骤是：打开第三截止阀305、第四截止阀306、第五截止阀307和电动调节阀401，关闭第一截止阀303和第二截止阀304，吸收式热泵循环系统不运行，单独运行二效蒸馏循环系统，淡碱溶液和补充水的处理过程与上述联合运行模式相同，不同的是，第二蒸发器106内产生的二次蒸气进入第四蒸发器205与补充水换热，之后与第四蒸发器205出口f4流出的补充水混合进入第四离心泵301内加压，之后经第四截止阀306流入储能器208内，储能相变材料通过相变产生大量热量，水溶液吸收热量后变成湿饱和蒸汽，然后经第五截止阀307流入气液分离器302分离液滴，分离后的液态水经第三截止阀305与二次蒸汽、补充水进行混合进行下一步循环，水蒸气由气液分离器302出口g2流入第一蒸发器105内与淡碱溶液换热，产生的水蒸汽流入第二蒸发器106进行下一次循环。When the printing and dyeing factory has no medium-temperature wastewater discharge, but needs to carry out light lye treatment, the distillation treatment mode is activated. The specific method steps are: open the third stop valve 305, the fourth stop valve 306, the fifth stop valve 307 and the electric regulating valve. 401, close the first shut-off valve 303 and the second shut-off valve 304, the absorption heat pump circulation system does not operate, and the two-effect distillation circulation system is operated alone. , the secondary steam generated in the second evaporator 106 enters the fourth evaporator 205 to exchange heat with the supplementary water, and then mixes with the supplementary water flowing out of the outlet f4 of the fourth evaporator 205 and enters the fourth centrifugal pump 301 for pressure, and then passes through The fourth shut-off valve 306 flows into the accumulator 208, the energy-storing phase change material generates a large amount of heat through the phase change, the aqueous solution absorbs the heat and becomes wet saturated steam, and then flows into the gas-liquid separator 302 through the fifth shut-off valve 307 to separate droplets , the separated liquid water is mixed with the secondary steam and supplementary water through the third cut-off valve 305 for the next cycle, and the water vapor flows into the first evaporator 105 from the outlet g2 of the gas-liquid separator 302 to exchange heat with the light alkaline solution, The generated water vapor flows into the second evaporator 106 for the next cycle.

所述电动调节阀401的开度与气液分离器302内的液位高度成反比例调节关系，当气液分离器302内的液位高度变高时，说明液态水量充足，此时需要调小电动调节阀401的阀门开度，减少补充水流量，所述电动调节阀401的开度与气液分离器302出口蒸汽温度成正比例调节关系，当气液分离器302出口蒸汽温度升高时，说明系统可利用热量富裕，需要增大电动调节阀401阀门开度，增加补充水流量，从而降低蒸汽温度。The opening of the electric regulating valve 401 is in an inversely proportional adjustment relationship with the liquid level in the gas-liquid separator 302. When the liquid level in the gas-liquid separator 302 becomes higher, it means that the amount of liquid water is sufficient. At this time, it needs to be adjusted smaller. The valve opening of the electric control valve 401 reduces the flow of supplementary water. The opening of the electric control valve 401 is proportional to the steam temperature at the outlet of the gas-liquid separator 302. When the temperature of the steam at the outlet of the gas-liquid separator 302 increases, It shows that the system can be rich in heat, and it is necessary to increase the valve opening of the electric regulating valve 401 to increase the flow of supplementary water, thereby reducing the steam temperature.

虽然本发明披露如上，但本发明并非限定于此。任何本领域技术人员，在不脱离本发明的精神和范围内，均可作各种变更与修改，因此本发明的保护范围应当以权利要求所限定的范围为准。Although the present invention is disclosed above, the present invention is not limited thereto. Any person skilled in the art can make various changes and modifications without departing from the spirit and scope of the present invention. Therefore, the protection scope of the present invention should be based on the scope defined by the claims.

Claims (7)

1. The printing and dyeing weak lye absorption heat pump multi-effect distillation system comprises a multi-effect distillation circulation system and an absorption heat pump circulation system, and is characterized in that the multi-effect distillation circulation system comprises: the dyeing and finishing machine comprises a first centrifugal pump (101), a first preheater (102), a second preheater (103), a third preheater (104), a first evaporator (105) and a second evaporator (106), wherein dyeing and finishing weak lye is communicated with an inlet of the first centrifugal pump (101) through a pipeline, an outlet of the first centrifugal pump (101) is connected with an inlet (a 1) of the first preheater (102) through a pipeline, an outlet a2 of the first preheater (102) is connected with an inlet (b 1) of the second preheater (103) through a pipeline, an outlet (b 2) of the second preheater (103) is connected with an inlet (c 1) of the third preheater (104) through a pipeline, an outlet (c 2) of the third preheater (104) is connected with a solution inlet (d 1) of the first evaporator (105) through a pipeline, a solution outlet (d 2) of the first evaporator (105) is connected with a solution inlet (e 1) of the second evaporator (106) through a first pressure reducing valve (107), a condensed water outlet (d 4) of the first evaporator (105) is connected with an inlet (c 3) of the third preheater (104) through a pipeline, and an outlet (105) of the first evaporator is connected with a steam inlet (e 3) of the second evaporator (106) through a steam inlet (106) of the second evaporator (106); the solution outlet (e 2) of the second evaporator (106) is connected to the inlet (a 3) of the first preheater (102) through a pipeline, and the condensed water outlet (e 4) of the second evaporator (106) is connected to the inlet (b 3) of the second preheater (103) through a pipeline;
the absorption heat pump circulation system comprises: the system comprises a generator (201), a condenser (202), a second centrifugal pump (203), a third evaporator (204), a fourth evaporator (205), an absorber (206), a fifth evaporator (207), an energy storage device (208), a fourth preheater (209) and a third centrifugal pump (210); the medium-temperature waste water is connected with an inlet (o 1) of a generator (201) through a pipeline, an outlet (o 2) of the generator (201) is connected to an inlet (j 4) of a first evaporator (105) through a pipeline, an outlet (j 3) of the first evaporator (105) is connected with a discharge pipeline, a steam outlet (o 4) of the generator (201) is connected with an inlet (k 1) of a condenser (202) through a pipeline, an outlet (k 2) of the condenser (202) is connected to an inlet (j 6) of the first evaporator (105) through a pipeline by a second centrifugal pump (203), an outlet (j 5) of the first evaporator (105) is connected to an inlet (f 5) of a second evaporator (106) through a pipeline, and an outlet (f 6) of the second evaporator (106) is connected to a steam inlet (m 2) of an absorber (206) through a pipeline; a concentrated lithium bromide solution outlet (o 5) of the generator (201) is connected to an inlet (i 4) of a fourth preheater (209) through a pipeline by a third centrifugal pump (210), and an outlet (i 3) of the fourth preheater (209) is connected to a concentrated solution inlet (m 1) of an absorber (206) through a pipeline; a lithium bromide dilute solution outlet (m 3) of the absorber (206) is connected to an inlet (h 3) of the third evaporator (204) through a pipeline, an outlet (h 4) of the third evaporator (204) is connected to a heat storage pipeline inlet (n 1) of the energy storage device (208) through a pipeline, an outlet (n 2) of the energy storage device (208) is connected to an inlet (i 1) of the fourth preheater (209) through a pipeline, and an outlet (i 2) of the fourth preheater (209) is connected to a lithium bromide dilute solution inlet (o 3) of the generator (201) through a second pressure reducing valve (211) through a pipeline;
the top secondary steam outlet (e 5) of the second evaporator (106) is connected to the inlet (f 1) of a fourth evaporator (205) through a pipeline, the outlet (f 2) of the fourth evaporator (205) is connected to the inlet of a fourth centrifugal pump (301) through a pipeline, the outlet of the fourth centrifugal pump (301) is connected to the inlet (h 1) of a fifth evaporator (207) through a pipeline by a first stop valve (303), the outlet (h 2) of the fifth evaporator (207) is connected to the inlet (g 1) of a gas-liquid separator (302) through a pipeline by a second stop valve (304), the steam outlet (g 2) of the gas-liquid separator (302) is connected to the steam inlet (d 3) of the first evaporator (105) through a pipeline, and the water outlet (g 3) of the gas-liquid separator (302) is connected to the inlet pipeline of the fourth centrifugal pump (301) through a third stop valve (305) through a pipeline;
the system make-up water is sequentially connected to an inlet (j 1) of a third evaporator (204) through an electric regulating valve (401) and a fifth centrifugal pump (402) through pipelines, an outlet (j 2) of the third evaporator (204) is connected to an inlet (f 3) of a second evaporator (106) through a pipeline, and an outlet (f 4) of the second evaporator (106) is connected to an inlet pipeline of a fourth centrifugal pump (301) through a pipeline.
2. The multiple-effect distillation system of the dyeing weak lye absorption heat pump according to claim 1, characterized in that the outlet of the fourth centrifugal pump (301) is further connected to the inlet (n 3) of the energy accumulator (208) through a fourth stop valve (306) by a pipeline, and the outlet (n 4) of the energy accumulator (208) is connected to the inlet (g 1) of the gas-liquid separator (302) through a fifth stop valve (307) by a pipeline.
3. The multiple-effect distillation system of the printing and dyeing weak lye absorption heat pump according to claim 1, characterized in that a liquid level controller (308) is arranged in the gas-liquid separator (302), a temperature controller (309) is arranged on an outlet pipeline of the gas-liquid separator (302), and the liquid level controller (308) and the temperature controller (309) are connected with an electric regulating valve (401) through signal lines.
4. The multiple-effect distillation system of the printing and dyeing weak lye absorption heat pump according to claim 1, wherein the multiple-effect distillation circulating system is arranged as a two-effect distillation circulating system, a three-effect distillation circulating system or a four-effect distillation circulating system according to the concentration of the weak lye.
5. The multiple-effect distillation system of the absorption heat pump for the printing and dyeing weak lye as claimed in claim 1, wherein the first preheater (102) is further provided with a concentrated solution outlet (a 4); the second preheater (103) is also provided with a condensed water outlet (b 4); the third preheater (104) is also provided with a condensed water outlet (c 4); the condenser (202) is also provided with a cooling water outlet (k 3) and a low-temperature cooling water inlet (k 4).
6. The working method of the multiple-effect distillation system of the printing and dyeing weak lye absorption heat pump is characterized by comprising a combined operation mode, an energy storage mode and a distillation treatment mode:
1. a combined operation mode:
when medium-temperature wastewater exists in a printing and dyeing mill and weak alkali liquor needs to be treated, a combined operation mode is started, and the specific method comprises the following steps: opening a first stop valve (303), a second stop valve (304), a third stop valve (305) and an electric regulating valve (401), closing a fourth stop valve (306) and a fifth stop valve (307), enabling the dilute light alkali solution to enter a first centrifugal pump (101) for pressurization, then sequentially passing through a first preheater (102), a second preheater (103) and a third preheater (104) for preheating, and then entering a first evaporator (105), enabling steam generated after the dilute light alkali solution in the first evaporator (105) is heated to flow into a second evaporator (106) through a steam outlet (d 5) of the first evaporator (105), enabling the light alkali solution to flow out from a solution outlet (d 2) of the first evaporator (105), reducing the pressure through a first pressure reducing valve (107), then continuously entering the second evaporator (106) for heat exchange, and enabling condensate water to flow into a third preheater (104) through a condensate water outlet (d 4) of the first evaporator (105) for heat exchange; the weak alkali concentrated solution in the second evaporator (106) flows into the first preheater (102) from a solution outlet (e 2) of the second evaporator (106) for heat exchange, condensed water flows into the second preheater (103) from a condensed water outlet (e 4) of the second evaporator (106) for heat exchange, secondary steam flows into the fourth evaporator (205) from a secondary steam outlet (e 5) at the top of the second evaporator (106) for heat exchange, the liquefied condensed water enters the second centrifugal pump (203) for pressure rise, then enters the fifth evaporator (207) for heat absorption and vaporization to form saturated steam, and enters the gas-liquid separator (302) through the second stop valve (304), and the water vapor flows into the first evaporator (105) from a steam outlet (g 2) of the gas-liquid separator (302) for continuous next circulation; the secondary steam after being reheated can not meet the operation of the two-effect distillation circulating system, the steam needs to be supplemented, make-up water enters a fifth centrifugal pump (402) through an electric regulating valve (401), is preheated through a third evaporator (204) and a fourth evaporator (205) in sequence after being boosted, is mixed with condensate water flowing out of an outlet (f 2) of the fourth evaporator (205), and enters a second centrifugal pump (203) for pressurization;
the medium-temperature wastewater enters a generator (201) for heat exchange, then enters a third evaporator (204) for continuous heat exchange, and then is discharged from an outlet (j 3) of the third evaporator (204); dilute lithium bromide solution in the generator (201) is heated to generate low-pressure working medium water vapor, the water vapor flows into the condenser (202) from a vapor outlet (o 4) of the generator (201), exchanges heat with low-temperature cooling water and is condensed into saturated water, the saturated water enters the third evaporator (204) to exchange heat with medium-temperature wastewater after being boosted by the fourth centrifugal pump (301), then enters the fourth evaporator (205) to exchange heat with secondary vapor, and enters the absorber (206) to exchange heat and mass after the temperature is raised; the concentrated lithium bromide solution flows into a third centrifugal pump (210) from a concentrated lithium bromide solution outlet (o 5) of the generator (201) for boosting, then enters a fourth preheater (209) for heat exchange, and enters an absorber (206) for heat and mass exchange after the temperature is raised; in the absorber (206), high-pressure working medium steam is absorbed by the concentrated solution to generate a large amount of absorption heat, so that the temperature of the lithium bromide solution in the absorber (206) is increased rapidly; the heated dilute lithium bromide solution enters a fifth evaporator (207) for heat exchange, the dilute lithium bromide solution with the reduced temperature enters an energy storage device (208) for heat exchange with an energy storage phase-change material, then the dilute lithium bromide solution enters a fourth preheater (209) for heat exchange, and finally the dilute lithium bromide solution enters a generator (201) for next circulation after being subjected to pressure reduction by a second pressure reducing valve (211);
2. energy storage mode
When medium-temperature wastewater exists in a printing and dyeing mill but no weak alkali liquor treatment requirement exists, an energy storage mode is started, and the specific method comprises the following steps: closing the first stop valve (303), the second stop valve (304), the third stop valve (305), the fourth stop valve (306), the fifth stop valve (307) and the electric regulating valve (401), wherein the double-effect distillation circulating system does not operate, and the absorption heat pump circulating system operates independently, the process of the double-effect distillation circulating system is the same as the combined operation mode, and the energy accumulator (208) is used for storing high-temperature heat for standby;
3. distillation treatment mode
When no medium temperature waste water is discharged from a printing and dyeing mill but light alkali liquor treatment is needed, a distillation treatment mode is started, and the specific method comprises the following steps: the method comprises the steps of opening a third stop valve (305), a fourth stop valve (306), a fifth stop valve (307) and an electric control valve (401), closing a first stop valve (303) and a second stop valve (304), not operating an absorption heat pump circulating system, operating a two-effect distillation circulating system independently, enabling the treatment processes of the weak base solution and the make-up water to be the same as the combined operation mode, except that secondary steam generated in a second evaporator (106) enters a fourth evaporator (205) for heat exchange, then is mixed with the make-up water flowing out of an outlet (f 4) of the fourth evaporator (205) to enter a fourth centrifugal pump (301) for pressurization, then flows into an energy storage phase change material for heat exchange through the fourth stop valve (306) and flows into a gas-liquid separator (302) through the fifth stop valve (307) after the temperature is increased, separated liquid water is mixed with the secondary steam and the make-up water through the third stop valve (305), and the make-up steam flows into a first evaporator (105) through a steam outlet (g 2) of the gas-liquid separator (302) for heat exchange, and the generated water flows into the second evaporator (106) for primary circulation mode.
7. The working method of the printing and dyeing weak alkali solution absorption heat pump multi-effect distillation system as claimed in claim 6, characterized in that the opening degree of the electric control valve (401) is inversely proportional to the liquid level height in the gas-liquid separator (302); the opening degree of the electric regulating valve (401) is in direct proportion regulation relation with the temperature of steam at the outlet of the gas-liquid separator (302).
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Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN106241833A (en) * 2016-10-08 2016-12-21 无锡诚尔鑫环保装备科技有限公司 A kind of method of the recycling of light alkali wasteliquid regeneration high alkali liquid
CN106766342A (en) * 2016-12-12 2017-05-31 松下制冷（大连）有限公司 Ammonia still process column overhead ammonia vapour residual heat system is reclaimed using lithium bromide absorption type heat pump
CN108126362A (en) * 2018-01-31 2018-06-08 宜兴市华东印染机械厂 A kind of light alkali evaporation equipment of multistage and mercerizing diluting alkali recovery system
CN109099743A (en) * 2018-07-02 2018-12-28 东南大学 A kind of multi-heat source residual neat recovering system
CN111087034A (en) * 2019-12-12 2020-05-01 西安交通大学 Desulfurization waste water and salt recovery system and method of integrated absorption heat pump

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN106241833A (en) * 2016-10-08 2016-12-21 无锡诚尔鑫环保装备科技有限公司 A kind of method of the recycling of light alkali wasteliquid regeneration high alkali liquid
CN106766342A (en) * 2016-12-12 2017-05-31 松下制冷（大连）有限公司 Ammonia still process column overhead ammonia vapour residual heat system is reclaimed using lithium bromide absorption type heat pump
CN108126362A (en) * 2018-01-31 2018-06-08 宜兴市华东印染机械厂 A kind of light alkali evaporation equipment of multistage and mercerizing diluting alkali recovery system
CN109099743A (en) * 2018-07-02 2018-12-28 东南大学 A kind of multi-heat source residual neat recovering system
CN111087034A (en) * 2019-12-12 2020-05-01 西安交通大学 Desulfurization waste water and salt recovery system and method of integrated absorption heat pump

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