WO2009094896A1 - An evaporating system and an evaporating-concentrating method - Google Patents

An evaporating system and an evaporating-concentrating method Download PDF

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Publication number
WO2009094896A1
WO2009094896A1 PCT/CN2009/000076 CN2009000076W WO2009094896A1 WO 2009094896 A1 WO2009094896 A1 WO 2009094896A1 CN 2009000076 W CN2009000076 W CN 2009000076W WO 2009094896 A1 WO2009094896 A1 WO 2009094896A1
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Prior art keywords
absorption solution
absorber
absorbent
crystallization
generator
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PCT/CN2009/000076
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French (fr)
Chinese (zh)
Inventor
Qingquan Su
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Qingquan Su
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Publication of WO2009094896A1 publication Critical patent/WO2009094896A1/en

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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D9/00—Crystallisation
    • B01D9/0059—General arrangements of crystallisation plant, e.g. flow sheets
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D1/00—Evaporating
    • B01D1/0011—Heating features
    • B01D1/0041—Use of fluids
    • B01D1/0047—Use of fluids in a closed circuit
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D1/00—Evaporating
    • B01D1/16—Evaporating by spraying
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
    • B01D5/0057—Condensation of vapours; Recovering volatile solvents by condensation in combination with other processes
    • B01D5/006—Condensation of vapours; Recovering volatile solvents by condensation in combination with other processes with evaporation or distillation

Definitions

  • the present invention relates to an evaporation technique in the fields of chemical industry, food industry, pharmaceuticals, water treatment and seawater desalination, and more particularly to an absorption evaporation system and an evaporation concentration method for evaporation under substantially no externally driven heat source. Background technique
  • FIG. 1 See Figure 1 for a flow chart of the existing evaporation system. It consists of a steam generator 400, a steam jet pump 440, a heater 410, an evaporation device 420, and a gas-liquid separator 430.
  • the steam generator 400 therein is used to generate high temperature steam, which is supplied to the heater 410 through the steam jet pump 400.
  • the feed liquid is input from the top thereof, absorbs heat from the heater 410, the solvent in the feed liquid is heated and evaporated, and the concentrated feed liquid and vapor are discharged from the evaporation device into the gas-liquid separator 430.
  • the concentrated feed liquid is discharged from the bottom of the gas-liquid separator, the spent steam is output from the top of the gas-liquid separator 430, and a part is led to the steam jet pump 440 which is mixed with the raw steam from the steam generator 400 and then input.
  • the above existing evaporation system has a simple structure and is widely used in the fields of petroleum, chemical, pharmaceutical, fertilizer, paper, aluminum, monosodium glutamate, brewing, sugar, and the like.
  • the main object of the present invention is to overcome the problems of the prior art evaporation system, and to provide an evaporation system and an evaporation concentration method, the technical problem to be solved is to enable the liquid evaporation of the material without substantially driving the external heat source. Concentration of the feed liquid, thereby significantly improving the energy efficiency of the evaporation system, while conserving water resources, is therefore more suitable for practical use.
  • An evaporation system includes a heating device and an evaporation device, the heating device comprising: a generator having a heat exchanger therein for concentrating the absorption solution and generating a vapor; An absorber of a heat exchanger for generating heat, a heat exchanger of the absorber and a heat exchanger of the generator Connected to form a thermal cycle loop for delivering heat generated in the absorber to the generator; and an absorbent crystallizer that receives the absorption solution from the absorber and/or generator and cools to form absorbent crystals and After crystallization, the solution is absorbed, the crystallization solution is sent to the generator, and the absorbent is crystallized and sent to the absorber;
  • the evaporation device comprises: a heater connected to the heating device via a vapor passage, receiving steam generated by the heating device; an evaporation device, performing heat exchange with the heater; and a gas-liquid separator, connecting The evaporation device is connected to the heating device through another vapor passage to supply the steam to the heating device.
  • the foregoing evaporation system further comprises: an absorption solution from the heat exchanger, the absorption solution from the generator and/or the absorption solution from the absorber, and the crystallization of the absorption solution and/or the absorbent after crystallization. Or an absorption solution containing an crystallization of an absorbent for heat exchange.
  • the foregoing evaporation system further comprises: an absorption solution from the heat exchanger for exchanging heat between the absorption solution from the absorber and the post-crystallization absorption solution from the absorbent crystallizer.
  • the foregoing evaporation system further comprises: an absorption solution from the heat exchanger for exchanging heat from the absorption solution from the absorber with the absorption crystal of the absorbent from the absorbent crystallizer or the absorption solution containing the absorbent.
  • the foregoing evaporation system further comprises: an absorption solution from the heat exchanger for crystallization of the absorption solution from the absorber with the crystallization solution and the absorbent from the absorbent crystallizer or the absorption solution containing the absorbent crystals. Perform heat exchange.
  • the absorption solution from the generator and the absorption solution from the absorber are mixed into the absorption solution from the heat exchanger, and the absorption solution and the absorbent from the absorbent crystallizer are crystallized or crystallized with the absorbent.
  • the solution is absorbed for heat exchange.
  • the thermal cycle is provided with an external heat source heating device for compensating for insufficient heat of the generator due to heat loss or the like.
  • the gas-liquid separator of the previous evaporation device is connected to the heater of the next evaporation device; the heater of the first evaporation device
  • the generator connected to the heating device through the vapor passage receives the steam generated by the heating device; the gas-liquid separator of the last evaporation device is connected to the absorber of the heating device to supply the steam to the heating device.
  • the foregoing evaporation system further comprises a compression refrigeration device comprising an absorbent crystallization-evaporator, a compressor, an absorption solution heat exchange-condenser, a throttle valve, and a compression refrigeration refrigerant pipe,
  • a compression refrigeration device comprising an absorbent crystallization-evaporator, a compressor, an absorption solution heat exchange-condenser, a throttle valve, and a compression refrigeration refrigerant pipe,
  • the above absorbent crystallizer provides a cooling capacity.
  • the above evaporation apparatus is employed, which comprises the following steps:
  • the foregoing evaporation concentration method further comprises: after the crystallization solution is transported to the generator after the crystallization, and the absorption solution output by the absorber is cooled, the absorption solution output by the absorber is After crystallization, the solution is absorbed for heat exchange.
  • the foregoing evaporation concentration method further comprises: crystallization of the absorbent or an absorption solution containing an absorbent crystal before the absorption agent is crystallized and transported to the absorber, and before the absorption solution output from the absorber is cooled.
  • the heat exchange is performed with the absorption solution output from the absorber.
  • the foregoing evaporation concentration method further comprises: before the crystallization solution is transported to the generator after crystallization, before the crystallization of the absorbent is delivered to the absorber, and before the absorption solution of the absorber is cooled, the absorber The output absorption solution exchanges heat with the crystallizing absorption solution and the absorbent crystal or the absorption solution containing the absorbent crystal.
  • the foregoing evaporation concentration method further comprises: before the crystallization solution is transported to the generator after the crystallization, the absorption solution of the absorber is output before the absorption agent is crystallized and sent to the absorber. Before the cooling is performed, and the absorption solution outputted by the generator is sent to the absorber, the absorption solution outputted by the generator is mixed with the absorption solution outputted by the absorber to form a mixed absorption solution, and the mixed absorption solution and the crystal are The post-absorption solution and the absorbent crystals or the absorption solution containing the absorbent crystals are subjected to heat exchange.
  • an insufficient portion of the heat of the generator is compensated by an external heat source.
  • the aforementioned evaporation concentration method provides the cooling amount required for the absorption solution to cool the crystal by the compression refrigeration cycle to the above step (5).
  • the temperature of the crystallization solution in the step (5) is -18 to 60 ° C.
  • the present invention has significant advantages and advantageous effects over the prior art. It can be seen from the above technical solutions that the evaporation system and the evaporation concentration method of the present invention have an absorbent crystallizer because of the heat supply device, and the heat generated by the absorber is directly supplied to the generator through the thermal cycle as a heat source of the generator.
  • the external driving heat source required for the absorption heating cycle can be omitted in the heating device, the absorption heating cycle that drives the heat source to be substantially self-supplied, and the heat energy can be sent to the evaporation device through the vapor for the evaporation concentration process, so that the whole
  • the evaporation system basically eliminates the need for an external heat source, effectively conserving energy and water resources, making it more suitable for practical use.
  • Figure 1 is a flow chart of a prior art evaporation system.
  • Fig. 2 is a flow chart showing the evaporation system of the first embodiment of the present invention.
  • Figure 3 is a flow chart of the evaporation system of Embodiment 2 of the present invention.
  • Figure 4 is a flow chart of the evaporation system of Embodiment 3 of the present invention.
  • Figure 5 is a flow chart showing an evaporation system of Embodiment 4 of the present invention.
  • Figure 6 is a flow chart showing an evaporation system of Embodiment 5 of the present invention.
  • Heater 320 Evaporation equipment
  • the evaporation system mainly includes a heating device and an evaporation device, wherein the heating device includes: a generator 11, an absorber 14, an absorption solution from the heat exchanger 150, an absorbent crystallizer 141, and a mixer 142.
  • a pair of water-deuterated lithium working fluid is circulated between the generator 11 and the absorber 14 as an absorbing solution.
  • the generator 11 is for concentrating the absorbing solution and generating superheated steam, and is provided therein with a heat exchanger 110, in which the heat circulating medium from the heat exchanger 140 in the absorber 14 is passed, and the pair is used as an absorbing solution.
  • the lithium telluride solution is heated to evaporate the water, so that the concentration of the absorbent of the absorbing solution is increased, and the high-temperature superheated vapor generated by the bismuth telluride is output to the evaporation device through the vapor passage 19.
  • the generator 11 outlet absorption solution enters the absorber 14 through the absorption solution conduit 20, and the absorber 14 outlet absorption solution enters the generator 11 through the absorption solution conduit 30.
  • the absorption solution is circulated between the generator 11 and the absorber 14 by the absorption solution conduits 20, 30.
  • the absorber 14 receives spent steam from the evaporation device, and the absorber 14 is provided with a heat exchanger 140.
  • the high concentration absorption solution from the generator 11 absorbs the spent steam from the evaporation device and generates The heat is absorbed to increase the temperature of the thermal cycle medium in the heat exchanger 140.
  • the heat exchanger 140 and the heat exchanger 110 in the generator 11 A thermal cycle is formed by the thermal cycle medium conduit 60 so that the heat of absorption generated by the absorber 14 is supplied to the generator 11 as a driving heat source for the generator.
  • the thermal cycle is a heat pipe circulation circuit. At this time, the installation position of the generator 11 is higher than the installation position of the absorber 14.
  • the heat pipe circulates, and the working medium in the heat pipe can form convection through the condensation-evaporation process without external driving force, thereby circulating and transferring heat between the generator and the absorber.
  • An external heat source heating device 160 is disposed on the thermal cycle to compensate for insufficient heat of the generator due to heat loss or the like.
  • the absorption solution is disposed between the absorber 14 and the generator 11 from the heat exchanger 150, the absorbent crystallizer 141, and the mixer 142.
  • the absorbent crystallizer 141 has an absorption solution inlet, an absorption solution outlet, and a crystallization outlet.
  • the absorption solution inlet of the absorbent crystallizer 141 is connected to the absorption solution outlet of the absorber 14 via the absorption solution from the heat exchanger 150, and the absorption solution outlet of the absorbent crystallizer is connected to the generator 11 from the heat exchanger 150 via the absorption solution.
  • the absorption solution inlet of the absorbent crystallizer is connected to the absorption solution inlet of the absorber 11.
  • the crystallization outlet described above is connected to the absorbing solution inlet of the absorber 11 via the mixer 142.
  • the generator 11 outlet absorbing solution enters the absorber 14 through the absorbing solution conduit 20 via the mixer 142, and the absorber 14 outlet absorbing solution passes through the absorbing solution conduit 30 through the absorbing solution from the heat exchanger 150 to the absorbent crystallizer 141.
  • the absorption solution is cooled and crystallized by using a low-temperature cooling amount, and crystallization occurs when the lithium bromide aqueous solution reaches the crystallization temperature of the lithium niobate.
  • the lower the crystallization temperature the lower the equilibrium concentration of the lithium bromide in the liquid phase, and therefore, Cooling crystallization, no matter how high the concentration of lithium bromide in the absorption solution before cooling and crystallization, the lithium bromide concentration of the liquid phase after crystallization can reach or approach the equilibrium concentration of lithium bromide at the cooling temperature.
  • the crystallization absorption solution in the absorbent crystallizer 141 is sent from the heat exchanger 150 to the generator 11 through the absorption solution pipe 30 through the absorption solution.
  • the above-mentioned absorbent crystallizer 141 may use a cold source of 15 to 60 ° C.
  • the above evaporation device is configured to evaporate water in the liquid to be concentrated, and includes a heater 310, an evaporation device 320, and a gas-liquid separator 330.
  • the heater 310 is connected to the generator 11 through the vapor passage 19, and the receiving occurs.
  • the superheated vapor generated by the device 11; the heater 310 and the evaporation device 320 have good heat exchange efficiency, so that the heat of the vapor can be conducted to the liquid in the evaporation device 320, and the evaporation device 320 has the liquid input pipe 301 and the liquid output.
  • the gas-liquid separator 330 is connected to the evaporation device 320 through the liquid-liquid output pipe 302; the gas-liquid separator 330 is connected to the absorber 14 of the heating device through the vapor passage 18 for providing the absorber 14 Lack of steam.
  • a concentrated liquid outlet 303 is provided at the bottom of the gas-liquid separator 330 for outputting the concentrated liquid.
  • a condensate outlet is provided at the bottom of the heater 310 for outputting water evaporated from the material.
  • an external heat source heating means 160 is provided on the thermal circuit between the generator 11 and the absorber 14 for compensating for insufficient heat of the generator due to heat loss or the like.
  • the evaporation system of the first embodiment basically does not need to provide a special driving heat source to carry out evaporation and concentration of the liquid.
  • the absorbing solution can form an absorbent crystal in the absorbent crystallizer 141 and absorb the solution after crystallization.
  • the crystallization of the absorbent described in this embodiment and the following examples is not intended to limit it to only the absorbent crystal particles, but may also be an absorption solution containing the absorbent crystal particles.
  • the relationship between the absorber 14, the generator 11, the absorption solution from the heat exchanger 150 and the absorbent crystallizer 141 is as follows.
  • FIG. 3 is a flowchart of Embodiment 2 of the present invention.
  • the absorption solution is supplied from the heat exchanger 150 for heat exchange of the absorption solution from the absorber 14 with the absorbent (or the absorption solution containing the absorbent crystals) output from the absorbent crystallizer 141.
  • the absorption solution output line 20 of the generator 11 is connected to the absorption solution input line of the absorber, whereby the absorption solution output from the generator 11 is crystallized and mixed with the heat-treated absorbent, and is input into the absorber.
  • the post-crystallization absorption solution output from the absorbent crystallizer 141 is sent to the generator 11 through the absorption solution input pipe 30.
  • the heat-absorbed absorption solution from the absorber 14 is input to the absorbent crystallizer 141 for cooling crystallization and solid-liquid separation; the heat-treated absorbent crystals output from the absorbent crystallizer 141 are passed through the absorption solution input pipe. It is delivered to the absorber 14. Since the temperature of the absorbing solution from the absorber 14 is much higher than the temperature at which the absorbing agent is output from the absorbent crystallizer 141, the temperature of the absorbing solution entering the absorbent crystallizer 141 is greatly lowered after the heat exchange, so that the use can be reduced. The cooling capacity of the absorption solution is cooled.
  • the temperature of the crystallization of the absorbent from the absorbent crystallizer after heat exchange is greatly increased, and is transported to the absorber, absorbing the same amount of working fluid vapor, and releasing the heat of absorption at a higher working temperature, thereby It can increase the temperature of the external heating of the absorber and increase the heating grade, thereby improving energy efficiency.
  • FIG. 4 is a flowchart of Embodiment 3 of the present invention.
  • the crystallized solution output from the absorbent crystallizer 141 is also passed from the heat exchanger 150 via the absorption solution, and the absorption solution from the absorber 14 is crystallized with the absorbent output from the absorbent crystallizer 141 (or the absorption solution containing the absorbent crystals). And heat transfer while absorbing the solution after crystallization.
  • Absorption solution after crystallization after heat exchange The overabsorbent solution input conduit 30 is delivered to the generator 11.
  • the absorption solution output pipe 20 of the generator 11 is connected to the absorption solution input pipe of the absorber, whereby the absorption solution output from the generator 11 is crystallized and mixed with the heat-treated absorbent, and is input into the absorber.
  • the post-crystallization absorption solution output from the absorbent crystallizer 141 is sent to the generator 11 through the absorption solution input pipe 30.
  • the heat-absorbed absorption solution from the absorber 14 is input to the absorbent crystallizer 141 for cooling crystallization and solid-liquid separation; the heat-treated absorbent crystals output from the absorbent crystallizer 141 are passed through the absorption solution input pipe. It is delivered to the absorber 14.
  • the temperature of the absorbing solution from the absorber 14 is much higher than the temperature of the absorbing agent crystallized from the absorbent crystallizer 141 and the absorbing solution after crystallization, the temperature of the absorbing solution entering the absorbent crystallizer 141 is greatly lowered after heat exchange. Thereby, the amount of cooling for cooling the absorption solution can be reduced.
  • the temperature of the crystallization of the absorbent from the absorbent crystallizer after heat exchange is greatly increased, and is transported to the absorber, absorbing the same amount of working fluid vapor, and releasing the heat of absorption at a higher working temperature, thereby It can increase the temperature of the external heating of the absorber and increase the heating grade.
  • the temperature of the crystallization solution from the absorbent crystallizer is greatly increased, and is sent to the generator to evaporate the same working fluid vapor. This embodiment can reduce the heat consumed by the generator, thereby improving the energy. usage efficiency.
  • the absorption solution output line 20 of the generator 11 is connected to the absorption solution output line 30 of the absorber 14, and the connected node is located before the absorption solution from the heat exchanger 150.
  • the absorbing solution from the generator 11 is mixed with the absorbing solution from the absorbing unit 14 and then introduced into the absorbing solution from the heat exchanger 150, and is condensed with the absorbing agent output from the absorbent crystallizer 141, and the absorbing solution is simultaneously subjected to heat exchange.
  • the absorption solution is sent to the generator 11 through the absorption solution input pipe.
  • the heat-treated absorbent crystals are transported to the absorber 14 through the absorption solution input line.
  • the absorption solution from the generator 11 is mixed with the absorption solution from the absorber 14 to be cooled and crystallized, and the amount of the absorption solution of the cooled crystal is increased as compared with the above-described manner, so that more absorption solution after crystallization can be obtained. Thereby, the use efficiency of the absorbent crystallizer can be improved.
  • FIG. 6 is a flow chart of the evaporation system of Embodiment 5 of the present invention.
  • the evaporation system proposed in this embodiment is basically the same as the foregoing embodiment, except that it further includes a compression refrigeration cycle device for supplying a low temperature cooling amount to the absorbent crystallizer 141.
  • the compression refrigeration cycle apparatus includes an absorbent crystallization-evaporator 200, a compressor 210, an absorption solution heat exchange-condenser 220, a throttle valve 230, and a compression-type refrigerant refrigerant pipe 240.
  • the lithium bromide concentration of the absorption solution after the solid-liquid separation of the absorbent crystallizer 141 is lowered.
  • the crystallization solution i.e., the lithium bromide dilute solution, passes through the crystallization solution absorption pipe 50, and is introduced into the generator 11 through the absorption solution heat exchange-condenser 220 and the absorption solution from the heat exchanger 150.
  • the absorption solution containing the absorbent crystals after the solid-liquid separation of the absorbent crystallizer 141 is introduced into the mixer 142 through the pipe 40 through the absorption solution heat exchange-condenser 220 and the absorption solution from the heat exchanger 150.
  • the absorption solution from the heat exchanger 150 functions to exchange heat between the higher temperature absorption solution from the absorber 14 and the lower temperature crystallization absorption solution and the crystal containing solution from the absorbent crystallizer, thereby increasing the supply generator.
  • the solution temperature of 11 and mixer 142 is simultaneously lowered by the temperature of the absorption solution supplied to the absorbent crystallizer.
  • the absorption solution heat exchange-condenser 220 functions to lower the temperature of the compression refrigeration refrigerant vapor at the outlet of the compression refrigeration cycle subsystem compressor 210 and the lower temperature crystallization absorption solution at the outlet of the absorbent crystallizer 141.
  • the heat is exchanged with the absorption solution containing the crystallization of the absorbent to condense the vapor of the above-mentioned refrigerant, and at the same time partially or completely melt the crystal of lithium halide and increase the temperature of the solution.
  • concentration of the generator 11 the generator of the lithium bromide concentration is increased.
  • the outlet absorption solution is introduced into the mixer 142 through the absorption solution pipe 20 and mixed with the absorption solution containing the absorbent crystals, and then introduced into the absorber 14 together. .
  • the present invention can separately set and optimize the working concentration of the absorption solution of the absorber 14 and the generator 11.
  • the present invention can achieve a process condition that is very beneficial for the absorption heat pump cycle, that is, while the absorber is operated at a high lithium bromide concentration, the generator operates at a lower concentration of lithium bromide than the absorber. This is difficult to achieve with conventional absorption heat pump cycles. Since the absorbent crystallizer 141 is provided, and the heat generated by the absorber 14 is directly supplied to the generator 11 through the thermal cycle, the externally driven heat source for supplying heat to the generator 11 in the existing absorption heat pump cycle can be substantially omitted. An absorption heat pump cycle in which the driving heat source is substantially self-supplied is realized, and the generator 11 supplies steam to the outside to supply heat to the heater 310 of the evaporation device.
  • the evaporation apparatus of this embodiment is the same as the evaporation apparatus of the first embodiment.
  • the evaporation device of the embodiment can concentrate the liquid of the milk, the plant extract, the ethanol fermentation liquid distillation bottom substrate, the chemical raw material, etc., without substantially driving the heat source. Achieve low-energy seawater desalination.
  • the embodiment of the present invention may be provided as a plurality of evaporation devices, and each evaporation device is preceded by evaporation.
  • the gas-liquid separator of the device is connected to the heater of the next evaporation device; the heater of the first evaporation device is connected to the generator of the heating device through the vapor passage, receives the steam generated by the heating device; the gas of the last evaporation device
  • the liquid separator is coupled to the absorber of the heating device to provide spent steam to the absorber; thereby forming a multi-effect evaporation system.
  • Embodiment 6 of the present invention proposes an evaporation concentration method for concentrating a water-based solvent solution using the evaporation system described in the embodiment, the evaporation concentration method comprising the following steps:
  • the heater 310 exchanges heat with the evaporation device 320 to evaporate water in the liquid in the evaporation device 320 into a vapor to concentrate the liquid;
  • the absorption solution outputted by the absorber exchanges heat with the post-crystallization absorption solution before the crystallization solution is transported to the generator after the crystallization, and the absorption solution output from the absorber is cooled.
  • the absorbent crystals exchange heat with the absorption solution output by the absorber before the absorption of the absorbent crystals to the absorber and before the absorption of the absorber output is cooled.
  • the absorption solution is transferred to the generator, and the absorbent is crystallized.
  • the absorption solution outputted by the absorber exchanges heat with the absorption and crystallization solution of the absorbent.
  • the absorption solution output by the generator is sent to the absorber.
  • the absorption solution outputted by the generator is mixed with the absorption solution output from the absorber to form a mixed absorption solution, and the mixed absorption solution is subjected to heat exchange with the absorbent after crystallization and crystallization.
  • the absorption of the absorbing solution output from the absorber 14 and the crystallization of the absorbing solution and the absorbing agent (or the absorbing solution containing the absorbing agent) output from the absorbent crystallizer 141 are performed, thereby maintaining the lower generator absorbing solution lithium bromide.
  • the working concentration of lithium bromide absorbed by the absorber 14 can be significantly increased, so that a higher temperature absorption heat can be obtained in the absorber 14, so that the heat of absorption can be used as the driving heat of the generator 11 and occurs.
  • the operating temperature of the device 11 is higher, that is, it is capable of generating a superheated vapor having a higher temperature.
  • the thermal compensation is performed during the above thermal cycle, i.e., an external heat source heating device 160 is provided to compensate for a small amount of heat shortage of the generator due to heat loss, etc., thereby ensuring the continuous progress of the entire heating process. Together, it constitutes a liquid evaporation and concentration method.
  • Embodiment 7 of the present invention provides another evaporation concentration method which is substantially the same as that of Embodiment 6, except that the low-temperature cooling amount required for the crystallization of the absorption solution in the absorbent crystallizer 141 comes from the compression type.
  • Refrigeration cycle process Specifically, the vapor of the refrigerant crystallization-evaporator 200 exiting the compressed refrigerant is compressed by the compressor 210 and then enters the absorption solution heat exchange-condenser 220 for condensation, and the condensed compressed refrigerant is passed through the throttle valve 230. Evaporation is carried out in the absorbent crystallization-evaporator 200 to complete the compression refrigeration cycle.
  • the cooling refrigerant of the embodiment is condensed in the absorption solution heat exchanger-condenser 220 from the cooling capacity of the outlet solution of the lithium bromide crystallizer 141, the evaporation temperature and the condensation temperature of the cycle are relatively close, thereby A higher coefficient of refrigeration performance can be achieved. That is, the compression refrigeration cycle of the present embodiment consumes less energy.
  • the temperature of the cooled crystallization provided by the absorption refrigeration process during the compression refrigeration cycle is - 18 to 7 °C.
  • the technical solution described in the above embodiments of the present invention has no special type of absorption solution used.
  • the above examples are exemplified by water-lithium bromide as the absorbing solution of the working medium.
  • the working medium may be one or more of water, sterol and ethanol.
  • the mixture; the absorbent is one of or a mixture of LiBr, LiCl, LiN0 3 , NaBr, KBr, CaCl 2 , MgBr 2 and ZnC 1 2 .
  • This example was carried out by seawater desalination using the method described in Example 6.
  • the seawater has a water content (mass percentage) of about 96%.
  • the saturated steam at 165 °C is used as an external heat source to heat the working fluid in the thermal circuit to compensate for the insufficient heat of the generator-driven heat source due to heat loss.
  • the dimercaptosilicone oil is used as the thermal cycle working medium, and the cooling water of 20 ° C is used to cool the absorbent crystallizer 141, and the water content (mass percentage) of the brine obtained is 90%, and the energy of the heating device is
  • the efficiency (COP) is 1.00, and the heat production rate per p ⁇ fresh water is about 270 MJ.
  • the energy efficiency COP of the heating device of this example is calculated as follows:
  • Example 6 the method described in Example 6 is used to evaporate the concentrated milk.
  • the water content (mass percentage) of the raw milk is 88%, and the working medium in the thermal cycle is heated by using 210 ° C saturated steam as an external heat source.
  • the dimercaptosilicone oil is used as the thermal cycle working medium, and the cooling crystal water of the absorbent crystallizer 141 is cooled by the cooling water of 60 ° C to obtain the water of the concentrated milk.
  • the content (weight percent) is 60%, and the energy efficiency (COP) of the heating device is 10.0.
  • Example 7 the method described in Example 7 is used to evaporate the concentrated milk.
  • the water content (mass percentage) of the raw milk is: 88%
  • the working medium in the thermal cycle is heated by using 200 ° C saturated steam as an external heat source.
  • di-n-based silicone oil as the thermal cycle working fluid
  • TC compression refrigerant to cool the absorbent crystal 5 ⁇
  • the energy content (COP) of the heating device is 6.5.
  • the calculation formula of this example COP is as follows:
  • the COP-output heat / (the amount of heat input to the external heat source + the power consumption of the compressor X 3.0)
  • the primary energy generation efficiency of the grid customer terminal that supplies the compressor is 33.3%.
  • Example 7 the method described in Example 7 is used to evaporate and concentrate the plant extract, the water content (mass percentage) of the raw material is 95%, and the working fluid in the thermal cycle is heated by using 130 ° C saturated steam as an external heat source. Compensating for the insufficient heat of the generator-driven heat source caused by heat loss, etc., using dimercaptosilicone oil as the thermal cycle working fluid, and using the compression refrigeration cycle provided by the compression refrigeration cycle to cool the absorbent crystal 141.
  • the obtained plant extract concentrate had a water content of 70% and the heating device had an energy efficiency (COP) of 5.9.
  • the COP output heat / (the amount of heat input to the external heat source + the power consumption of the compressor X 3.0)
  • the primary energy generation efficiency of the grid customer terminal that supplies the compressor is 33.3%.
  • Table 1 below shows the operating parameters and performance of the above examples 1 ⁇ 4.
  • the evaporation system and the evaporation concentration method of the present invention since the heating device has an absorbent crystallizer, and the heat generated by the absorber is directly supplied to the generator as a heat source of the generator through the heat circulation circuit, thereby saving in the heating device
  • the external driving heat source required for the absorption heating cycle realizes an absorption heating cycle in which the driving heat source is substantially self-supply, and the heat energy is sent to the evaporation device through the vapor for the evaporation concentration process, so that the entire evaporation system basically does not require an external heat source. It effectively saves energy and water resources, making it more suitable for practical use.

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Crystallography & Structural Chemistry (AREA)
  • Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
  • Gas Separation By Absorption (AREA)

Abstract

An evaporating system and an evaporating-concentrating method using the system. The evaporating system comprises: a generator (11) for concentrating the absorbing solution and generating vapor; an absorber (14) for generating heat, a heat circulating loop being set between the generator (11) and the absorber (14) for transferring the heat generated from the absorber (14) to the generator (11); an absorbent crystallizer (141) having the inlet of absorbent solution, the outlet of after-crystallization absorbent solution, and the outlet of crystal, the inlet of absorbent solution of the absorbent crystallizer (141) being connected to the outletof absorbent solution of the absorber (14), the outlet of after-crystallization absorbent solution of the absorbent crystallizer (141) being connected to the inlet of absorbent solution of the generator (11), the outlet of crystal of the absorbent crystallizer (141) being connected with the inlet of absorbent solution of the absorber (14); a heater (310) for receiving the vapor generated by the generator (11); an evaporating device (320) for heat-exchanging with the heater (310); a gas-liquid separator (330).

Description

蒸发系统以及蒸发浓缩方法 技术领域  Evaporation system and evaporation concentration method
本发明涉及一种化工、 食品工业、 制药、 水处理和海水淡化等领域的 蒸发技术， 特别涉及一种在基本无外部驱动热源条件下进行蒸发的吸收式 蒸发系统以及蒸发浓缩方法。 背景技术  The present invention relates to an evaporation technique in the fields of chemical industry, food industry, pharmaceuticals, water treatment and seawater desalination, and more particularly to an absorption evaporation system and an evaporation concentration method for evaporation under substantially no externally driven heat source. Background technique
请参阅图 1所示， 是现有的蒸发系统的流程图。 其由蒸汽发生器 400、 蒸汽喷射泵 440、 加热器 410、 蒸发设备 420以及气液分离器 430组成。 其 中的蒸汽发生器 400用于产生高温蒸汽， 通过蒸汽喷射泵 400供应到加热 器 410 中。 在蒸发设备 420 内， 料液从其顶部输入， 吸收来自加热器 410 的热量， 料液中的溶剂被加热蒸发， 浓缩后的料液以及蒸气从蒸发设备输 出后进入气液分离器 430 内。 经气液分离后， 浓缩料液从气液分离器的底 部输出， 乏蒸汽从气液分离器 430的顶部输出， 一部分引至蒸汽喷射泵 440 与来自蒸气发生器 400的生蒸汽混合后被输入到加热器 410。上述现有的蒸 发系统结构简单， 被广泛用于石油、 化工、 医药、 化肥、 造纸、 铝行业、 味精、 酿酒、 制糖等领域。  See Figure 1 for a flow chart of the existing evaporation system. It consists of a steam generator 400, a steam jet pump 440, a heater 410, an evaporation device 420, and a gas-liquid separator 430. The steam generator 400 therein is used to generate high temperature steam, which is supplied to the heater 410 through the steam jet pump 400. In the evaporation device 420, the feed liquid is input from the top thereof, absorbs heat from the heater 410, the solvent in the feed liquid is heated and evaporated, and the concentrated feed liquid and vapor are discharged from the evaporation device into the gas-liquid separator 430. After the gas-liquid separation, the concentrated feed liquid is discharged from the bottom of the gas-liquid separator, the spent steam is output from the top of the gas-liquid separator 430, and a part is led to the steam jet pump 440 which is mixed with the raw steam from the steam generator 400 and then input. To the heater 410. The above existing evaporation system has a simple structure and is widely used in the fields of petroleum, chemical, pharmaceutical, fertilizer, paper, aluminum, monosodium glutamate, brewing, sugar, and the like.
但是， 现有蒸发系统中的蒸汽发生器必须采用外部能量来产生蒸汽， 因而能量效率较低， 此外， 当所排乏蒸汽的冷凝热采用冷却塔向外排放时， 还需消耗大量的水资源。 发明内容  However, the steam generator in the existing evaporation system must use external energy to generate steam, so the energy efficiency is low. In addition, when the condensed heat of the exhausted steam is discharged to the outside of the cooling tower, a large amount of water is consumed. Summary of the invention
本发明的主要目的在于克服现有的蒸发系统存在的问题， 而提供一种 蒸发系统以及蒸发浓缩方法，所要解决的技术问题是使其能够在基本无外 部驱动热源的条件下进行料液蒸发， 实现料液的浓缩， 从而显著提高蒸发 系统的能量效率， 同时节约水资源， 因而更加适于实用。  The main object of the present invention is to overcome the problems of the prior art evaporation system, and to provide an evaporation system and an evaporation concentration method, the technical problem to be solved is to enable the liquid evaporation of the material without substantially driving the external heat source. Concentration of the feed liquid, thereby significantly improving the energy efficiency of the evaporation system, while conserving water resources, is therefore more suitable for practical use.
本发明的目的及解决其技术问题是采用以下技术方案来实现的。 依据 本发明提出的一种蒸发系统， 其包括供热装置和蒸发装置， 所述的供热装 置包括： 发生器， 其内设有换热器， 用于浓缩吸收溶液并产生蒸气； 内设 有换热器的吸收器， 用于产生热量， 该吸收器的换热器与发生器的换热器 相连接， 形成热循环回路，用于将吸收器中产生的热量输送至发生器中；及 吸收剂结晶器， 接收来自吸收器和 /或发生器的吸收溶液并进行冷却， 形成 吸收剂结晶和结晶后吸收溶液， 所述的结晶后溶液输送至发生器， 所述的 吸收剂结晶输送至吸收器； The object of the present invention and solving the technical problems thereof are achieved by the following technical solutions. An evaporation system according to the present invention includes a heating device and an evaporation device, the heating device comprising: a generator having a heat exchanger therein for concentrating the absorption solution and generating a vapor; An absorber of a heat exchanger for generating heat, a heat exchanger of the absorber and a heat exchanger of the generator Connected to form a thermal cycle loop for delivering heat generated in the absorber to the generator; and an absorbent crystallizer that receives the absorption solution from the absorber and/or generator and cools to form absorbent crystals and After crystallization, the solution is absorbed, the crystallization solution is sent to the generator, and the absorbent is crystallized and sent to the absorber;
所述的蒸发装置包括： 加热器，通过蒸气通路与上述的供热装置相连 接，接收供热装置产生的蒸气； 蒸发设备， 与所述的加热器进行换热； 及气 液分离器， 连接于蒸发设备， 并通过另一蒸气通道连接于供热装置， 向供 热装置提供乏蒸汽。  The evaporation device comprises: a heater connected to the heating device via a vapor passage, receiving steam generated by the heating device; an evaporation device, performing heat exchange with the heater; and a gas-liquid separator, connecting The evaporation device is connected to the heating device through another vapor passage to supply the steam to the heating device.
本发明的目的及解决其技术问题还可采用以下技术措施进一步实现。 优选的， 前述的蒸发系统， 还包括： 吸收溶液自换热器， 用于所述的 来自发生器的吸收溶液和 /或来自吸收器的吸收溶液， 与结晶后吸收溶液和 /或吸收剂结晶或者含吸收剂结晶的吸收溶液进行换热。  The object of the present invention and solving the technical problems thereof can be further achieved by the following technical measures. Preferably, the foregoing evaporation system further comprises: an absorption solution from the heat exchanger, the absorption solution from the generator and/or the absorption solution from the absorber, and the crystallization of the absorption solution and/or the absorbent after crystallization. Or an absorption solution containing an crystallization of an absorbent for heat exchange.
优选的， 前述的蒸发系统， 还包括： 吸收溶液自换热器， 用于将来自 吸收器的吸收溶液与来自吸收剂结晶器的结晶后吸收溶液进行换热。  Preferably, the foregoing evaporation system further comprises: an absorption solution from the heat exchanger for exchanging heat between the absorption solution from the absorber and the post-crystallization absorption solution from the absorbent crystallizer.
优选的， 前述的蒸发系统， 还包括： 吸收溶液自换热器， 用于将来自 吸收器的吸收溶液与来自吸收剂结晶器的吸收剂结晶或者含吸收剂结晶的 吸收溶液进行换热。  Preferably, the foregoing evaporation system further comprises: an absorption solution from the heat exchanger for exchanging heat from the absorption solution from the absorber with the absorption crystal of the absorbent from the absorbent crystallizer or the absorption solution containing the absorbent.
优选的， 前述的蒸发系统， 还包括： 吸收溶液自换热器， 用于将来自 吸收器的吸收溶液与来自吸收剂结晶器的结晶后吸收溶液和吸收剂结晶或 者含吸收剂结晶的吸收溶液进行换热。  Preferably, the foregoing evaporation system further comprises: an absorption solution from the heat exchanger for crystallization of the absorption solution from the absorber with the crystallization solution and the absorbent from the absorbent crystallizer or the absorption solution containing the absorbent crystals. Perform heat exchange.
优选的， 前述的蒸发系统， 来自发生器的吸收溶液和来自吸收器的吸 收溶液混合后进入吸收溶液自换热器， 与来自吸收剂结晶器的吸收溶液和 吸收剂结晶或者含吸收剂结晶的吸收溶液进行换热。  Preferably, in the foregoing evaporation system, the absorption solution from the generator and the absorption solution from the absorber are mixed into the absorption solution from the heat exchanger, and the absorption solution and the absorbent from the absorbent crystallizer are crystallized or crystallized with the absorbent. The solution is absorbed for heat exchange.
优选的， 前述的蒸发系统， 其中所述的热循环回路上设有外部热源加 热装置， 用于补偿由于散热损失等引起的发生器热量的不足部分。  Preferably, in the foregoing evaporation system, wherein the thermal cycle is provided with an external heat source heating device for compensating for insufficient heat of the generator due to heat loss or the like.
优选的， 前述的蒸发系统， 其中所述的蒸发装置为多个， 各蒸发装置 间， 前一个蒸发装置的气液分离器连接于下一个蒸发装置的加热器； 第一 个蒸发装置的加热器通过蒸气通路连接于供热装置的发生器， 接收供热装 置产生的蒸气； 最后一个蒸发装置的气液分离器连接于供热装置的吸收器， 向供热装置提供乏蒸汽。 优选的， 前述的蒸发系统， 其还包括由吸收剂结晶-蒸发器、 压缩机、 吸收溶液换热-冷凝器、 节流阀以及压缩式制冷工质管道构成的压缩式制冷 装置， 用于向上述吸收剂结晶器提供冷量。 Preferably, in the foregoing evaporation system, wherein the plurality of evaporation devices are plural, and between the evaporation devices, the gas-liquid separator of the previous evaporation device is connected to the heater of the next evaporation device; the heater of the first evaporation device The generator connected to the heating device through the vapor passage receives the steam generated by the heating device; the gas-liquid separator of the last evaporation device is connected to the absorber of the heating device to supply the steam to the heating device. Preferably, the foregoing evaporation system further comprises a compression refrigeration device comprising an absorbent crystallization-evaporator, a compressor, an absorption solution heat exchange-condenser, a throttle valve, and a compression refrigeration refrigerant pipe, The above absorbent crystallizer provides a cooling capacity.
本发明的目的及解决其技术问题是采用以下技术方案来实现的。 依据 本发明提出的一种蒸发浓缩方法， 采用上述的蒸发装置， 其包括以下步骤： The object of the present invention and solving the technical problems thereof are achieved by the following technical solutions. According to an evaporation concentration method proposed by the present invention, the above evaporation apparatus is employed, which comprises the following steps:
( 1 )在发生器中浓缩吸收溶液同时产生蒸气， 并将上述蒸气输送到加 热器， 吸收溶液输送至吸收器中； (1) concentrating the absorption solution in the generator while generating a vapor, and delivering the vapor to the heater, and the absorption solution is delivered to the absorber;
( 2 )加热器与蒸发设备进行换热， 使蒸发设备中的料液蒸发浓缩； (2) heat exchange between the heater and the evaporation device to evaporate and concentrate the liquid in the evaporation device;
( 3 )蒸发设备中的浓缩料液和蒸气输入到气液分离器中进行气液分离；(3) The concentrated liquid and vapor in the evaporation device are input into the gas-liquid separator for gas-liquid separation;
( 4 ) 经气液分离后的蒸气输送到吸收器中， 来自发生器的吸收溶液吸 收所述蒸气并产生吸收热， 同时吸收溶液浓度降低并被输送至吸收剂结晶 器中； (4) The vapor separated by the gas-liquid separation is sent to the absorber, and the absorption solution from the generator absorbs the vapor and generates absorption heat, while the concentration of the absorption solution is lowered and sent to the absorbent crystallizer;
( 5 )在吸收剂结晶器中进行吸收溶液冷却结晶和固液分离， 形成吸收 剂结晶和结晶后吸收溶液， 固液分离后的结晶后吸收溶液输送至发生器中， 而吸收剂结晶或含吸收剂结晶的吸收溶液输送至吸收器中；  (5) performing absorption crystallization and solid-liquid separation in an absorbent crystallizer to form an absorbent crystallization and crystallization solution, and the absorbing solution after solid-liquid separation is transported to the generator, and the absorbent is crystallized or contained. The absorption solution of the crystallization of the absorbent is delivered to the absorber;
( 6 )在吸收器和发生器之间进行热循环， 将吸收溶液在吸收器中吸收 蒸气时产生的吸收热输送至发生器中。  (6) Thermal cycling between the absorber and the generator, the absorption heat generated when the absorption solution absorbs the vapor in the absorber is delivered to the generator.
本发明的目的及解决其技术问题还可采用以下技术措施进一步实现。 优选的， 前述的蒸发浓缩方法， 还包括： 在所述的结晶后吸收溶液输 送到发生器之前， 且吸收器输出的吸收溶液进行冷却之前， 所述的吸收器 输出的吸收溶液与所述的结晶后吸收溶液进行换热。  The object of the present invention and solving the technical problems thereof can be further achieved by the following technical measures. Preferably, the foregoing evaporation concentration method further comprises: after the crystallization solution is transported to the generator after the crystallization, and the absorption solution output by the absorber is cooled, the absorption solution output by the absorber is After crystallization, the solution is absorbed for heat exchange.
优选的， 前述的蒸发浓缩方法， 还包括： 在所述的吸收剂结晶输送到 吸收器之前， 且吸收器输出的吸收溶液进行冷却之前， 所述的吸收剂结晶 或者含吸收剂结晶的吸收溶液与所述的吸收器输出的吸收溶液进行换热。  Preferably, the foregoing evaporation concentration method further comprises: crystallization of the absorbent or an absorption solution containing an absorbent crystal before the absorption agent is crystallized and transported to the absorber, and before the absorption solution output from the absorber is cooled. The heat exchange is performed with the absorption solution output from the absorber.
优选的， 前述的蒸发浓缩方法， 还包括： 在所述的结晶后吸收溶液输 送到发生器之前， 吸收剂结晶输送到吸收器之前， 且吸收器输出的吸收溶 液进行冷却之前， 所述吸收器输出的吸收溶液与所述的结晶后吸收溶液和 吸收剂结晶或者含吸收剂结晶的吸收溶液进行换热。  Preferably, the foregoing evaporation concentration method further comprises: before the crystallization solution is transported to the generator after crystallization, before the crystallization of the absorbent is delivered to the absorber, and before the absorption solution of the absorber is cooled, the absorber The output absorption solution exchanges heat with the crystallizing absorption solution and the absorbent crystal or the absorption solution containing the absorbent crystal.
优选的， 前述的蒸发浓缩方法， 还包括： 在所述的结晶后吸收溶液输 送到发生器之前， 吸收剂结晶输送到吸收器之前， 吸收器输出的吸收溶液 进行冷却之前， 且所述发生器输出的吸收溶液输送到吸收器之前， 该发生 器输出的吸收溶液与所述吸收器输出的吸收溶液混合形成混合吸收溶液， 该混合吸收溶液与所述的结晶后吸收溶液和吸收剂结晶或者含吸收剂结晶 的吸收溶液进行换热。 Preferably, the foregoing evaporation concentration method further comprises: before the crystallization solution is transported to the generator after the crystallization, the absorption solution of the absorber is output before the absorption agent is crystallized and sent to the absorber. Before the cooling is performed, and the absorption solution outputted by the generator is sent to the absorber, the absorption solution outputted by the generator is mixed with the absorption solution outputted by the absorber to form a mixed absorption solution, and the mixed absorption solution and the crystal are The post-absorption solution and the absorbent crystals or the absorption solution containing the absorbent crystals are subjected to heat exchange.
优选的， 前述的蒸发浓缩方法， 在所述的步骤（6 ) 的热循环过程中， 通过外部热源补偿发生器热量的不足部分。  Preferably, in the foregoing evaporation concentration method, during the thermal cycle of the step (6), an insufficient portion of the heat of the generator is compensated by an external heat source.
优选的，前述的蒸发浓缩方法，通过压缩式制冷循环向上述的步骤（5 ) 提供吸收溶液冷却结晶所需的冷量。  Preferably, the aforementioned evaporation concentration method provides the cooling amount required for the absorption solution to cool the crystal by the compression refrigeration cycle to the above step (5).
优选的， 前述的蒸发浓缩方法， 所述的步骤（5 ) 中的吸收溶液冷却结 晶的温度为 -18 ~ 60°C。  Preferably, in the foregoing evaporation concentration method, the temperature of the crystallization solution in the step (5) is -18 to 60 ° C.
本发明与现有技术相比具有明显的优点和有益效果。 由以上技术方案 可知，本发明的蒸发系统以及蒸发浓缩方法， 由于其供热装置具有了吸收剂 结晶器，并且吸收器所产生的热量作为发生器热源通过热循环回路直接供 给发 i器， 因而可以在供热装置中省去吸收式制热循环所需的外部驱动热 源， 实现驱动热源基本自供的吸收式制热循环， 并将热能通过蒸气输送到 蒸发装置用于进行蒸发浓缩过程， 使整个蒸发系统基本无需外部热源， 有 效地节约了能源和水资源， 从而更加适于实用。  The present invention has significant advantages and advantageous effects over the prior art. It can be seen from the above technical solutions that the evaporation system and the evaporation concentration method of the present invention have an absorbent crystallizer because of the heat supply device, and the heat generated by the absorber is directly supplied to the generator through the thermal cycle as a heat source of the generator. The external driving heat source required for the absorption heating cycle can be omitted in the heating device, the absorption heating cycle that drives the heat source to be substantially self-supplied, and the heat energy can be sent to the evaporation device through the vapor for the evaporation concentration process, so that the whole The evaporation system basically eliminates the need for an external heat source, effectively conserving energy and water resources, making it more suitable for practical use.
上述说明仅是本发明技术方案的概述， 为了能够更清楚了解本发明的 技术手段， 并可依照说明书的内容予以实施， 以下以本发明的较佳实施例 并配合附图详细说明如后。 附图说明  The above description is only an overview of the technical solutions of the present invention, and the technical means of the present invention can be more clearly understood and implemented in accordance with the contents of the specification. Hereinafter, the preferred embodiments of the present invention will be described in detail with reference to the accompanying drawings. DRAWINGS
图 1是现有的蒸发系统的流程图。  Figure 1 is a flow chart of a prior art evaporation system.
图 2是本发明实施例 1的蒸发系统的流程图。  Fig. 2 is a flow chart showing the evaporation system of the first embodiment of the present invention.
图 3是本发明实施例 2的蒸发系统的流程图。  Figure 3 is a flow chart of the evaporation system of Embodiment 2 of the present invention.
图 4是本发明实施例 3的蒸发系统的流程图。  Figure 4 is a flow chart of the evaporation system of Embodiment 3 of the present invention.
图 5是本发明实施例 4的蒸发系统的流程图。  Figure 5 is a flow chart showing an evaporation system of Embodiment 4 of the present invention.
图 6是本发明实施例 5的蒸发系统的流程图。  Figure 6 is a flow chart showing an evaporation system of Embodiment 5 of the present invention.
11: 发生器 12: 冷凝器  11: Generator 12: Condenser
13: 蒸发器 14: 吸收器 17 : 冷凝水管道 18、 19 : 蒸气通路 13: Evaporator 14: Absorber 17 : Condensate pipe 18, 19 : Vapor path
20、 30: 吸收溶液管道 40: 结晶后吸收溶液管道  20, 30: absorption solution pipe 40: absorption solution pipe after crystallization
50: 含结晶溶液管道 60: 热循环工质管道  50: Pipe with crystallization solution 60: Thermal cycle refrigerant pipe
110、 120、 130、 140:换热器  110, 120, 130, 140: heat exchanger
141： 吸收剂结晶器 142 : 混合器  141: Absorbent crystallizer 142 : Mixer
150 吸收溶液自换热器 160 外部热源加热装置  150 absorption solution from heat exchanger 160 external heat source heating device
200 吸收剂结晶-蒸发器 210 压缩机  200 absorbent crystallization - evaporator 210 compressor
220 吸收溶液换热-冷凝器 230 节流阀  220 absorption solution heat transfer - condenser 230 throttle valve
240 压缩式制冷工质管道 301 : 料液输入管道  240 Compressed Refrigerant Pipeline 301 : Material Input Pipe
302 料液输出管道 303: 浓缩料输出管道  302 feed liquid output pipe 303: concentrate output pipe
310 加热器 320: 蒸发设备  310 Heater 320: Evaporation equipment
330 气液分离器 实现发明的最佳方式  330 gas-liquid separator The best way to achieve the invention
为更进一步阐述本发明为达成预定发明目的所采取的技术手段及功 效，以下结合附图及较佳实施例， 对依据本发明提出的蒸发系统其具体实施 方式、 结构、 特征及其功效， 详细说明如后。  In order to further illustrate the technical means and efficacy of the present invention for achieving the intended purpose of the invention, the specific embodiments, structures, features and functions of the evaporation system according to the present invention will be described in detail below with reference to the accompanying drawings and preferred embodiments. The description is as follows.
请参阅图 2所示， 是本发明实施例 1的蒸发系统的流程图。 该蒸发系 统主要包括供热装置和蒸发装置， 其中所述的供热装置包括： 发生器 11、 吸收器 14、 吸收溶液自换热器 150、 吸收剂结晶器 141和混合器 142。 发生 器 11和吸收器 14之间循环有水-渙化锂工质对作为吸收溶液。 发生器 11 用于浓缩吸收溶液并产生过热蒸气， 其内设有换热器 110 , 在该换热器 110 通入来自吸收器 14中的换热器 140的热循环工质， 对作为吸收溶液的渙化 锂溶液进行加热使水蒸发， 从而使吸收溶液的吸收剂浓度提高，其所产生的 高温过热蒸气通过蒸气通路 19输出至蒸发装置。 发生器 11 出口吸收溶液 通过吸收溶液管道 20进入到吸收器 14内， 而吸收器 14出口吸收溶液通过 吸收溶液管道 30进入到发生器 11内。 通过吸收溶液管道 20、 30使吸收溶 液在发生器 11和吸收器 14之间循环。 所述的吸收器 14接收来自蒸发装置 的乏蒸汽， 吸收器 14内设有换热器 140,在吸收器 14中， 来自发生器 11的 高浓度的吸收溶液吸收来自蒸发装置的乏蒸汽并产生吸收热，从而提高换 热器 140中的热循环工质的温度。该换热器 140与发生器 11中的换热器 110 由热循环工质管道 60相连形成热循环回路，以便使吸收器 14产生的吸收热 作为发生器的驱动热源供应给发生器 11。 本实施例中， 热循环回路为热管 循环回路， 此时， 发生器 11的安装位置高于吸收器 14的安装位置。 所述 的热管循环， 热管中工质无需外界驱动力即可通过冷凝 -蒸发过程形成对 流， 从而在发生器和吸收器之间循环并传递热量。 在热循环回路上设置有 外部热源加热装置 160 ,用于补偿由于散热损失等引起的发生器热量的不足 部分。 所述的吸收溶液自换热器 150、吸收剂结晶器 141和混合器 142设置 于吸收器 14和发生器 11之间。 该吸收剂结晶器 141具有吸收溶液入口、 吸收溶液出口和结晶输出口。 该吸收剂结晶器 141 的吸收溶液入口经吸收 溶液自换热器 150连接于吸收器 14的吸收溶液出口 , 该吸收剂结晶器的吸 收溶液出口经吸收溶液自换热器 150连接于发生器 11的吸收溶液入口， 该 吸收剂结晶器的结晶输出口连接于吸收器 11的吸收溶液入口。 在有混合器 142的情况下， 上述的结晶输出口经混合器 142后连接于吸收器 11的吸收 溶液入口。 发生器 11 出口吸收溶液通过吸收溶液管道 20经混合器 142进 入到吸收器 14， 而吸收器 14 出口吸收溶液通过吸收溶液管道 30， 经吸收 溶液自换热器 150进入到吸收剂结晶器 141。在吸收剂结晶器 141中采用低 温冷量对吸收溶液进行冷却结晶， 由于溴化锂水溶液达到渙化锂的结晶温 度时会出现结晶， 结晶温度越低液相的溴化锂平衡浓度就越低，因此， 通过 冷却结晶， 无论冷却结晶前的吸收溶液溴化锂浓度有多高， 结晶后液相的 溴化锂浓度可达到或接近冷却温度下的溴化锂平衡浓度。 结晶并进行固液 分离后，吸收剂结晶器 141中的结晶后吸收溶液即溴化锂稀溶液经吸收溶液 自换热器 150由吸收溶液管道 30输送到发生器 11中。 上述的吸收剂结晶 器 141所采用的冷源可以为 15 ~ 60 °C的水。 Referring to FIG. 2, it is a flow chart of the evaporation system of Embodiment 1 of the present invention. The evaporation system mainly includes a heating device and an evaporation device, wherein the heating device includes: a generator 11, an absorber 14, an absorption solution from the heat exchanger 150, an absorbent crystallizer 141, and a mixer 142. A pair of water-deuterated lithium working fluid is circulated between the generator 11 and the absorber 14 as an absorbing solution. The generator 11 is for concentrating the absorbing solution and generating superheated steam, and is provided therein with a heat exchanger 110, in which the heat circulating medium from the heat exchanger 140 in the absorber 14 is passed, and the pair is used as an absorbing solution. The lithium telluride solution is heated to evaporate the water, so that the concentration of the absorbent of the absorbing solution is increased, and the high-temperature superheated vapor generated by the bismuth telluride is output to the evaporation device through the vapor passage 19. The generator 11 outlet absorption solution enters the absorber 14 through the absorption solution conduit 20, and the absorber 14 outlet absorption solution enters the generator 11 through the absorption solution conduit 30. The absorption solution is circulated between the generator 11 and the absorber 14 by the absorption solution conduits 20, 30. The absorber 14 receives spent steam from the evaporation device, and the absorber 14 is provided with a heat exchanger 140. In the absorber 14, the high concentration absorption solution from the generator 11 absorbs the spent steam from the evaporation device and generates The heat is absorbed to increase the temperature of the thermal cycle medium in the heat exchanger 140. The heat exchanger 140 and the heat exchanger 110 in the generator 11 A thermal cycle is formed by the thermal cycle medium conduit 60 so that the heat of absorption generated by the absorber 14 is supplied to the generator 11 as a driving heat source for the generator. In this embodiment, the thermal cycle is a heat pipe circulation circuit. At this time, the installation position of the generator 11 is higher than the installation position of the absorber 14. The heat pipe circulates, and the working medium in the heat pipe can form convection through the condensation-evaporation process without external driving force, thereby circulating and transferring heat between the generator and the absorber. An external heat source heating device 160 is disposed on the thermal cycle to compensate for insufficient heat of the generator due to heat loss or the like. The absorption solution is disposed between the absorber 14 and the generator 11 from the heat exchanger 150, the absorbent crystallizer 141, and the mixer 142. The absorbent crystallizer 141 has an absorption solution inlet, an absorption solution outlet, and a crystallization outlet. The absorption solution inlet of the absorbent crystallizer 141 is connected to the absorption solution outlet of the absorber 14 via the absorption solution from the heat exchanger 150, and the absorption solution outlet of the absorbent crystallizer is connected to the generator 11 from the heat exchanger 150 via the absorption solution. The absorption solution inlet of the absorbent crystallizer is connected to the absorption solution inlet of the absorber 11. In the case of a mixer 142, the crystallization outlet described above is connected to the absorbing solution inlet of the absorber 11 via the mixer 142. The generator 11 outlet absorbing solution enters the absorber 14 through the absorbing solution conduit 20 via the mixer 142, and the absorber 14 outlet absorbing solution passes through the absorbing solution conduit 30 through the absorbing solution from the heat exchanger 150 to the absorbent crystallizer 141. In the absorbent crystallizer 141, the absorption solution is cooled and crystallized by using a low-temperature cooling amount, and crystallization occurs when the lithium bromide aqueous solution reaches the crystallization temperature of the lithium niobate. The lower the crystallization temperature, the lower the equilibrium concentration of the lithium bromide in the liquid phase, and therefore, Cooling crystallization, no matter how high the concentration of lithium bromide in the absorption solution before cooling and crystallization, the lithium bromide concentration of the liquid phase after crystallization can reach or approach the equilibrium concentration of lithium bromide at the cooling temperature. After crystallization and solid-liquid separation, the crystallization absorption solution in the absorbent crystallizer 141, that is, the lithium bromide solution, is sent from the heat exchanger 150 to the generator 11 through the absorption solution pipe 30 through the absorption solution. The above-mentioned absorbent crystallizer 141 may use a cold source of 15 to 60 ° C.
上述的蒸发装置， 用于将料液中的水分蒸发进行浓缩， 其包括加热器 310、 蒸发设备 320和气液分离器 330， 所述的加热器 310通过蒸气通路 19 连接于发生器 11 ,接收发生器 11产生的过热蒸气； 加热器 310和蒸发设备 320具有良好的热交换效率，从而可以将蒸气的热量传导至蒸发设备 320内 的料液， 蒸发设备 320具有料液输入管道 301和料液输出管道 302; 所述的 气液分离器 330通过料液输出管道 302连接于蒸发设备 320; 气液分离器 330通过蒸气通路 18连接于供热装置的吸收器 14， 用于向吸收器 14提供 乏蒸汽。 气液分离器 330底部设有浓缩液输出口 303, 用于将浓缩后的料液 输出。 加热器 310底部设有冷凝水输出口， 用于输出从物料蒸发出来的水。 The above evaporation device is configured to evaporate water in the liquid to be concentrated, and includes a heater 310, an evaporation device 320, and a gas-liquid separator 330. The heater 310 is connected to the generator 11 through the vapor passage 19, and the receiving occurs. The superheated vapor generated by the device 11; the heater 310 and the evaporation device 320 have good heat exchange efficiency, so that the heat of the vapor can be conducted to the liquid in the evaporation device 320, and the evaporation device 320 has the liquid input pipe 301 and the liquid output. The gas-liquid separator 330 is connected to the evaporation device 320 through the liquid-liquid output pipe 302; the gas-liquid separator 330 is connected to the absorber 14 of the heating device through the vapor passage 18 for providing the absorber 14 Lack of steam. A concentrated liquid outlet 303 is provided at the bottom of the gas-liquid separator 330 for outputting the concentrated liquid. A condensate outlet is provided at the bottom of the heater 310 for outputting water evaporated from the material.
较佳的， 在发生器 11和吸收器 14之间的热循环回路上设置有外部热 源加热装置 160， 用于补偿由于散热损失等引起的发生器热量的不足部分。  Preferably, an external heat source heating means 160 is provided on the thermal circuit between the generator 11 and the absorber 14 for compensating for insufficient heat of the generator due to heat loss or the like.
本实施例 1 的蒸发系统除必要的动力设备外， 基本不需要提供专门的 驱动热源即可进行料液的蒸发浓缩。  In addition to the necessary power equipment, the evaporation system of the first embodiment basically does not need to provide a special driving heat source to carry out evaporation and concentration of the liquid.
吸收溶液在吸收剂结晶器 141 中可以形成吸收剂结晶和结晶后吸收溶 液。 本实施例以及下述实施例中所述的吸收剂结晶不用于限定其仅仅为吸 收剂结晶颗粒， 其还可以是含有吸收剂结晶颗粒的吸收溶液。 吸收器 14、 发生器 11、 吸收溶液自换热器 150和吸收剂结晶器 141之间的关系还有如 下方式。  The absorbing solution can form an absorbent crystal in the absorbent crystallizer 141 and absorb the solution after crystallization. The crystallization of the absorbent described in this embodiment and the following examples is not intended to limit it to only the absorbent crystal particles, but may also be an absorption solution containing the absorbent crystal particles. The relationship between the absorber 14, the generator 11, the absorption solution from the heat exchanger 150 and the absorbent crystallizer 141 is as follows.
请参阅图 3所示， 是本发明实施例 2的流程图。 所述的吸收溶液自换 热器 150, 用于使来自吸收器 14的吸收溶液与从吸收剂结晶器 141输出的 吸收剂结晶 （或者含吸收剂结晶的吸收溶液）进行换热。 发生器 11的吸收 溶液输出管道 20与吸收器的吸收溶液输入管道相连， 从而将发生器 11输 出的吸收溶液与经过换热后的吸收剂结晶混合后共同输入到吸收器中。 从 吸收剂结晶器 141输出的结晶后吸收溶液经吸收溶液输入管道 30输送到发 生器 11 内。 经过换热后的来自吸收器 14的吸收溶液输入到吸收剂结晶器 141中进行冷却结晶和固液分离；经过换热后的从吸收剂结晶器 141输出的 吸收剂结晶经吸收溶液输入管道被输送至吸收器 14中。由于来自吸收器 14 的吸收溶液的温度远高于从吸收剂结晶器 141 输出的吸收剂结晶的温度， 所以经过换热后， 进入吸收剂结晶器 141 的吸收溶液温度大大降低， 从而 可以减少用于冷却吸收溶液的冷量。 同时， 经过换热后的来自吸收剂结晶 器的吸收剂结晶的温度大大提高， 其被输送到吸收器中， 吸收同样量的工 质蒸汽， 可以在更高的工作温度下释放吸收热， 从而可以提高吸收器向外 供热的温度， 提高供热品位， 从而提高能源利用效率。  Please refer to FIG. 3, which is a flowchart of Embodiment 2 of the present invention. The absorption solution is supplied from the heat exchanger 150 for heat exchange of the absorption solution from the absorber 14 with the absorbent (or the absorption solution containing the absorbent crystals) output from the absorbent crystallizer 141. The absorption solution output line 20 of the generator 11 is connected to the absorption solution input line of the absorber, whereby the absorption solution output from the generator 11 is crystallized and mixed with the heat-treated absorbent, and is input into the absorber. The post-crystallization absorption solution output from the absorbent crystallizer 141 is sent to the generator 11 through the absorption solution input pipe 30. The heat-absorbed absorption solution from the absorber 14 is input to the absorbent crystallizer 141 for cooling crystallization and solid-liquid separation; the heat-treated absorbent crystals output from the absorbent crystallizer 141 are passed through the absorption solution input pipe. It is delivered to the absorber 14. Since the temperature of the absorbing solution from the absorber 14 is much higher than the temperature at which the absorbing agent is output from the absorbent crystallizer 141, the temperature of the absorbing solution entering the absorbent crystallizer 141 is greatly lowered after the heat exchange, so that the use can be reduced. The cooling capacity of the absorption solution is cooled. At the same time, the temperature of the crystallization of the absorbent from the absorbent crystallizer after heat exchange is greatly increased, and is transported to the absorber, absorbing the same amount of working fluid vapor, and releasing the heat of absorption at a higher working temperature, thereby It can increase the temperature of the external heating of the absorber and increase the heating grade, thereby improving energy efficiency.
请参阅图 4所示， 是本发明实施例 3的流程图。 从吸收剂结晶器 141 输出的结晶后溶液也经由吸收溶液自换热器 150, 使来自吸收器 14的吸收 溶液与从吸收剂结晶器 141 输出的吸收剂结晶 （或者含吸收剂结晶的吸收 溶液）和结晶后吸收溶液同时进行换热。 经过换热后的结晶后吸收溶液通 过吸收溶液输入管道 30输送至发生器 11中。 发生器 11的吸收溶液输出管 道 20与吸收器的吸收溶液输入管道相连， 从而将发生器 11输出的吸收溶 液与经过换热后的吸收剂结晶混合后共同输入到吸收器中。 从吸收剂结晶 器 141输出的结晶后吸收溶液经吸收溶液输入管道 30输送到发生器 11内。 经过换热后的来自吸收器 14的吸收溶液输入到吸收剂结晶器 141中进行冷 却结晶和固液分离； 经过换热后的从吸收剂结晶器 141 输出的吸收剂结晶 经吸收溶液输入管道被输送至吸收器 14 中。 由于来自吸收器 14的吸收溶 液的温度远高于从吸收剂结晶器 141输出的吸收剂结晶和结晶后吸收溶液 的温度， 所以经过换热后， 进入吸收剂结晶器 141 的吸收溶液温度大大降 低， 从而可以减少用于冷却吸收溶液的冷量。 同时， 经过换热后的来自吸 收剂结晶器的吸收剂结晶的温度大大提高， 其被输送到吸收器中， 吸收同 样量的工质蒸汽， 可以在更高的工作温度下释放吸收热， 从而可以提高吸 收器向外供热的温度， 提高供热品位。 经过换热后的来自吸收剂结晶器的 结晶后溶液的温度大大提高， 其被输送到发生器中， 蒸发出同样的工质蒸 汽， 本实施例可以减少发生器的消耗的热量， 从而提高能源利用效率。 Please refer to FIG. 4, which is a flowchart of Embodiment 3 of the present invention. The crystallized solution output from the absorbent crystallizer 141 is also passed from the heat exchanger 150 via the absorption solution, and the absorption solution from the absorber 14 is crystallized with the absorbent output from the absorbent crystallizer 141 (or the absorption solution containing the absorbent crystals). And heat transfer while absorbing the solution after crystallization. Absorption solution after crystallization after heat exchange The overabsorbent solution input conduit 30 is delivered to the generator 11. The absorption solution output pipe 20 of the generator 11 is connected to the absorption solution input pipe of the absorber, whereby the absorption solution output from the generator 11 is crystallized and mixed with the heat-treated absorbent, and is input into the absorber. The post-crystallization absorption solution output from the absorbent crystallizer 141 is sent to the generator 11 through the absorption solution input pipe 30. The heat-absorbed absorption solution from the absorber 14 is input to the absorbent crystallizer 141 for cooling crystallization and solid-liquid separation; the heat-treated absorbent crystals output from the absorbent crystallizer 141 are passed through the absorption solution input pipe. It is delivered to the absorber 14. Since the temperature of the absorbing solution from the absorber 14 is much higher than the temperature of the absorbing agent crystallized from the absorbent crystallizer 141 and the absorbing solution after crystallization, the temperature of the absorbing solution entering the absorbent crystallizer 141 is greatly lowered after heat exchange. Thereby, the amount of cooling for cooling the absorption solution can be reduced. At the same time, the temperature of the crystallization of the absorbent from the absorbent crystallizer after heat exchange is greatly increased, and is transported to the absorber, absorbing the same amount of working fluid vapor, and releasing the heat of absorption at a higher working temperature, thereby It can increase the temperature of the external heating of the absorber and increase the heating grade. After the heat exchange, the temperature of the crystallization solution from the absorbent crystallizer is greatly increased, and is sent to the generator to evaporate the same working fluid vapor. This embodiment can reduce the heat consumed by the generator, thereby improving the energy. usage efficiency.
请参阅图 5所示， 是本发明实施例 4的流程图。 所述的发生器 11的吸 收溶液输出管道 20与吸收器 14的吸收溶液输出管道 30相连， 相连的节点 位于进入吸收溶液自换热器 150之前。 来自发生器 11的吸收溶液与来自吸 收器 14的吸收溶液混合后进入吸收溶液自换热器 150, 与从吸收剂结晶器 141输出的吸收剂结晶和结晶后吸收溶液同时进行换热。经过换热后的结晶 后吸收溶液通过吸收溶液输入管道输送至发生器 11中。 经过换热后的吸收 剂结晶通过吸收溶液输入管道输送至吸收器 14中。 将来自发生器 11的吸 收溶液与来自吸收器 14的吸收溶液混合后进行冷却结晶，与前述方式相比， 增加了被冷却结晶的吸收溶液的量， 从而可以得到更多的结晶后吸收溶液， 从而可以提高吸收剂结晶器的使用效率。  Referring to FIG. 5, it is a flowchart of Embodiment 4 of the present invention. The absorption solution output line 20 of the generator 11 is connected to the absorption solution output line 30 of the absorber 14, and the connected node is located before the absorption solution from the heat exchanger 150. The absorbing solution from the generator 11 is mixed with the absorbing solution from the absorbing unit 14 and then introduced into the absorbing solution from the heat exchanger 150, and is condensed with the absorbing agent output from the absorbent crystallizer 141, and the absorbing solution is simultaneously subjected to heat exchange. After the crystallization after heat exchange, the absorption solution is sent to the generator 11 through the absorption solution input pipe. The heat-treated absorbent crystals are transported to the absorber 14 through the absorption solution input line. The absorption solution from the generator 11 is mixed with the absorption solution from the absorber 14 to be cooled and crystallized, and the amount of the absorption solution of the cooled crystal is increased as compared with the above-described manner, so that more absorption solution after crystallization can be obtained. Thereby, the use efficiency of the absorbent crystallizer can be improved.
请参阅图 6所示，是本发明实施例 5的蒸发系统的流程图。 本实施例提 出的蒸发系统与前述实施例基本相同， 不同之处在于， 其还包括压缩式制 冷循环装置， 用于向吸收剂结晶器 141 提供低温冷量。 该压缩式制冷循环 装置包括：吸收剂结晶-蒸发器 200、压缩机 210、吸收溶液换热-冷凝器 220、 节流阀 230以及压缩式制冷工质管道 240。压缩式制冷工质在吸收溶液换热 -冷凝器 220进行冷凝后， 经节流阀 230, 在吸收剂结晶-蒸发器 200中进行 蒸发，从而实现为吸收剂结晶器 141提供低温冷量。吸收剂结晶-蒸发器 200 出口压缩式制冷工质的蒸气经压缩机 21 Q压缩后进入吸收溶液换热-冷凝器 220 , 从而完成压缩式制冷循环。 Please refer to FIG. 6, which is a flow chart of the evaporation system of Embodiment 5 of the present invention. The evaporation system proposed in this embodiment is basically the same as the foregoing embodiment, except that it further includes a compression refrigeration cycle device for supplying a low temperature cooling amount to the absorbent crystallizer 141. The compression refrigeration cycle apparatus includes an absorbent crystallization-evaporator 200, a compressor 210, an absorption solution heat exchange-condenser 220, a throttle valve 230, and a compression-type refrigerant refrigerant pipe 240. Compressed refrigerant in the absorption solution heat transfer After the condenser 220 is condensed, it is evaporated in the absorbent crystallization-evaporator 200 via the throttle valve 230, thereby achieving a low-temperature cooling amount for the absorbent crystallizer 141. Absorbent Crystallization - Evaporator 200 The vapor of the outlet compressed refrigerant is compressed by the compressor 21 Q and then passed to the absorption solution heat exchanger-condenser 220, thereby completing the compression refrigeration cycle.
由于部分溴化锂的结晶析出， 在吸收剂结晶器 141 固液分离后的结晶 后吸收溶液的溴化锂浓度得到了降低。 上述结晶后吸收溶液即溴化锂稀溶 液通过结晶后吸收溶液管道 50,经吸收溶液换热-冷凝器 220和吸收溶液自 换热器 150被引入到发生器 11中。 另一方面， 在吸收剂结晶器 141固液分 离后的含吸收剂结晶的吸收溶液通过管道 40 ,经吸收溶液换热-冷凝器 220、 吸收溶液自换热器 150被引入到混合器 142。吸收溶液自换热器 150的作用 在于使来自吸收器 14的温度较高的吸收溶液与来自吸收剂结晶器的温度较 低的结晶后吸收溶液和含结晶溶液进行热交换， 从而提高供给发生器 11和 混合器 142的溶液温度，同时降低供给吸收剂结晶器的吸收溶液的温度。 而 吸收溶液换热-冷凝器 220的作用在于使压缩式制冷循环子系统压缩机 210 出口的温度较高的压缩式制冷工质蒸气与吸收剂结晶器 141 出口的温度较 低的结晶后吸收溶液和含吸收剂结晶的吸收溶液进行热交换， 从而使上述 制冷工质蒸气冷凝， 同时部分或全部融解渙化锂结晶并提高溶液温度。 通 过发生器 11的浓缩， 溴化锂浓度得到了提升的发生器 11 出口吸收溶液通 过吸收溶液管道 20被引入到混合器 142 中与含吸收剂结晶的吸收溶液混 合， 然后一起被引入到吸收器 14 中。 本发明可分别设定和优化吸收器 14 和发生器 11的吸收溶液的工作浓度。 也就是说， 本发明可实现一种对于吸 收式热泵循环十分有益的工艺条件， 即，使吸收器在高溴化锂浓度条件下工 作的同时， 发生器在比吸收器低的溴化锂浓度条件下工作，而这是传统的吸 收式热泵循环所难以做到的。 由于具有了吸收剂结晶器 141， 并且吸收器 14 所产生的热量通过热循环回路直接供给发生器 11,从而可以基本省去现 有吸收式热泵循环中向发生器 11供热的外部驱动热源，实现驱动热源基本 自供的吸收式热泵循环， 由发生器 11对外提供蒸气， 向蒸发装置的加热器 310供热。 本实施例的蒸发装置与实施例 1所述的蒸发装置相同。  Due to the crystallization of part of the lithium bromide, the lithium bromide concentration of the absorption solution after the solid-liquid separation of the absorbent crystallizer 141 is lowered. The crystallization solution, i.e., the lithium bromide dilute solution, passes through the crystallization solution absorption pipe 50, and is introduced into the generator 11 through the absorption solution heat exchange-condenser 220 and the absorption solution from the heat exchanger 150. On the other hand, the absorption solution containing the absorbent crystals after the solid-liquid separation of the absorbent crystallizer 141 is introduced into the mixer 142 through the pipe 40 through the absorption solution heat exchange-condenser 220 and the absorption solution from the heat exchanger 150. The absorption solution from the heat exchanger 150 functions to exchange heat between the higher temperature absorption solution from the absorber 14 and the lower temperature crystallization absorption solution and the crystal containing solution from the absorbent crystallizer, thereby increasing the supply generator. The solution temperature of 11 and mixer 142 is simultaneously lowered by the temperature of the absorption solution supplied to the absorbent crystallizer. The absorption solution heat exchange-condenser 220 functions to lower the temperature of the compression refrigeration refrigerant vapor at the outlet of the compression refrigeration cycle subsystem compressor 210 and the lower temperature crystallization absorption solution at the outlet of the absorbent crystallizer 141. The heat is exchanged with the absorption solution containing the crystallization of the absorbent to condense the vapor of the above-mentioned refrigerant, and at the same time partially or completely melt the crystal of lithium halide and increase the temperature of the solution. By the concentration of the generator 11, the generator of the lithium bromide concentration is increased. The outlet absorption solution is introduced into the mixer 142 through the absorption solution pipe 20 and mixed with the absorption solution containing the absorbent crystals, and then introduced into the absorber 14 together. . The present invention can separately set and optimize the working concentration of the absorption solution of the absorber 14 and the generator 11. That is, the present invention can achieve a process condition that is very beneficial for the absorption heat pump cycle, that is, while the absorber is operated at a high lithium bromide concentration, the generator operates at a lower concentration of lithium bromide than the absorber. This is difficult to achieve with conventional absorption heat pump cycles. Since the absorbent crystallizer 141 is provided, and the heat generated by the absorber 14 is directly supplied to the generator 11 through the thermal cycle, the externally driven heat source for supplying heat to the generator 11 in the existing absorption heat pump cycle can be substantially omitted. An absorption heat pump cycle in which the driving heat source is substantially self-supplied is realized, and the generator 11 supplies steam to the outside to supply heat to the heater 310 of the evaporation device. The evaporation apparatus of this embodiment is the same as the evaporation apparatus of the first embodiment.
本实施例的蒸发装置可以在基本不需要驱动热源的情况下， 实现对牛 奶、 植物提取液、 乙醇发酵液蒸馏塔底物、 化工原料等料液的浓缩， 也可 实现低能耗的海水淡化。 The evaporation device of the embodiment can concentrate the liquid of the milk, the plant extract, the ethanol fermentation liquid distillation bottom substrate, the chemical raw material, etc., without substantially driving the heat source. Achieve low-energy seawater desalination.
在上述的实施例中， 其中所述的蒸发装置为一个， 为更好地利用供热 装置提供的热能， 可以本发明的实施例可以设置为多个蒸发装置，各蒸发装 置间， 前一个蒸发装置的气液分离器连接于下一个蒸发装置的加热器； 第 一个蒸发装置的加热器通过蒸气通路连接于供热装置的发生器， 接收供热 装置产生的蒸气； 最后一个蒸发装置的气液分离器连接于供热装置的吸收 器， 向吸收器提供乏蒸汽； 从而形成多效蒸发系统。  In the above embodiment, wherein the evaporation device is one, in order to better utilize the thermal energy provided by the heating device, the embodiment of the present invention may be provided as a plurality of evaporation devices, and each evaporation device is preceded by evaporation. The gas-liquid separator of the device is connected to the heater of the next evaporation device; the heater of the first evaporation device is connected to the generator of the heating device through the vapor passage, receives the steam generated by the heating device; the gas of the last evaporation device The liquid separator is coupled to the absorber of the heating device to provide spent steam to the absorber; thereby forming a multi-effect evaporation system.
本发明的实施例 6提出了一种蒸发浓缩方法， 采用实施例所述的蒸发 系统对以水为溶剂的料液进行浓缩， 该蒸发浓缩方法其包括以下步骤： Embodiment 6 of the present invention proposes an evaporation concentration method for concentrating a water-based solvent solution using the evaporation system described in the embodiment, the evaporation concentration method comprising the following steps:
( 1 )在发生器 11中浓缩吸收溶液同时产生蒸气， 并将上述蒸气输送到 蒸发装置的加热器 310, 所述的浓缩吸收溶液被输送至吸收器 14中； (1) concentrating the absorption solution in the generator 11 while generating a vapor, and delivering the vapor to the heater 310 of the evaporation device, the concentrated absorption solution being sent to the absorber 14;
( 2 )加热器 310与蒸发设备 320进行换热， 使蒸发设备 320中的料液 中的水蒸发为蒸气， 使料液浓缩；  (2) The heater 310 exchanges heat with the evaporation device 320 to evaporate water in the liquid in the evaporation device 320 into a vapor to concentrate the liquid;
( 3 ) 蒸发设备 320中的浓缩料液和蒸气输入到气液分离器 330中进行 气液分离， 输出浓缩料液和乏蒸汽；  (3) The concentrated liquid and vapor in the evaporation device 320 are input to the gas-liquid separator 330 for gas-liquid separation, and the concentrated liquid and the spent steam are output;
( 4 )经气液分离后的乏蒸汽输送到供热装置的吸收器 14中， 来自发生 器 11的吸收溶液吸收所述乏蒸汽并产生吸收热， 同时吸收溶液浓度降氐并 被输送至吸收剂结晶器 141中；  (4) The spent steam separated by the gas-liquid separation is sent to the absorber 14 of the heating device, and the absorption solution from the generator 11 absorbs the spent steam and generates absorption heat, while the concentration of the absorption solution is lowered and sent to the absorption. In the crystallizer 141;
( 5 )在吸收剂结晶器 141 中进行吸收溶液冷却结晶和固液分离， 形成 吸收剂结晶和结晶后吸收溶液，所述的结晶后吸收溶液输送至发生器 11中， 而吸收剂结晶 （或含吸收剂结晶的吸收溶液）输送至吸收器 14中；  (5) performing absorption crystallization and solid-liquid separation in the absorbent crystallizer 141 to form an absorption crystallization and crystallization of the absorption solution, and the crystallization solution is transported to the generator 11 and the absorbent is crystallized (or An absorption solution containing crystallization of the absorbent) is delivered to the absorber 14;
( 6 )在吸收器 11和发生器 14之间进行热循环， 将吸收溶液在吸收器 中吸收乏蒸汽时产生的吸收热输送至发生器中。  (6) Thermal cycling is performed between the absorber 11 and the generator 14, and the absorption heat generated when the absorption solution absorbs the spent steam in the absorber is delivered to the generator.
较佳的， 在所述的结晶后吸收溶液输送到发生器之前， 且吸收器输出 的吸收溶液进行冷却之前， 所述的吸收器输出的吸收溶液与所述的结晶后 吸收溶液进行换热。  Preferably, the absorption solution outputted by the absorber exchanges heat with the post-crystallization absorption solution before the crystallization solution is transported to the generator after the crystallization, and the absorption solution output from the absorber is cooled.
较佳的， 在所述的吸收剂结晶输送到吸收器之前， 且吸收器输出的吸 收溶液进行冷却之前， 所述的吸收剂结晶与所述的吸收器输出的吸收溶液 进行换热。  Preferably, the absorbent crystals exchange heat with the absorption solution output by the absorber before the absorption of the absorbent crystals to the absorber and before the absorption of the absorber output is cooled.
较佳的， 在所述的结晶后吸收溶液输送到发生器之前， 吸收剂结晶输 送到吸收器之前， 且所述吸收器输出的收溶液进行冷却之前， 所述吸收器 输出的吸收溶液与所述的吸收剂结晶和结晶后吸收溶液进行换热。 Preferably, before the crystallization is carried out, the absorption solution is transferred to the generator, and the absorbent is crystallized. Before being sent to the absorber, and before the absorption solution output by the absorber is cooled, the absorption solution outputted by the absorber exchanges heat with the absorption and crystallization solution of the absorbent.
较佳的， 在所述的结晶后吸收溶液输送到发生器之前， 吸收剂结晶输 送到吸收器之前， 吸收器输出的吸收溶液进行冷却之前， 且所述发生器输 出的吸收溶液输送到吸收器之前， 该发生器输出的吸收溶液与所述吸收器 输出的吸收溶液混合形成混合吸收溶液， 该混合吸收溶液与所述的吸收剂 结晶和结晶后吸收溶液进行换热。  Preferably, before the crystallization of the absorption solution is sent to the generator, before the absorption of the absorption agent to the absorber, before the absorption solution of the absorber is cooled, the absorption solution output by the generator is sent to the absorber. Previously, the absorption solution outputted by the generator is mixed with the absorption solution output from the absorber to form a mixed absorption solution, and the mixed absorption solution is subjected to heat exchange with the absorbent after crystallization and crystallization.
通过对吸收器 14输出的吸收溶液与吸收剂结晶器 141输出的结晶后吸 收溶液和吸收剂结晶 （或含吸收剂结晶的吸收溶液）进行热交换， 从而在 保持较低的发生器吸收溶液溴化锂工作浓度的前提下， 可显著提高吸收器 14吸收溶液的溴化锂工作浓度，从而可在吸收器 14中得到温度更高的吸收 热， 使得该吸收热能够用作发生器 11的驱动热能并使发生器 11的工作温 度更高， 即能够产生温度更高的过热蒸气。  The absorption of the absorbing solution output from the absorber 14 and the crystallization of the absorbing solution and the absorbing agent (or the absorbing solution containing the absorbing agent) output from the absorbent crystallizer 141 are performed, thereby maintaining the lower generator absorbing solution lithium bromide. Under the premise of working concentration, the working concentration of lithium bromide absorbed by the absorber 14 can be significantly increased, so that a higher temperature absorption heat can be obtained in the absorber 14, so that the heat of absorption can be used as the driving heat of the generator 11 and occurs. The operating temperature of the device 11 is higher, that is, it is capable of generating a superheated vapor having a higher temperature.
较佳的， 在上述的热循环过程中进行热补偿， 即设置有外部热源加热 装置 160 以补偿由于散热损失等引起的发生器热量的少量不足， 从而可以 保证整个制热过程的持续进行。 共同构成料液蒸发浓缩方法。  Preferably, the thermal compensation is performed during the above thermal cycle, i.e., an external heat source heating device 160 is provided to compensate for a small amount of heat shortage of the generator due to heat loss, etc., thereby ensuring the continuous progress of the entire heating process. Together, it constitutes a liquid evaporation and concentration method.
本发明的实施例 7提供了另一种蒸发浓缩方法，该方法与实施例 6基本 相同， 不同之处在于， 吸收剂结晶器 141 中进行的吸收溶液冷却结晶所需 的低温冷量来自压缩式制冷循环过程。 具体的， 吸收剂结晶-蒸发器 200出 口压缩式制冷工质的蒸气经压缩机 210 压缩后进入吸收溶液换热-冷凝器 220进行冷凝， 冷凝后的压缩式制冷工质经节流阀 230 , 在吸收剂结晶-蒸 发器 200 中进行蒸发， 从而完成压缩式制冷循环。 由于本实施例的压缩式 制冷工质在吸收溶液换热-冷凝器 220冷凝时的冷量来自溴化锂结晶器 141 出口溶液所具有的冷量， 因此本循环的蒸发温度和冷凝温度较为接近， 从 而可达到较高的制冷性能系数。 也就是说， 本实施例的压缩式制冷循环的 能耗较低。 该压缩式制冷循环过程为吸收溶液提供的冷却结晶的温度为 - 18 ~ 7 °C。  Embodiment 7 of the present invention provides another evaporation concentration method which is substantially the same as that of Embodiment 6, except that the low-temperature cooling amount required for the crystallization of the absorption solution in the absorbent crystallizer 141 comes from the compression type. Refrigeration cycle process. Specifically, the vapor of the refrigerant crystallization-evaporator 200 exiting the compressed refrigerant is compressed by the compressor 210 and then enters the absorption solution heat exchange-condenser 220 for condensation, and the condensed compressed refrigerant is passed through the throttle valve 230. Evaporation is carried out in the absorbent crystallization-evaporator 200 to complete the compression refrigeration cycle. Since the cooling refrigerant of the embodiment is condensed in the absorption solution heat exchanger-condenser 220 from the cooling capacity of the outlet solution of the lithium bromide crystallizer 141, the evaporation temperature and the condensation temperature of the cycle are relatively close, thereby A higher coefficient of refrigeration performance can be achieved. That is, the compression refrigeration cycle of the present embodiment consumes less energy. The temperature of the cooled crystallization provided by the absorption refrigeration process during the compression refrigeration cycle is - 18 to 7 °C.
本发明的上述实施例所述的技术方案对所采用吸收溶液的种类并无特 别的限制， 上述实施例皆以水-溴化鋰为工质对的吸收溶液为例进行说明， 在其他的实施方式中， 也可以采用工质为水、 曱醇和乙醇其中之一或几种 物质的混合物；吸收剂为 LiBr、 LiCl、 LiN03、 NaBr、 KBr、 CaCl2、 MgBr2 和 ZnC 12其中之一或几种物质的混合物。 The technical solution described in the above embodiments of the present invention has no special type of absorption solution used. In other embodiments, the above examples are exemplified by water-lithium bromide as the absorbing solution of the working medium. In other embodiments, the working medium may be one or more of water, sterol and ethanol. The mixture; the absorbent is one of or a mixture of LiBr, LiCl, LiN0 3 , NaBr, KBr, CaCl 2 , MgBr 2 and ZnC 1 2 .
以下通过具有具体参数的实例来说明上述实施例的可实施性。  The feasibility of the above embodiments will be explained below by way of examples with specific parameters.
实例 1  Example 1
本实例采用实施例 6 所述的方法进行海水淡化。 海水的水含量（质量 百分含量） 约为 96 % , 采用 165 °C饱和蒸气作为外部热源对热循环回路中 的工质进行加热， 以补偿由于散热损失等引起的发生器驱动热源的热量不 足部分， 采用二曱基硅油作为热循环工质， 而采用 20°C的冷却水来冷却吸 收剂结晶器 141 , 得到的卤水的水含量（质量百分含量） 为 90 % , 供热装 置的能量效率 （COP ) 为 10. 0， 每 p屯淡水的产水热耗约为 270MJ。  This example was carried out by seawater desalination using the method described in Example 6. The seawater has a water content (mass percentage) of about 96%. The saturated steam at 165 °C is used as an external heat source to heat the working fluid in the thermal circuit to compensate for the insufficient heat of the generator-driven heat source due to heat loss. In part, the dimercaptosilicone oil is used as the thermal cycle working medium, and the cooling water of 20 ° C is used to cool the absorbent crystallizer 141, and the water content (mass percentage) of the brine obtained is 90%, and the energy of the heating device is The efficiency (COP) is 1.00, and the heat production rate per p屯 fresh water is about 270 MJ.
本实例的供热装置的能量效率 COP的计算公式如下：  The energy efficiency COP of the heating device of this example is calculated as follows:
COP-输出热量 /所投入外部热源的热量  COP-output heat / heat input to external heat source
实例 2  Example 2
本实例采用实施例 6 所述的方法， 蒸发浓缩牛奶， 原料牛奶的水含量 (质量百分含量）为 88 % , 采用 210°C饱和蒸气作为外部热源对热循环回路 中的工质进行加热， 以补偿由于散热损失等引起的发生器驱动热源的热量 不足部分， 采用二曱基硅油作为热循环工质， 而采用 60°C的冷却水来冷却 吸收剂结晶器 141 , 得到的浓缩牛奶的水含量（重量百分含量） 为 60 % , 供热装置的能量效率 （COP ) 为 10. 0。  In this example, the method described in Example 6 is used to evaporate the concentrated milk. The water content (mass percentage) of the raw milk is 88%, and the working medium in the thermal cycle is heated by using 210 ° C saturated steam as an external heat source. In order to compensate for the insufficient heat of the heat source of the generator driven by the heat loss, etc., the dimercaptosilicone oil is used as the thermal cycle working medium, and the cooling crystal water of the absorbent crystallizer 141 is cooled by the cooling water of 60 ° C to obtain the water of the concentrated milk. The content (weight percent) is 60%, and the energy efficiency (COP) of the heating device is 10.0.
本实例 COP的计算公式如下：  The calculation formula for this example COP is as follows:
COP 输出热量 /所投入外部热源的热量  COP output heat / heat input to external heat source
实例 3  Example 3
本实例采用实施例 7 所述的方法， 蒸发浓缩牛奶， 原料牛奶的水含量 (质量百分含量） 为： 88 %， 采用 200°C饱和蒸气作为外部热源对热循环回 路中的工质进行加热， 以补偿由于散热损失等引起的发生器驱动热源的热 量不足部分， 采用二曱基硅油作为热循环工质， 而采用压缩式制冷循环提 供的（TC的压缩式制冷工质来冷却吸收剂结晶器 141， 得到的浓缩牛奶的水 含量为 60 % , 供热装置的能量效率 （COP ) 为 5. 5。 本实例 COP的计算公式如下： In this example, the method described in Example 7 is used to evaporate the concentrated milk. The water content (mass percentage) of the raw milk is: 88%, and the working medium in the thermal cycle is heated by using 200 ° C saturated steam as an external heat source. To compensate for the insufficient heat of the generator-driven heat source caused by heat loss, etc., using di-n-based silicone oil as the thermal cycle working fluid, and using the compression refrigeration cycle provided by the compression refrigeration cycle (TC compression refrigerant to cool the absorbent crystal 5。 The energy content (COP) of the heating device is 6.5. The calculation formula of this example COP is as follows:
COP-输出热量 / (所投入外部热源的热量 +压缩机的耗电量 X 3.0) 在此， 取为所述压缩机供电的电网用户端的一次能源发电效率为 33. 3%。  The COP-output heat / (the amount of heat input to the external heat source + the power consumption of the compressor X 3.0) Here, the primary energy generation efficiency of the grid customer terminal that supplies the compressor is 33.3%.
实例 4  Example 4
本实例采用实施例 7 所述的方法， 蒸发浓缩植物提取液， 该原料水含 量（质量百分比）为 95%, 采用 130°C饱和蒸气作为外部热源对热循环回路 中的工质进行加热， 以补偿由于散热损失等引起的发生器驱动热源的热量 不足部分， 采用二曱基硅油作为热循环工质， 而采用压缩式制冷循环提供 的- 18°C的压缩式制冷工质来冷却吸收剂结晶器 141。 得到的植物提取物浓 缩液的水含量为 70 %， 供热装置的能量效率 （COP ) 为 5. 5。  In this example, the method described in Example 7 is used to evaporate and concentrate the plant extract, the water content (mass percentage) of the raw material is 95%, and the working fluid in the thermal cycle is heated by using 130 ° C saturated steam as an external heat source. Compensating for the insufficient heat of the generator-driven heat source caused by heat loss, etc., using dimercaptosilicone oil as the thermal cycle working fluid, and using the compression refrigeration cycle provided by the compression refrigeration cycle to cool the absorbent crystal 141. The obtained plant extract concentrate had a water content of 70% and the heating device had an energy efficiency (COP) of 5.9.
本实例 COP的计算公式如下：  The calculation formula for this example COP is as follows:
COP输出热量 / (所投入外部热源的热量 +压缩机的耗电量 X 3.0) 在此， 取为所述压缩机供电的电网用户端的一次能源发电效率为 33. 3%。  The COP output heat / (the amount of heat input to the external heat source + the power consumption of the compressor X 3.0) Here, the primary energy generation efficiency of the grid customer terminal that supplies the compressor is 33.3%.
下表 1为上述实例 1 ~ 4的工作参数和性能。  Table 1 below shows the operating parameters and performance of the above examples 1 ~ 4.
表 1  Table 1
Figure imgf000015_0001
外部 进口热循环工质温度（ °C ) 160. 0 125. 0 热源
Figure imgf000015_0001
External inlet thermal cycle working temperature ( °C ) 160. 0 125. 0 heat source
力口热 出口热循环工质温度（ °C ) 160. 4 205. 4 195. 4 125. 4 装置  Heat outlet heat cycle temperature ( °C ) 160. 4 205. 4 195. 4 125. 4
COP 10. 0 10. 0 5. 5 5. 5 以上所述， 仅是本发明的较佳实施例而已，并非对本发明作任何形式上 的限制， 虽然本发明已以较佳实施例揭露如上， 然而并非用以限定本发明， 任何熟悉本专业的技术人员， 在不脱离本发明技术方案范围内，当可利用上 述揭示的技术内容作出些许更动或修饰为等同变化的等效实施例，但凡是 未脱离本发明技术方案的内容， 依据本发明的技术实质对以上实施例所作 的任何简单修改、 等同变化与修饰， 均仍属于本发明技术方案的范围内。 工业应用性  COP 10. 0 10. 0 5. 5 5. 5 The above is only a preferred embodiment of the present invention, and is not intended to limit the present invention in any way, although the present invention has been disclosed above by way of preferred embodiments. However, it is not intended to limit the invention, and those skilled in the art can make some modifications or modifications to equivalent embodiments, which can be modified by the above-disclosed embodiments without departing from the scope of the invention. Any simple modifications, equivalent changes and modifications to the above embodiments in accordance with the technical spirit of the present invention are still within the scope of the technical solutions of the present invention. Industrial applicability
本发明的蒸发系统以及蒸发浓缩方法， 由于其供热装置具有了吸收剂 结晶器，并且吸收器所产生的热量作为发生器热源通过热循环回路直接供 给发生器， 因而可以在供热装置中省去吸收式制热循环所需的外部驱动热 源， 实现驱动热源基本自供的吸收式制热循环， 并将热能通过蒸气输送到 蒸发装置用于进行蒸发浓缩过程， 使整个蒸发系统基本无需外部热源， 有 效地节约了能源和水资源， 从而更加适于实用。  The evaporation system and the evaporation concentration method of the present invention, since the heating device has an absorbent crystallizer, and the heat generated by the absorber is directly supplied to the generator as a heat source of the generator through the heat circulation circuit, thereby saving in the heating device The external driving heat source required for the absorption heating cycle realizes an absorption heating cycle in which the driving heat source is substantially self-supply, and the heat energy is sent to the evaporation device through the vapor for the evaporation concentration process, so that the entire evaporation system basically does not require an external heat source. It effectively saves energy and water resources, making it more suitable for practical use.

Claims

权 利 要 求 Rights request
1、 一种蒸发系统， 其特征在于其包括供热装置和蒸发装置， An evaporation system, characterized in that it comprises a heating device and an evaporation device,
所述的供热装置包括：  The heating device includes:
发生器， 其内设有换热器（110 ), 用于浓缩吸收溶液并产生蒸气； 吸收器， 用于产生热量， 其内设有换热器（140 )， 该换热器（140 ) 与换热器（110 )相连接， 形成热循环回路， 用于将吸收器中产生的热量输 送至发生器中； 及  a generator having a heat exchanger (110) for concentrating the absorption solution and generating a vapor; an absorber for generating heat, wherein a heat exchanger (140) is disposed, the heat exchanger (140) and The heat exchangers (110) are connected to form a thermal circuit for delivering heat generated in the absorber to the generator;
吸收剂结晶器, 接收来自吸收器和 /或发生器的吸收溶液并进行冷 却， 形成吸收剂结晶和结晶后吸收溶液， 所述的结晶后溶液输送至发生器， 所述的吸收剂结晶输送至吸收器；  An absorbent crystallizer, which receives the absorption solution from the absorber and/or the generator and cools it to form an absorption solution after crystallization and crystallization of the absorbent, the post-crystallization solution is sent to a generator, and the absorbent is crystallized to Absorber;
所述的蒸发装置包括：  The evaporation device includes:
加热器， 通过蒸气通路与上述供热装置的发生器相连接， 接收供 热装置产生的蒸气；  a heater connected to the generator of the heating device via a vapor passage to receive the steam generated by the heating device;
蒸发设备， 与所述的加热器进行换热； 及  Evaporating the device, exchanging heat with the heater; and
气液分离器， 连接于蒸发设备， 并通过另一蒸气通道连接于供热 装置的吸收器， 向供热装置提供蒸气。  The gas-liquid separator is connected to the evaporation device and connected to the absorber of the heating device through another vapor passage to supply steam to the heating device.
2、 根据权利要求 1所述的蒸发系统， 其特征在于， 该系统还包括： 吸 收溶液自换热器， 用于所述的来自发生器的吸收溶液和 /或来自吸收器的吸 收溶液， 与结晶后吸收溶液和 /或吸收剂结晶或者含吸收剂结晶的吸收溶液 进行换热。  2. The evaporation system according to claim 1, wherein the system further comprises: an absorption solution from the heat exchanger, the absorption solution from the generator and/or the absorption solution from the absorber, and After crystallization, the absorption solution and/or the absorbent crystals or the absorption solution containing the absorbent crystals are subjected to heat exchange.
3、 根据权利要求 1所述的蒸发系统， 其特征在于其还包括： 吸收溶液 自换热器， 用于将来自吸收器的吸收溶液与来自吸收剂结晶器的结晶后吸 收溶液进行换热。  3. The evaporation system of claim 1 further comprising: an absorption solution from the heat exchanger for heat exchange of the absorption solution from the absorber with the post-crystallization absorption solution from the absorbent crystallizer.
4、 根据权利要求 1所述的蒸发系统， 其特征在于其还包括： 吸收溶液 自换热器， 用于将来自吸收器的吸收溶液与来自吸收剂结晶器的吸收剂结 晶或者含吸收剂结晶的吸收溶液进行换热。  4. The evaporation system according to claim 1, further comprising: an absorption solution from the heat exchanger for crystallizing or absorbing the absorption solution from the absorber with the absorbent from the absorbent crystallizer The absorption solution is subjected to heat exchange.
5、 根据权利要求 1所述的蒸发系统， 其特征在于其还包括： 吸收溶液 自换热器， 用于将来自吸收器的吸收溶液与来自吸收剂结晶器的结晶后吸 收溶液和吸收剂结晶或者含吸收剂结晶的吸收溶液进行换热。 5. The evaporation system according to claim 1, further comprising: an absorption solution from the heat exchanger for crystallizing the absorption solution from the absorber with the post-crystallization absorption solution and the absorbent from the absorbent crystallizer Or an absorption solution containing an crystallization of an absorbent for heat exchange.
6、 根据权利要求 5所述的蒸发系统， 其特^在于来自发生器的吸收溶 液和来自吸收器的吸收溶液混合后进入吸收溶液自换热器， 与来自吸收剂 结晶器的吸收溶液和吸收剂结晶或者含吸收剂结晶的吸收溶液进行换热。 6. The evaporation system according to claim 5, wherein the absorption solution from the generator and the absorption solution from the absorber are mixed into the absorption solution from the heat exchanger, and the absorption solution and absorption from the absorbent crystallizer. The crystallization of the agent or the absorption solution containing the crystallization of the absorbent is carried out for heat exchange.
7、 根据权利要求 1-6任一项所述的蒸发系统， 其特征在于其中所述的 热循环回路上设有外部热源加热装置。  7. An evaporation system according to any of claims 1-6, wherein said thermal circuit is provided with an external heat source heating means.
8、 根据权利要求 7所述的蒸发系统， 其特征在于其中所述的蒸发装置 为多个， 各蒸发装置间， 前一个蒸发装置的气液分离器连接于下一个蒸发 装置的加热器； 第一个蒸发装置的加热器通过蒸气通路连接于供热装置的 发生器， 接收供热装置产生的蒸气； 最后一个蒸发装置的气液分离器连接 于供热装置的吸收器， 向供热装置提供蒸气。  The evaporation system according to claim 7, wherein the plurality of evaporation devices are plural, and between the evaporation devices, the gas-liquid separator of the previous evaporation device is connected to the heater of the next evaporation device; a heater of an evaporation device is connected to the generator of the heating device through a vapor passage to receive the steam generated by the heating device; the gas-liquid separator of the last evaporation device is connected to the absorber of the heating device, and supplies the heating device with Vapor.
9、 根据权利要求 1-8任一项所述的蒸发系统， 其特征在于其还包括由 吸收剂结晶-蒸发器、 压缩机、 吸收溶液换热-冷凝器、 节流阀以及压缩式 制冷工质管道构成的压缩式制冷装置， 用于向上述吸收剂结晶器提供冷量。  9. The evaporation system according to any one of claims 1-8, characterized in that it further comprises an absorption crystallization-evaporator, a compressor, an absorption solution heat exchange-condenser, a throttle valve, and a compression type refrigerator. A compression refrigeration device comprising a mass conduit for supplying a cooling capacity to the absorbent crystallizer.
10、 一种蒸发浓缩方法， 采用前述任一权利要求所述的蒸发装置， 其 包括以下步骤：  10. An evaporation concentration method, using the evaporation apparatus of any of the preceding claims, comprising the steps of:
( 1 )在发生器中浓缩吸收溶液同时产生蒸气， 并将上述蒸气输送到加 热器， 所述的浓缩吸收溶液被输送至吸收器中；  (1) concentrating the absorption solution in the generator while generating a vapor, and delivering the vapor to the heater, the concentrated absorption solution being sent to the absorber;
( 2 )加热器与蒸发设备进行换热， 使蒸发设备中的料液蒸发浓缩； (2) heat exchange between the heater and the evaporation device to evaporate and concentrate the liquid in the evaporation device;
( 3 )蒸发设备中的浓缩料液和蒸气输入到气液分离器中进行气液分离； ( 4 ) 经气液分离后的蒸气输送到吸收器中， 来自发生器的吸收溶液吸 收所述蒸气并产生吸收热， 同时吸收溶液浓度降低并被输送至吸收剂结晶 器中； (3) The concentrated liquid and vapor in the evaporation device are input into the gas-liquid separator for gas-liquid separation; (4) the vapor separated by the gas-liquid separation is sent to the absorber, and the absorption solution from the generator absorbs the vapor And generating absorption heat, while the concentration of the absorption solution is lowered and sent to the absorbent crystallizer;
( 5 )在吸收剂结晶器中进行吸收溶液的冷却结晶和固液分离， 形成吸 收剂结晶和结晶后吸收溶液， 固液分离后的结晶后吸收溶液输送至发生器 中， 吸收剂结晶或含吸收剂结晶的吸收溶液输送至吸收器中；  (5) performing cooling crystallization and solid-liquid separation of the absorption solution in the absorbent crystallizer to form an absorption solution crystal and crystallization solution, and the absorption solution after solid-liquid separation is sent to the generator, and the absorbent is crystallized or contained. The absorption solution of the crystallization of the absorbent is delivered to the absorber;
( 6 )在吸收器和发生器之间进行热循环， 将吸收溶液在吸收器中吸收 蒸气时产生的吸收热输送至发生器中。  (6) Thermal cycling between the absorber and the generator, the absorption heat generated when the absorption solution absorbs the vapor in the absorber is delivered to the generator.
11、 根据权利要求 10所述的蒸发浓缩方法， 其特征在于还包括： 在所 述的结晶后吸收溶液输送到发生器之前， 且吸收 H输出的吸收溶液进行冷 却之前， 所述的吸收器输出的吸收溶液与所述的结晶后吸收溶液进行换热。 11. The evaporation concentration method according to claim 10, further comprising: said absorber output before said crystallization solution is transported to the generator after crystallization and absorbing the H output absorbing solution for cooling The absorbing solution exchanges heat with the crystallization solution after crystallization.
12、 根据权利要求 10所述的蒸发浓缩方法， 其特征在于还包括： 在所 述的吸收剂结晶输送到吸收器之前， 且吸收器输出的吸收溶液进行冷却之 前， 所述的吸收剂结晶或者含吸收剂结晶的吸收溶液与所述的吸收器输出 的吸收溶液进行换热。 12. The evaporation concentration method according to claim 10, further comprising: crystallization of said absorbent before said crystallization of said absorbent is delivered to said absorber, and said absorbing solution output from said absorber is cooled. The absorption solution containing the crystallization of the absorbent exchanges heat with the absorption solution output from the absorber.
13、 根据权利要求 10所述的蒸发浓缩方法， 其特征在于还包括： 在所 述的结晶后吸收溶液输送到发生器之前， 吸收剂结晶输送到吸收器之前， 且吸收器输出的吸收溶液进行冷却之前， 所述吸收器输出的吸收溶液与所 述的结晶后吸收溶液和吸收剂结晶或者含吸收剂结晶的吸收溶液进行换 热。  13. The evaporation concentration method according to claim 10, further comprising: before the crystallization of the absorption solution is sent to the generator, before the absorption of the absorption agent to the absorber, and the absorption solution output by the absorber is performed. Before cooling, the absorption solution output from the absorber exchanges heat with the post-crystallization absorption solution and the absorbent crystal or the absorption solution containing the absorbent crystal.
14、 根据权利要求 10所述的蒸发浓缩方法， 其特征在于还包括： 在所 述的结晶后吸收溶液输送到发生器之前， 吸收剂结晶输送到吸收器之前， 吸收器输出的吸收溶液进行冷却之前， 且所述发生器输出的吸收溶液输送 到吸收器之前， 该发生器输出的吸收溶液与所述吸收器输出的吸收溶液混 合形成混合吸收溶液， 该混合吸收溶液与所述的结晶后吸收溶液和吸收剂 结晶或者含吸收剂结晶的吸收溶液进行换热。  14. The evaporation concentration method according to claim 10, further comprising: before the crystallization solution is transported to the generator after the crystallization, before the crystallization of the absorbent is delivered to the absorber, the absorption solution output from the absorber is cooled. Before, and before the absorption solution outputted by the generator is sent to the absorber, the absorption solution outputted by the generator is mixed with the absorption solution outputted by the absorber to form a mixed absorption solution, and the mixed absorption solution is absorbed after the crystallization. The solution and the absorbent crystal or the absorption solution containing the absorbent crystal are subjected to heat exchange.
15、 根据权利要求 10所述的蒸发浓缩方法， 其特征在于在所述的步骤 ( 6 ) 的热循环过程中， 通过外部热源向发生器补尝热量。  15. The evaporation concentration method according to claim 10, characterized in that during the thermal cycle of the step (6), heat is compensated to the generator by an external heat source.
16、 根据权利要求 10所述的蒸发浓缩方法， 其特征在于通过压缩式制 冷循环向上述的步骤（5 )提供吸收溶液冷却结晶所需的冷量。  The evaporation concentration method according to claim 10, characterized in that the step (5) of the above-described step (5) is supplied with a cooling amount required for cooling the crystal by a compression refrigeration cycle.
17、 根据权利要求 10-16任一项所述的蒸发浓缩方法， 其特征在于所 述的步骤（5 ) 中的吸收溶液冷却结晶的温度为- 18 ~ 60°C。  The evaporation concentration method according to any one of claims 10-16, characterized in that the temperature of the crystallization solution in the step (5) is -18 to 60 °C.
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