WO2009094896A1 - Système d'évaporation et procédé d'évaporation-concentration - Google Patents

Système d'évaporation et procédé d'évaporation-concentration 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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English (en)
Chinese (zh)
Inventor
Qingquan Su
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Qingquan Su
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Publication of WO2009094896A1 publication Critical patent/WO2009094896A1/fr

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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.

Abstract

La présente invention concerne un système d'évaporation et un procédé d'évaporation-concentration utilisant ce système. Le système d'évaporation comprend: un générateur (11) servant à concentrer la solution d'absorbant et à produire de la vapeur; un absorbeur (14) servant à produire de la chaleur, une boucle de circulation de chaleur étant établie entre le générateur (11) et l'absorbeur (14) de façon à transférer de l'absorbeur (14) au générateur (11) la chaleur produite; un cristallisoir d'absorbant (141) où l'orifice d'entrée de solution d'absorbant, l'orifice de sortie de solution d'absorbant de post-cristallisation, l'orifice de sortie des cristaux, ainsi l'orifice d'entrée de solution d'absorbant du cristallisoir d'absorbant (141) sont reliés à la sortie de solution d'absorbant (14), l'orifice de sortie de la solution d'absorbant de post-cristallisation du cristallisoir d'absorbant (141) étant relié à l'orifice d'entrée de la solution d'absorbant du générateur (11), l'orifice de sortie de cristaux du cristallisoir d'absorbant (141) étant relié à l'orifice d'entrée de la solution d'absorbant de l'absorbeur (14); un réchauffeur (310) servant à recevoir la vapeur produite par le générateur (11); un évaporateur (320) servant à l'échange thermique avec le réchauffeur (310); un séparateur gaz-liquide (330).
PCT/CN2009/000076 2008-01-22 2009-01-12 Système d'évaporation et procédé d'évaporation-concentration WO2009094896A1 (fr)

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CN110508016A (zh) * 2019-08-22 2019-11-29 无锡市海昌机械设备有限公司 模块式溶剂蒸发系统
CN113932474A (zh) * 2021-11-15 2022-01-14 江苏科技大学 一种热泵多效蒸发耦合式水处理系统及其工作方法

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CN110508016A (zh) * 2019-08-22 2019-11-29 无锡市海昌机械设备有限公司 模块式溶剂蒸发系统
CN113932474A (zh) * 2021-11-15 2022-01-14 江苏科技大学 一种热泵多效蒸发耦合式水处理系统及其工作方法

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