WO2009094895A1 - A distillation system and a distillation method - Google Patents

A distillation system and a distillation method Download PDF

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Publication number
WO2009094895A1
WO2009094895A1 PCT/CN2009/000075 CN2009000075W WO2009094895A1 WO 2009094895 A1 WO2009094895 A1 WO 2009094895A1 CN 2009000075 W CN2009000075 W CN 2009000075W WO 2009094895 A1 WO2009094895 A1 WO 2009094895A1
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WO
WIPO (PCT)
Prior art keywords
absorption solution
absorber
crystallization
absorbent
solution
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Application number
PCT/CN2009/000075
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French (fr)
Chinese (zh)
Inventor
Qingquan Su
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Qingquan Su
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Publication date
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Publication of WO2009094895A1 publication Critical patent/WO2009094895A1/en

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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/14—Fractional distillation or use of a fractionation or rectification column
    • 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

Definitions

  • the present invention relates to a distillation technique in the chemical field, and more particularly to a distillation system and a distillation method for performing distillation without externally driven heat sources. Background technique
  • FIG. 1 is a flow chart of the existing distillation system. It consists of a distillation column 300, a chiller 310, a material recycle tank 320, and a reboiler 330.
  • the steaming tower 300 is used for separating components in the material.
  • the top of the distillation column is provided with a condenser 310.
  • the low boiling component is output from the top of the distillation column and then cooled in the condenser 310 to enter the material return storage tank 320.
  • a part of the material output a part of the material is returned to the distillation column 300.
  • the bottom of the distillation column 300 outputs a high boiling component, a part of the material is output, and a part of the material is heated by the reboiler 330 and sent to the distillation column to continue to be steamed.
  • the above-mentioned prior distillation system requires a heat source to be supplied to the reboiler 330 for raising the temperature of the bottom material of the distillation column, and a condenser 310 for supplying a cold source to the top of the distillation column is required for cooling the material. .
  • the condenser 310 of the distillation system outputs heat to the outside, but this heat is not utilized by the reboiler because the condenser can provide a temperature significantly lower than that required by the reboiler. Therefore, the existing steam distillation system is less energy efficient, and in addition, when the heat of condensation of the overhead material is discharged by a cooling tower, a large amount of water is consumed.
  • the main object of the present invention is to overcome the problems of the prior distillation system, and to provide a new distillation system and a distillation method, the technical problem to be solved is to enable the distillation of materials without substantially driving the external heat source.
  • the process which significantly increases the energy efficiency of the distillation system and saves water resources, is more suitable for practical use.
  • a distillation system comprising: a generator having a heat exchanger for concentrating an absorption solution and generating a vapor; a condenser having a heat exchanger therein; and an evaporator a heat exchanger; an absorber having a heat exchanger therein, the heat exchanger of the absorber being connected to the heat exchanger of the generator to form a heat circulation loop for conveying heat generated in the absorber to occur
  • a collecting crystallizer receiving an absorption solution from the absorber and/or the generator and cooling, forming an absorption crystallization and crystallization of the absorption solution, the post-crystallization absorption solution is sent to a generator, and the absorption agent is crystallized and conveyed To the absorber; and a distillation column, which is provided with a heat exchanger connected to the evaporator of the overhead line to form an overhead recycle loop, and a heat exchanger connected to the
  • the foregoing distillation 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 solution and/or the absorbent crystal after crystallization or The absorption solution containing the crystal of the absorbent is subjected to heat exchange.
  • the foregoing distillation 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 distillation system further comprises: an absorption solution from the heat exchanger for exchanging the absorption solution from the absorber with the absorption crystal of the absorbent from the absorbent crystallizer or the absorption solution containing the absorbent crystal.
  • the foregoing distillation system further comprises: an absorption solution from the heat exchanger for performing the absorption solution from the absorber with the crystallization solution of the absorption crystallization solution and the absorbent from the absorbent crystallizer or the absorption solution containing the crystallization of the absorbent. Heat exchange.
  • the absorption solution from the generator and the absorption solution from the absorber are mixed and then enter the absorption solution from the heat exchanger, and the crystallization solution and the absorbent from the absorption crystallizer are crystallized or The absorption solution containing the crystal of the absorbent is subjected to heat exchange.
  • the heat circulation circuit is provided with an external heat source heating device for compensating for a shortage of heat of the generator due to heat loss or the like.
  • the aforementioned steaming system further comprises a compression refrigeration device comprising an absorbent crystallizer-evaporator, a compressor, an absorption solution heat exchange-condenser, a throttle valve and a compression refrigeration refrigerant pipe, A cooling amount is supplied to the above absorbent crystallizer.
  • a compression refrigeration device comprising an absorbent crystallizer-evaporator, a compressor, an absorption solution heat exchange-condenser, a throttle valve and a compression refrigeration refrigerant pipe, A cooling amount is supplied to the above absorbent crystallizer.
  • the above evaporation apparatus is used, which comprises the following steps:
  • the absorption solution from the generator absorbs vapor from the evaporator and generates absorption heat, while the concentration of the absorption solution is lowered and sent to the absorbent crystallizer;
  • the foregoing distillation method further comprises: before the crystallization, the absorbing solution is sent to the generator, and before the absorbing solution output by the absorber is cooled, the absorbing solution output by the absorber is absorbed after the crystallization.
  • the solution is subjected to heat exchange.
  • the foregoing steaming method further comprises: before the crystallization of the absorbent is transported to the absorber, and before the absorption solution output by the absorber is cooled, the absorbent crystal or the absorption solution containing the absorbent crystal is The absorption solution output by the absorber performs heat exchange.
  • the foregoing distillation method further comprises: before the crystallization of the absorption solution after the crystallization is delivered to the generator, before the crystallization of the absorbent is delivered to the absorber, and before the absorption solution of the absorber is cooled, the output of the absorber
  • the absorbing solution exchanges heat with the crystallization solution and the absorbing agent crystals or the absorbing solution containing the absorbing agent.
  • the foregoing steaming method further comprises: before the crystallization is carried out before the absorbing solution is sent to the generator, before the crystallization of the absorbent is delivered to the absorber, before the absorption solution of the absorber is cooled, and the generator output Before the absorption solution is delivered 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 crystallized absorption solution and the absorbent are crystallized or absorbed.
  • the crystallization solution of the agent is subjected to heat exchange.
  • heat is compensated to the generator by an external heat source during the thermal cycle of the step (6).
  • the cooling amount required for the crystallization of the absorption solution is provided to the above step (5) by a compression refrigeration cycle.
  • the temperature of the crystallization solution in the step (5) is -18 to 32 °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 distillation system and the distillation method of the present invention convert the heat of condensation of the distillation column overhead into a heat source for raising the temperature of the bottom liquid by using an absorption heat pump cycle, and the steam distillation system has The absorbent crystallizer, and thus the heat generated by the absorber, is directly supplied to the absorption heat pump cycle which is substantially self-supply through the thermal circulation circuit, thereby effectively saving energy and water resources, thereby being more suitable for practical use.
  • Figure 1 is a flow chart of a prior art steaming system.
  • Figure 2 is a flow chart of the distillation system of Example 1 of the present invention.
  • Figure 3 is a flow chart of the distillation system of Example 1 of the present invention.
  • Figure 4 is a flow chart of a distillation system of Example 3 of the present invention.
  • Fig. 5 is a flow chart showing the steaming system of the fourth embodiment of the present invention.
  • Figure 6 is a flow chart of a distillation system of Example 5 of the present invention.
  • bottom liquid outlet 404 bottom liquid line
  • the distillation system mainly comprises a generator 11, a condenser 12, an evaporator 13, an absorber 14, an absorption solution self-heat exchanger 150, an absorbent crystallizer 141, a mixer 142, and a distillation column 410.
  • a water-lithium bromide working medium is circulated between the generator 11 and the absorber 14 as an absorbing solution.
  • the generator 11 is used for concentrating the absorption solution, and is provided therein with a heat exchanger 110, in which the heat cycle working medium from the heat exchanger 140 in the absorber 14 is passed, as an absorption solution.
  • the lithium bromide solution is heated to evaporate the working water, so that the lithium bromide concentration of the absorbing solution is increased, and the high-temperature vapor generated by the lithium bromide is output to the condenser 12 through the vapor passage 19.
  • Generator 11 outlet The 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 absorbing solution is circulated between the generator 11 and the absorber 14 by absorbing the solution pipes 20, 30.
  • the condenser 12 is provided with a heat exchanger 120.
  • the heat exchanger 120 is connected to the bottom liquid line 404 of the distillation column 410 to form a bottom liquid circulation circuit, so that the bottom liquid output from the distillation tower passes through the condenser 12.
  • the heat exchanger 120 is then returned to the distillation column, which is heated and heated in the heat exchanger 120. Therefore, the condenser 12 and the heat exchanger 120 function as a reboiler. After the vapor in the condenser 12 exchanges heat with the bottom liquid, it is condensed into condensed water and sent to the evaporator 13 through the condensed water pipe 17.
  • a bottom liquid outlet 403 is also provided on the bottom liquid line 404 for outputting the product of the distillation system.
  • the evaporator 13 is provided with a heat exchanger 130.
  • the heat exchanger 130 is connected to the overhead line 402 of the distillation column 410 to form an overhead circulation loop for evaporating the overhead product.
  • the heat exchanger 130 of the unit 13 is post-condensed and a part is refluxed into the distillation column, so that the evaporator 13 and the heat exchanger 130 function as an overhead condenser.
  • an overheads outlet 405 is provided on the overhead recycle loop for outputting the overhead product of the distillation system. In the evaporator 13, the heat released from the overhead distills the condensed water from the condenser 12 into a vapor and is sent to the absorber 14 through the vapor passage 18.
  • the absorber 14 is provided with a heat exchanger 140.
  • the absorption solution from the generator 11 absorbs the vapor from the evaporator 13 and generates heat of absorption, thereby increasing 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 are connected by a thermal cycle fluid conduit 60 to form a thermal circuit, so that the heat of absorption generated by the absorber 14 is supplied to the generator 11 as a driving heat source of the generator.
  • the heat cycle circuit is a heat pipe circulation circuit, and at this time, the installation position of the generator 11 is higher than the installation position of the absorber 14.
  • the heat medium can form a 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, a crystallization 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 through the absorption solution from the heat exchanger 150, and the absorption solution outlet of the absorption crystallizer is connected to the heat exchanger 150 via the absorption solution.
  • the absorbing solution inlet of the vessel 11 is connected to the absorbing solution inlet of the absorber 11 by the crystallization outlet of the absorbent crystallizer.
  • 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 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, and the lower the crystallization temperature is, the lower the equilibrium concentration of the lithium bromide in the liquid phase is.
  • the lithium bromide concentration of the liquid phase after crystallization can reach or approach the equilibrium concentration of lithium bromide at the cooling temperature. Cooling junction After the crystal is subjected to solid-liquid separation, the crystallization after absorption solution in the absorbent crystallizer 141, that is, the lithium bromide diluted solution, is sent from the heat exchanger 15 G to the generator 11 through the absorption solution through the absorption solution.
  • the above-mentioned absorbent crystallizer 141 may be a cold source of 0 to 32 ° C cooling water.
  • the steamed pylon 410 is provided with a feed line 401, the top of which is provided with an overhead line 402, and the heat exchanger 130 connected to the evaporator forms an overhead loop, and in the cycle
  • An overhead outlet 405 is arranged on the circuit;
  • a bottom liquid line 404 is arranged at the bottom of the distillation tower, and the heat exchanger 120 connected to the condenser forms a bottom liquid circulation loop, and a tower is arranged on the circulation loop.
  • Base outlet 403. The distillation of the material is carried out in a distillation column.
  • the steaming system of the first embodiment except for the necessary power equipment, basically does not need to provide a special driving heat source for heating the bottom liquid, and the distillation process of the material can be performed.
  • the absorbing solution forms an absorbent crystal in the absorbent crystallizer 141 and absorbs the solution after crystallization.
  • the absorbent crystals described in this Example 1 and the following examples are not intended to limit them 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 also as follows.
  • FIG. 3 is a flowchart of Embodiment 2 of the present invention.
  • the absorbing solution is supplied from the heat exchanger 150 for heat exchange of the absorbing solution from the absorber 14 with the absorbing agent (or the absorbing solution containing the crystallization of the absorbing agent) output from the absorbing agent crystallizer 141.
  • 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 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.
  • 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).
  • the absorption solution is sent to the generator 11 through the absorption solution input pipe 30.
  • 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.
  • 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 there is shown a flow chart of the distillation system of Example 5 of the present invention.
  • the distillation system is substantially 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 compressed refrigerant is condensed in the absorption solution heat exchange-condenser 220, and is vaporized in the absorbent crystallization-evaporator 200 via the throttle valve 230, thereby providing a low-temperature cooling amount to the absorbent crystallizer 141.
  • Absorbent Crystallization - Evaporator 200 The vapor of the outlet compressed refrigerant is compressed by the compressor 210 and then passed to the absorption solution heat exchange-condenser 220, thereby completing the compression refrigeration cycle.
  • the lithium bromide concentration of the absorption solution after the solid-liquid separation of the absorbent crystallizer 141 is lowered.
  • the absorption solution that is, the lithium bromide solution
  • the crystallization solution absorption pipe 50 passes through the crystallization solution absorption pipe 50, and the absorption solution heat exchange condenser 220 and the absorption solution are introduced into the generator 11 from the heat exchanger 150.
  • the crystal-containing solution after the solid-liquid separation of the absorbent crystallizer 141 passes through the crystallization-containing pipe 40, and is introduced into the mixer 142 from the heat exchanger 150 through the absorption solution heat-condenser 220 and the absorption solution.
  • the absorption solution from the heat exchanger 150 functions to exchange heat between the higher temperature absorption solution from the absorber and the lower temperature crystallization absorption solution and the crystal containing solution from the absorbent crystallizer, thereby increasing the supply generator 11
  • the solution temperature of the 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 exchange with the crystal-containing solution is performed to condense the above-mentioned refrigerant vapor, and at the same time partially or completely melt the lithium bromide crystal and raise the temperature of the solution.
  • the concentrate of the generator 11 whose concentration of lithium bromide is increased by concentration of the generator 11 is introduced into the mixer 142 through the absorption solution pipe 20 to be mixed with the crystallization-containing solution, 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. The drive heat is derived from the supplied absorption heat pump process, which is cooled by the generator 11 The condenser 12 provides steam for heating the bottoms.
  • the distilling system of this embodiment can achieve distillation of the material without substantially requiring a dedicated reboiler to drive the heat source.
  • Embodiment 6 of the present invention proposes a distillation method in which the distillation material is subjected to distillation separation using the distillation system described in the above embodiment, and the distillation method comprises the following steps:
  • the material is transferred from the feed line 401 to the distillation column, distilled in the distillation column, the overhead is output from the top of the distillation column, and the bottom liquid is output from the bottom of the distillation column.
  • the absorption solution from the generator absorbs the vapor from the evaporator and generates absorption heat, while the concentration of the absorption solution is lowered and sent to the absorbent crystallizer;
  • the bottom liquid is output from the bottom liquid outlet 403; the overhead is output from the overhead outlet 405 to control a suitable reflux ratio.
  • the distillation product is obtained from the bottom liquid outlet 403 and the overheads outlet 405.
  • 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 from the absorber before the solution is cooled.
  • the absorbing solution output by the absorber is The absorbent is crystallized and crystallized to absorb the solution for heat exchange.
  • 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 crystallization process of the absorbent is carried out in the above method, and the crystallization solution and the absorbent are crystallized (or the crystallization solution) are output by the absorption solution output from the absorber 14 (or the generator) and the absorbent crystallizer 141.
  • the heat exchange is performed to significantly increase the working concentration of lithium bromide absorbed by the absorber 14 under the premise of maintaining the working concentration of the solution lithium bromide, so that a higher temperature absorption heat can be obtained in the absorber 14, thereby This heat of absorption can be used as the driving heat of the generator 11 and the operating temperature of the generator 11 is higher, that is, a higher temperature vapor can be generated.
  • 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 continuation of the entire heat pump cycle.
  • the distillation method of this example is collectively constructed.
  • Another embodiment of the present invention provides a distillation method which is substantially the same as that of the embodiment 6, except that the low-temperature cooling required for the crystallization of the absorption solution in the absorbent crystallizer 141 comes from compression refrigeration.
  • the cycle process Specifically, the vapor of the absorbent 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 present embodiment is cooled by the absorption solution heat exchange-condenser 220, the cooling amount of the outlet solution of the lithium bromide crystallizer 141 is relatively close, so that the evaporation temperature and the condensation temperature of the cycle are relatively close. Reachable To a higher coefficient of refrigeration performance. That is, the compression refrigeration cycle of the present embodiment consumes less energy.
  • the temperature of the cooled crystallization provided by the absorbing solution during the compression refrigeration cycle is -18 to 7 °C.
  • the technical solution described in the above embodiments of the present invention is not particularly limited in the type of the absorption solution to be used.
  • the above embodiments are all described by taking an aqueous solution of lithium-bromide as an absorption solution.
  • the absorbent is one or more of LiBr, LiCl, LiN0 3 , NaBr, KBr, CaCl 2 , MgBr 2 and ZnCl 2 a mixture of substances.
  • Example 6 the method described in Example 6 is used to distill the aqueous ethanol solution to a water content of 50% (mass percentage), and the working fluid in the thermal cycle is heated by using 160 ° C saturated steam as an external heat source.
  • the dihydrazyl silicone oil is used as the thermal cycle working medium, and the absorbent crystallizer 141 is cooled by the cooling water of 20 °C.
  • Example 7 the method described in Example 7 is used to steam the ethanol aqueous solution, the water content is 50% (mass percentage), and the working fluid in the thermal cycle is heated by using 160 ° C saturated steam as an external heat source.
  • the di-n-based silicone oil is used as the thermal cycle working medium, and the compression refrigeration medium provided by the compression refrigeration cycle is used to cool the absorption.
  • Agent crystallizer 141 Table 1 below shows the operating parameters and performance of the above example 1-2.
  • Thermal outlet heat cycle temperature (°C) 155. 4 155. 4 Apparatus As described above, it is merely a preferred embodiment of the present invention, and does not impose any form limitation on the present invention, although the present invention has The preferred embodiments are disclosed above, but are not intended to limit the present invention. Any one skilled in the art can make some changes or modifications to the equivalents without departing from the technical scope of the present invention. The present invention is not limited to the details of the technical solutions of the present invention, and any modifications, equivalent changes and modifications made 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
  • the distillation system and the distillation method of the present invention convert the condensation heat of the distillation column overhead into a heat source for raising the temperature of the bottom liquid by using an absorption heat pump cycle, and the distillation system has an absorbent crystallizer, and further The heat generated by the absorber is directly supplied to the generator through the thermal circulation loop, so that the externally driven heat source can be substantially eliminated in the absorption heat pump cycle, and the absorption heat pump cycle that drives the heat source to be substantially self-supply can be realized, thereby effectively saving energy and water resources. , thus more suitable for practical use.

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Crystallography & Structural Chemistry (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)

Abstract

A distillation system comprises a generator (11), a condenser (12), an evaporator (13), an absorber (14), a crystallizer (141) for absorbent and a distillation column (410). The heat exchanger (140) of the absorber (14) connects with the heat exchanger (110) of the generator (11) to form a heat circulation loop, which was used to transfer the heat produced by the absorber (14) to the generator (11). The absorbing solution inlet of the crystallizer (141) for absorbent connects with the absorbing solution outlet of the absorber (14). The outlet of after-crystallization absorbing solution of the absorbent crystallizer (141) for absorbent connects with the absorbing solution inlet of the generator (11). The crystal outlet of the crystallizer (141) for absorbent connects with the absorbing solution inlet of the absorber (14). The overhead product line (402) of the distillation column (410) connects with the heat exchanger (130) of the evaporator (13) to form an overhead circulation loop, while the bottom product line (404) of the distillation column (410) connects with the heat exchanger (120) of the condenser (12) to form a bottom circulation loop. A distillation method uses the distillation system.

Description

蒸馏系统以及蒸馏方法 技术领域  Distillation system and distillation method
本发明涉及一种化工领域的蒸馏技术， 特别涉及一种在无外部驱动热 源条件下进行蒸馏的蒸馏系统以及蒸馏方法。 背景技术  The present invention relates to a distillation technique in the chemical field, and more particularly to a distillation system and a distillation method for performing distillation without externally driven heat sources. Background technique
请参阅图 1所示， 是现有的蒸馏系统的流程图。 其由蒸馏塔 300、 冷却 器 310、物料循环储罐 320以及再沸器 330组成。该蒸傭塔 300用于将物料 中的组分进行分离， 蒸馏塔的塔顶设有冷凝器 310,低沸点组分从蒸馏塔顶 输出后在冷凝器 310中冷却， 进入物料回流储罐 320, —部分物料输出， 一 部分物料回流至蒸馏塔 300 内。 蒸馏塔 300的塔底输出高沸点组分， 一部 分物料输出， 一部分物料经再沸器 330加热后输送到蒸馏塔中， 继续进行 蒸 》  Please refer to Figure 1, which is a flow chart of the existing distillation system. It consists of a distillation column 300, a chiller 310, a material recycle tank 320, and a reboiler 330. The steaming tower 300 is used for separating components in the material. The top of the distillation column is provided with a condenser 310. The low boiling component is output from the top of the distillation column and then cooled in the condenser 310 to enter the material return storage tank 320. , - part of the material output, a part of the material is returned to the distillation column 300. The bottom of the distillation column 300 outputs a high boiling component, a part of the material is output, and a part of the material is heated by the reboiler 330 and sent to the distillation column to continue to be steamed.
上述的现有蒸馏系统， 其需要有热源提供给再沸器 330用于使蒸馏塔 的塔底物料温度升高， 且需要有冷源提供给蒸馏塔塔顶的冷凝器 310 用于 使物料降温。 该蒸馏系统的冷凝器 310是向外界输出热量， 但该热量并无 法被再沸器所利用， 因为冷凝器可提供的温度明显低于再沸器需要的温度。 所以， 现有的蒸镏系统的能量效率较低， 此外， 当塔顶物料的冷凝热采用 冷却塔加以排放时， 还需要消耗大量的水资源。 发明内容  The above-mentioned prior distillation system requires a heat source to be supplied to the reboiler 330 for raising the temperature of the bottom material of the distillation column, and a condenser 310 for supplying a cold source to the top of the distillation column is required for cooling the material. . The condenser 310 of the distillation system outputs heat to the outside, but this heat is not utilized by the reboiler because the condenser can provide a temperature significantly lower than that required by the reboiler. Therefore, the existing steam distillation system is less energy efficient, and in addition, when the heat of condensation of the overhead material is discharged by a 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馏系统存在的问题， 而提供一种 新的蒸馏系统以及蒸馏方法，所要解决的技术问题是使其能够在基本无需 外部驱动热源的条件下进行物料的蒸馏过程， 从而显著提高蒸馏系统的能 量效率， 并节约水资源， 更加适于实用。  The main object of the present invention is to overcome the problems of the prior distillation system, and to provide a new distillation system and a distillation method, the technical problem to be solved is to enable the distillation of materials without substantially driving the external heat source. The process, which significantly increases the energy efficiency of the distillation system and saves water resources, is 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馏系统， 其包括： 发生器， 其内设有换热器， 用于浓 缩吸收溶液并产生蒸气； 冷凝器， 其内设有换热器； 蒸发器， 其内设有换 热器； 吸收器， 其内设有换热器， 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； 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， 所述的结晶后吸收溶液输送至发生器， 所述 的吸收剂结晶输送至吸收器； 以及蒸馏塔， 其设有塔顶馏出物管线连接于 蒸发器的换热器， 形成塔顶馏出物循环回路， 还设有塔底液管线连接于冷 凝器的换热器， 形成塔底液循环回路。 The object of the present invention and solving the technical problems thereof are achieved by the following technical solutions. A distillation system according to the present invention, comprising: a generator having a heat exchanger for concentrating an absorption solution and generating a vapor; a condenser having a heat exchanger therein; and an evaporator a heat exchanger; an absorber having a heat exchanger therein, the heat exchanger of the absorber being connected to the heat exchanger of the generator to form a heat circulation loop for conveying heat generated in the absorber to occur In the device a collecting crystallizer, receiving an absorption solution from the absorber and/or the generator and cooling, forming an absorption crystallization and crystallization of the absorption solution, the post-crystallization absorption solution is sent to a generator, and the absorption agent is crystallized and conveyed To the absorber; and a distillation column, which is provided with a heat exchanger connected to the evaporator of the overhead line to form an overhead recycle loop, and a heat exchanger connected to the condenser , forming a bottom liquid circulation loop.
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， 前述的蒸馏系统还包括： 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 distillation 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 solution and/or the absorbent crystal after crystallization or The absorption solution containing the crystal of the absorbent is subjected to heat exchange.
优选的， 前述的蒸馏系统还包括： 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 distillation 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， 前述的蒸馏系统还包括： 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 distillation system further comprises: an absorption solution from the heat exchanger for exchanging the absorption solution from the absorber with the absorption crystal of the absorbent from the absorbent crystallizer or the absorption solution containing the absorbent crystal.
优选的， 前述的蒸馏系统还包括： 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 distillation system further comprises: an absorption solution from the heat exchanger for performing the absorption solution from the absorber with the crystallization solution of the absorption crystallization solution and the absorbent from the absorbent crystallizer or the absorption solution containing the crystallization of the absorbent. Heat exchange.
优选的， 前述的蒸馏系统， 所述的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, in the foregoing distillation system, the absorption solution from the generator and the absorption solution from the absorber are mixed and then enter the absorption solution from the heat exchanger, and the crystallization solution and the absorbent from the absorption crystallizer are crystallized or The absorption solution containing the crystal of the absorbent is subjected to heat exchange.
优选的， 前述的蒸馏系统， 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 distillation system, wherein the heat circulation circuit is provided with an external heat source heating device for compensating for a shortage of heat of the generator due to heat loss or the like.
优选的， 前述的蒸愤系统， 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, the aforementioned steaming system further comprises a compression refrigeration device comprising an absorbent crystallizer-evaporator, a compressor, an absorption solution heat exchange-condenser, a throttle valve and a compression refrigeration refrigerant pipe, A cooling amount is supplied to the above absorbent crystallizer.
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馏方法， 釆用上述的蒸发装置， 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 a distillation method proposed by the present invention, the above evaporation apparatus is used, 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冷 凝器， 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 condenser, the concentrated absorption solution being sent to the absorber;
( 2 )将蒸馏塔塔底液输送到冷凝器中加热， 然后输送回蒸馏塔， 来自 发生器的蒸气在冷凝器中冷凝为冷凝水， 并将该冷凝水输送至蒸发器；(2) conveying the bottom liquid of the distillation column to the condenser for heating, and then transporting it back to the distillation column, from The vapor of the generator is condensed into condensed water in the condenser, and the condensed water is sent to the evaporator;
( 3 )将蒸馏塔的塔顶熘出物输送到蒸发器中放热并冷凝， 然后一部分 回流至蒸馏塔， 来自冷凝器的冷凝水在蒸发器中蒸发为蒸气， 并将该蒸气 输送至吸收器中； (3) conveying the overhead of the distillation column to the evaporator for exotherm and condensation, and then a part of the reflux to the distillation column, the condensed water from the condenser is evaporated into vapor in the evaporator, and the vapor is sent to the absorption In the device;
( 4 ) 来自发生器的吸收溶液吸收来自蒸发器的蒸气并产生吸收热， 同 时吸收溶液浓度降低并被输送至吸收剂结晶器中；  (4) the absorption solution from the generator absorbs vapor from the evaporator 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； 以及  (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， 前述的蒸馏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 distillation method further comprises: before the crystallization, the absorbing solution is sent to the generator, and before the absorbing solution output by the absorber is cooled, the absorbing solution output by the absorber is absorbed after the crystallization. The solution is subjected to heat exchange.
优选的， 前述的蒸熘方法还包括： 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 steaming method further comprises: before the crystallization of the absorbent is transported to the absorber, and before the absorption solution output by the absorber is cooled, the absorbent crystal or the absorption solution containing the absorbent crystal is The absorption solution output by the absorber performs heat exchange.
优选的， 前述的蒸馏方法还包括： 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 distillation method further comprises: before the crystallization of the absorption solution after the crystallization is delivered to the generator, before the crystallization of the absorbent is delivered to the absorber, and before the absorption solution of the absorber is cooled, the output of the absorber The absorbing solution exchanges heat with the crystallization solution and the absorbing agent crystals or the absorbing solution containing the absorbing agent.
优选的， 前述的蒸熘方法还包括： 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 steaming method further comprises: before the crystallization is carried out before the absorbing solution is sent to the generator, before the crystallization of the absorbent is delivered to the absorber, before the absorption solution of the absorber is cooled, and the generator output Before the absorption solution is delivered 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 crystallized absorption solution and the absorbent are crystallized or absorbed. The crystallization solution of the agent is subjected to heat exchange.
优选的， 前述的蒸榴方法， 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偿热量。 优选的， 前述的蒸馏方法， 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, in the aforementioned steaming method, heat is compensated to the generator by an external heat source during the thermal cycle of the step (6). Preferably, in the above-described distillation method, the cooling amount required for the crystallization of the absorption solution is provided to the above step (5) by a compression refrigeration cycle.
优选的， 前述的蒸熘方法， 所述的步骤（5 ) 中的吸收溶液冷却结晶的 温度为 -18 ~ 32 °C。  Preferably, in the above steaming method, the temperature of the crystallization solution in the step (5) is -18 to 32 °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，本发明的蒸馏系统以及蒸馏方法， 由于采用了吸收式热泵循环将蒸镏 塔塔顶馏出物的冷凝热转化为对塔底液升温的热源， 并且本蒸熘系统具有 了吸收剂结晶器，进而吸收器所产生的热量通过热循环回路直接供给发生 基本自供的吸收式热泵循环， 从而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 distillation system and the distillation method of the present invention convert the heat of condensation of the distillation column overhead into a heat source for raising the temperature of the bottom liquid by using an absorption heat pump cycle, and the steam distillation system has The absorbent crystallizer, and thus the heat generated by the absorber, is directly supplied to the absorption heat pump cycle which is substantially self-supply through the thermal circulation circuit, thereby effectively saving energy and water resources, thereby being 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是现有的蒸镏系统的流程图。  Figure 1 is a flow chart of a prior art steaming system.
图 2是本发明实施例 1的蒸馏系统的流程图。  Figure 2 is a flow chart of the distillation system of Example 1 of the present invention.
图 3是本发明实施例 1的蒸馏系统的流程图。  Figure 3 is a flow chart of the distillation system of Example 1 of the present invention.
图 4是本发明实施例 3的蒸馏系统的流程图。  Figure 4 is a flow chart of a distillation system of Example 3 of the present invention.
图 5是本发明实施例 4的蒸镏系统的流程图。  Fig. 5 is a flow chart showing the steaming system of the fourth embodiment of the present invention.
图 6是本发明实施例 5的蒸馏系统的流程图。  Figure 6 is a flow chart of a distillation system of Example 5 of the present invention.
11 : 发生器 12 : 冷凝器  11 : Generator 12 : Condenser
1 3: 蒸发器 14 : 吸收器  1 3: Evaporator 14 : Absorber
17 : 冷凝水管道 18、 19 : 蒸气通路  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 200 吸收剂结晶-蒸发器 210 压缩机 150: absorption solution from heat exchanger 160: external heat source heating device 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 300 蒸馏塔  240 Compressed Refrigerant Pipeline 300 Distillation Tower
310 冷却器 320 物料循环储罐  310 cooler 320 material circulation tank
330 再沸器 410 蒸馏塔  330 reboiler 410 distillation tower
401 进料管线 402 塔顶镏出物管线  401 Intake Line 402 Tower Top Drainage Line
403 塔底液出口 404： 塔底液管线  403 bottom liquid outlet 404: bottom liquid line
405 塔顶馏出物出口 实现发明的最佳方式  405 Top Distillate Outlet 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馏系统以及蒸馏方 法其具体实施方式、 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, characteristics and the distillation system and distillation method according to the present invention will be described below with reference to the accompanying drawings and preferred embodiments. Efficacy, detailed description as follows.
请参阅图 2所示， 是本发明实施例 1的蒸镏系统的流程图。 该蒸馏系 统主要包括发生器 11、 冷凝器 12、 蒸发器 13、 吸收器 14、 吸收溶液自换 热器 150、 吸收剂结晶器 141、 混合器 142以及蒸镏塔 410。 发生器 11和吸 收器 14之间循环有水-溴化锂工质对作为吸收溶液。  Referring to Fig. 2, there is shown a flow chart of the steaming system of the first embodiment of the present invention. The distillation system mainly comprises a generator 11, a condenser 12, an evaporator 13, an absorber 14, an absorption solution self-heat exchanger 150, an absorbent crystallizer 141, a mixer 142, and a distillation column 410. A water-lithium bromide working medium is circulated between the generator 11 and the absorber 14 as an absorbing solution.
所述的发生器 11用于浓缩吸收溶液， 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 的溴化锂溶液进行加热使工质水蒸发， 从而使吸收溶液的溴化锂浓度提高， 其所产生的高温蒸气通过蒸气通路 19输出至冷凝器 12中。 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。  The generator 11 is used for concentrating the absorption solution, and is provided therein with a heat exchanger 110, in which the heat cycle working medium from the heat exchanger 140 in the absorber 14 is passed, as an absorption solution. The lithium bromide solution is heated to evaporate the working water, so that the lithium bromide concentration of the absorbing solution is increased, and the high-temperature vapor generated by the lithium bromide is output to the condenser 12 through the vapor passage 19. Generator 11 outlet The 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 absorbing solution is circulated between the generator 11 and the absorber 14 by absorbing the solution pipes 20, 30.
所述的冷凝器 12内设有换热器 120， 该换热器 120连接蒸馏塔 410的 塔底液管线 404 , 形成塔底液循环回路， 使蒸馏塔输出的塔底液经冷凝器 12的换热器 120后返回到蒸镏塔内，该塔底液在换热器 120内被加热升温， 所以， 冷凝器 12以及换热器 120充当了再沸器的作用。 冷凝器 12内的蒸 气与塔底液进行换热后， 冷凝为冷凝水， 并通过冷凝水管道 17输送到蒸发 器 1 3中。 另外， 还在塔底液管线 404上设有塔底液出口 403用于输出该蒸 馏系统的产品。 所述的蒸发器 13内设有换热器 130, 该换热器 130连接于蒸馏塔 410 的塔顶馏出物管线 402 , 形成塔顶馏出物循环回路，使塔顶馏出物经蒸发器 13的换热器 130后冷凝， 一部分回流至蒸馏塔内， 所以， 蒸发器 13以及换 热器 130充当了塔顶冷凝器的作用。 另外， 在塔顶馏出物循环回路上设有 塔顶馏出物出口 405， 用于输出该蒸馏系统的塔顶产品。在该蒸发器 13内， 塔顶馏出物放出的热量使来自冷凝器 12的冷凝水蒸发为蒸气， 并通过蒸气 通路 18输送至吸收器 14中。 The condenser 12 is provided with a heat exchanger 120. The heat exchanger 120 is connected to the bottom liquid line 404 of the distillation column 410 to form a bottom liquid circulation circuit, so that the bottom liquid output from the distillation tower passes through the condenser 12. The heat exchanger 120 is then returned to the distillation column, which is heated and heated in the heat exchanger 120. Therefore, the condenser 12 and the heat exchanger 120 function as a reboiler. After the vapor in the condenser 12 exchanges heat with the bottom liquid, it is condensed into condensed water and sent to the evaporator 13 through the condensed water pipe 17. In addition, a bottom liquid outlet 403 is also provided on the bottom liquid line 404 for outputting the product of the distillation system. The evaporator 13 is provided with a heat exchanger 130. The heat exchanger 130 is connected to the overhead line 402 of the distillation column 410 to form an overhead circulation loop for evaporating the overhead product. The heat exchanger 130 of the unit 13 is post-condensed and a part is refluxed into the distillation column, so that the evaporator 13 and the heat exchanger 130 function as an overhead condenser. Additionally, an overheads outlet 405 is provided on the overhead recycle loop for outputting the overhead product of the distillation system. In the evaporator 13, the heat released from the overhead distills the condensed water from the condenser 12 into a vapor and is sent to the absorber 14 through the vapor passage 18.
所述的吸收器 14内设有换热器 140，来自发生器 11的吸收溶液吸收来 自蒸发器 13的蒸气并产生吸收热，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。  The absorber 14 is provided with a heat exchanger 140. The absorption solution from the generator 11 absorbs the vapor from the evaporator 13 and generates heat of absorption, thereby increasing 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 are connected by a thermal cycle fluid conduit 60 to form a thermal circuit, so that the heat of absorption generated by the absorber 14 is supplied to the generator 11 as a driving heat source of the generator. In the present embodiment, the heat cycle circuit is a heat pipe circulation circuit, and at this time, the installation position of the generator 11 is higher than the installation position of the absorber 14. In the heat pipe circulation, the heat medium can form a 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.
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、 结 晶后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 的结晶后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结晶 温度时会出现结晶， 结晶温度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。 冷却结 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 15 G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 0 ~ 32 °C的冷却水。 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, a crystallization 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 through the absorption solution from the heat exchanger 150, and the absorption solution outlet of the absorption crystallizer is connected to the heat exchanger 150 via the absorption solution. The absorbing solution inlet of the vessel 11 is connected to the absorbing solution inlet of the absorber 11 by the crystallization outlet of the absorbent crystallizer. 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, and the lower the crystallization temperature is, the lower the equilibrium concentration of the lithium bromide in the liquid phase is. Therefore, by cooling the crystal, Regardless of 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. Cooling junction After the crystal is subjected to solid-liquid separation, the crystallization after absorption solution in the absorbent crystallizer 141, that is, the lithium bromide diluted solution, is sent from the heat exchanger 15 G to the generator 11 through the absorption solution through the absorption solution. The above-mentioned absorbent crystallizer 141 may be a cold source of 0 to 32 ° C cooling water.
所述的蒸榴塔 410，其设有进料管线 401 ,塔顶设有塔顶馏出物管线 402， 连接于蒸发器的换热器 130形成塔顶镏出物循环回路， 并在该循环回路上 设有塔顶馏出物出口 405; 在蒸馏塔底部设有塔底液管线 404 , 连接于冷凝 器的换热器 120， 形成塔底液循环回路， 并在该循环回路上设有塔底液出口 403。 物料的蒸馏过程在蒸馏塔内进行。  The steamed pylon 410 is provided with a feed line 401, the top of which is provided with an overhead line 402, and the heat exchanger 130 connected to the evaporator forms an overhead loop, and in the cycle An overhead outlet 405 is arranged on the circuit; a bottom liquid line 404 is arranged at the bottom of the distillation tower, and the heat exchanger 120 connected to the condenser forms a bottom liquid circulation loop, and a tower is arranged on the circulation loop. Base outlet 403. The distillation of the material is carried out in a distillation column.
本实施例 1 的蒸镏系统除必要的动力设备外， 基本不需要提供专门的 驱动热源用于加热塔底液， 即可进行物料的蒸馏过程。  The steaming system of the first embodiment, except for the necessary power equipment, basically does not need to provide a special driving heat source for heating the bottom liquid, and the distillation process of the material can be performed.
吸收溶液在吸收剂结晶器 141 中形成吸收剂结晶和结晶后吸收溶液。 本实施例 1 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 forms an absorbent crystal in the absorbent crystallizer 141 and absorbs the solution after crystallization. The absorbent crystals described in this Example 1 and the following examples are not intended to limit them 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 also 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。 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. 3, which is a flowchart of Embodiment 2 of the present invention. The absorbing solution is supplied from the heat exchanger 150 for heat exchange of the absorbing solution from the absorber 14 with the absorbing agent (or the absorbing solution containing the crystallization of the absorbing agent) output from the absorbing agent crystallizer 141. 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 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. 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. After the heat transfer, the absorption solution is sent to the generator 11 through the absorption solution input pipe 30. 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的蒸馏系统的流程图。 本实施例提 出的蒸馏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 210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。 Referring to Figure 6, there is shown a flow chart of the distillation system of Example 5 of the present invention. This embodiment provides The distillation system is substantially 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 compressed refrigerant is condensed in the absorption solution heat exchange-condenser 220, and is vaporized in the absorbent crystallization-evaporator 200 via the throttle valve 230, thereby providing a low-temperature cooling amount to the absorbent crystallizer 141. Absorbent Crystallization - Evaporator 200 The vapor of the outlet compressed refrigerant is compressed by the compressor 210 and then passed to the absorption solution heat exchange-condenser 220, thereby completing the compression refrigeration cycle.
由于部分溴化锂结晶析出， 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 后的含结晶溶液通过含结晶溶液管道 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 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结晶溶液进行热交换， 从而使上述制冷工质蒸气冷 凝， 同时部分或全部融解溴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中与含结晶溶液混合，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，实现驱动热源自供的吸收式热泵过程， 由发生器 11 对冷 凝器 12提供蒸气用于加热塔底液。 Since a part of the lithium bromide crystals are precipitated, the lithium bromide concentration of the absorption solution after the solid-liquid separation of the absorbent crystallizer 141 is lowered. After the crystallization, the absorption solution, that is, the lithium bromide solution, passes through the crystallization solution absorption pipe 50, and the absorption solution heat exchange condenser 220 and the absorption solution are introduced into the generator 11 from the heat exchanger 150. On the other hand, the crystal-containing solution after the solid-liquid separation of the absorbent crystallizer 141 passes through the crystallization-containing pipe 40, and is introduced into the mixer 142 from the heat exchanger 150 through the absorption solution heat-condenser 220 and the absorption solution. The absorption solution from the heat exchanger 150 functions to exchange heat between the higher temperature absorption solution from the absorber and the lower temperature crystallization absorption solution and the crystal containing solution from the absorbent crystallizer, thereby increasing the supply generator 11 The solution temperature of the 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 exchange with the crystal-containing solution is performed to condense the above-mentioned refrigerant vapor, and at the same time partially or completely melt the lithium bromide crystal and raise the temperature of the solution. The concentrate of the generator 11 whose concentration of lithium bromide is increased by concentration of the generator 11 is introduced into the mixer 142 through the absorption solution pipe 20 to be mixed with the crystallization-containing solution, 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. The drive heat is derived from the supplied absorption heat pump process, which is cooled by the generator 11 The condenser 12 provides steam for heating the bottoms.
本实施例的蒸镏系统可以在基本不需要专门的再沸器驱动热源的情况 下， 实现对物料的蒸馏。  The distilling system of this embodiment can achieve distillation of the material without substantially requiring a dedicated reboiler to drive the heat source.
本发明的实施例 6提出了一种蒸馏方法， 采用上述实施例所述的蒸馏 系统对以蒸馏物料进行蒸馏分离， 该蒸熘方法包括以下步骤：  Embodiment 6 of the present invention proposes a distillation method in which the distillation material is subjected to distillation separation using the distillation system described in the above embodiment, and the distillation method comprises the following steps:
物料从进料管线 401 输送到蒸熘塔中， 在蒸镏塔内进行蒸馏， 从蒸馏 塔塔顶输出塔顶馏出物， 从蒸馏塔塔底输出塔底液。  The material is transferred from the feed line 401 to the distillation column, distilled in the distillation column, the overhead is output from the top of the distillation column, and the bottom liquid is output from the bottom of the distillation column.
( 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冷 凝器， 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 condenser, the concentrated absorption solution being sent to the absorber;
( 2 )将蒸餾塔塔底液通过塔底液管线 404 输送到冷凝器的换热器 120 中加热， 然后输送回蒸镏塔， 来自发生器的蒸气在冷凝器中冷凝为冷凝水， 并将该冷凝水输送至蒸发器；  (2) The distillation column bottom liquid is sent to the heat exchanger 120 of the condenser through the bottom liquid line 404 for heating, and then sent back to the steaming tower, and the vapor from the generator is condensed into condensed water in the condenser, and The condensed water is delivered to the evaporator;
( 3 )将蒸馏塔的塔顶馏出物通过塔顶镏出物管线 402输送到蒸发器的 换热器 130 中放热并冷凝， 然后一部分回流至蒸熘塔， 来自冷凝器的冷凝 水在蒸发器中蒸发为蒸气， 并将该蒸气输送至吸收器中；  (3) The overhead of the distillation column is sent to the heat exchanger 130 of the evaporator through the overhead vapor line 402 to exotherm and condense, and then a portion is refluxed to the distillation column, and the condensed water from the condenser is Evaporating into a vapor in the evaporator and delivering the vapor to the absorber;
( 4 )来自发生器的吸收溶液吸收来自蒸发器的蒸气并产生吸收热， 同 时吸收溶液浓度降低并被输送至吸收剂结晶器中；  (4) the absorption solution from the generator absorbs the vapor from the evaporator 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， 所述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） 与来自发生器的浓缩后的吸收溶 液混合后输送至吸收器中； 以及  (5) performing absorption crystallization and solid-liquid separation in an absorbent crystallizer to form an absorption crystallization and crystallization of the absorption solution, the crystallization solution is transported to the generator, and the absorbent is crystallized (or contains absorption) The crystallization solution of the agent is mixed with the concentrated absorption solution from the generator and sent 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.
塔底液从塔底液出口 403输出一部分； 塔顶馏出物从塔顶馏出物出口 405输出一部分， 以便控制合适的回流比。从塔底液出口 403和塔顶馏出物 出口 405处得到蒸馏产物。  The bottom liquid is output from the bottom liquid outlet 403; the overhead is output from the overhead outlet 405 to control a suitable reflux ratio. The distillation product is obtained from the bottom liquid outlet 403 and the overheads outlet 405.
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, before the crystallization of the absorbent is delivered to the absorber, and the absorption of the absorber is absorbed The absorbent crystals exchange heat with the absorption solution output from the absorber before the solution 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吸收剂结晶和结晶后吸收溶液进行换热。  Preferably, before the crystallization of the absorbing solution is sent to the generator, before the crystallization of the absorbing agent is delivered to the absorber, and the absorbing solution output by the absorber is cooled, the absorbing solution output by the absorber is The absorbent is crystallized and crystallized to absorb the solution for heat exchange.
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.
由于在上述的方法中具有吸收剂结晶过程， 并且通过对吸收器 14 (或 者和发生器）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 （或含结晶溶液）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 温度更高的蒸气。  Since the crystallization process of the absorbent is carried out in the above method, and the crystallization solution and the absorbent are crystallized (or the crystallization solution) are output by the absorption solution output from the absorber 14 (or the generator) and the absorbent crystallizer 141. The heat exchange is performed to significantly increase the working concentration of lithium bromide absorbed by the absorber 14 under the premise of maintaining the working concentration of the solution lithium bromide, so that a higher temperature absorption heat can be obtained in the absorber 14, thereby This heat of absorption can be used as the driving heat of the generator 11 and the operating temperature of the generator 11 is higher, that is, a higher temperature vapor can be generated.
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 保证整个热泵循环过程的持续进行。 共同构成本实施例的蒸馏方法。  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 continuation of the entire heat pump cycle. The distillation method of this example is collectively constructed.
本发明的实施例 7提供了另一种蒸馏方法，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。 Another embodiment of the present invention provides a distillation method which is substantially the same as that of the embodiment 6, except that the low-temperature cooling required for the crystallization of the absorption solution in the absorbent crystallizer 141 comes from compression refrigeration. The cycle process. Specifically, the vapor of the absorbent 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 present embodiment is cooled by the absorption solution heat exchange-condenser 220, the cooling amount of the outlet solution of the lithium bromide crystallizer 141 is relatively close, so that the evaporation temperature and the condensation temperature of the cycle are relatively close. Reachable To a higher coefficient of refrigeration performance. That is, the compression refrigeration cycle of the present embodiment consumes less energy. The temperature of the cooled crystallization provided by the absorbing solution 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-溴化锂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 ZnCl2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 is not particularly limited in the type of the absorption solution to be used. The above embodiments are all described by taking an aqueous solution of lithium-bromide as an absorption solution. In other embodiments, It is also possible to use a mixture of one or more of water, sterol and ethanol; the absorbent is one or more of LiBr, LiCl, LiN0 3 , NaBr, KBr, CaCl 2 , MgBr 2 and ZnCl 2 a mixture of substances.
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。 实例 1  The feasibility of the above embodiments will be explained below by way of examples with specific parameters. Example 1
本实例采用实施例 6 所述的方法， 对乙醇水溶液进行蒸馏， 其水含量 为 50% (质量百分含量）， 釆用 160°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。 实例 2  In this example, the method described in Example 6 is used to distill the aqueous ethanol solution to a water content of 50% (mass percentage), and the working fluid in the thermal cycle is heated by using 160 ° C saturated steam as an external heat source. In order to compensate for the insufficient heat of the generator driving heat source due to heat loss or the like, the dihydrazyl silicone oil is used as the thermal cycle working medium, and the absorbent crystallizer 141 is cooled by the cooling water of 20 °C. Example 2
本实例采用实施例 7 所述的方法， 对乙醇水溶液进行蒸傭， 其水含量 为 50% (质量百分含量）， 采用 160°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。 下表 1为上述实例 1-2的工作参数和性能。  In this example, the method described in Example 7 is used to steam the ethanol aqueous solution, the water content is 50% (mass percentage), and the working fluid in the thermal cycle is heated by using 160 ° C saturated steam as an external heat source. In order to compensate for the insufficient heat of the generator-driven heat source caused by heat loss, etc., the di-n-based silicone oil is used as the thermal cycle working medium, and the compression refrigeration medium provided by the compression refrigeration cycle is used to cool the absorption. Agent crystallizer 141. Table 1 below shows the operating parameters and performance of the above example 1-2.
表 1  Table 1
Figure imgf000014_0001
凝 换热器出口温度.（ ° ) 86 95 器 压力 (kPa) 61 89 蒸 换热器进口温度（ 'C ) 75 75 发 换热器出口温度（ °C ) 75 75 ^ 压力 (kPa) 36. 1 36. 1
Figure imgf000014_0001
Condensing heat exchanger outlet temperature. ( ° ) 86 95 Pressure (kPa) 61 89 Steam heat exchanger inlet temperature ( 'C ) 75 75 Heat exchanger outlet temperature ( °C ) 75 75 ^ Pressure (kPa) 36. 1 36. 1
换热器入口热循环工质温度（°C ) 151. 0 151. 0  Heat exchanger inlet thermal cycle working temperature (°C) 151. 0 151. 0
吸 换热器出口热循环工质温度（ V ) 155. 0  Suction heat exchanger outlet thermal cycle working fluid temperature (V) 155. 0
收 进口溴化锂浓度 ( wt% ) 75 75 哭 出口溴化锂浓度 ( wt% ) 72 72  Receiving imported lithium bromide concentration (wt%) 75 75 crying export lithium bromide concentration (wt%) 72 72
压力 (kPa) 36. 0 36. 0  Pressure (kPa) 36. 0 36. 0
蒸 塔顶馏出物水含量（wt% ) 30 ■ 10 馏 塔底液水含量（ wt% ) 98 100 塔 塔顶回流比 1. 0 1. 0 吸收  Steam column overhead water content (wt%) 30 ■ 10 Distillation bottom liquid water content (wt%) 98 100 tower top reflux ratio 1. 0 1. 0 absorption
剂结 吸收剂结晶-蒸发器温度（ °C ) 20 -18 进口热循环工质温度（ °C )  Agent knot Absorber crystallization - evaporator temperature ( ° C ) 20 -18 inlet thermal cycle working temperature ( ° C )
力口热 出口热循环工质温度（ °C ) 155. 4 155. 4 装置 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 的任何筒单修改、 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  Thermal outlet heat cycle temperature (°C) 155. 4 155. 4 Apparatus As described above, it is merely a preferred embodiment of the present invention, and does not impose any form limitation on the present invention, although the present invention has The preferred embodiments are disclosed above, but are not intended to limit the present invention. Any one skilled in the art can make some changes or modifications to the equivalents without departing from the technical scope of the present invention. The present invention is not limited to the details of the technical solutions of the present invention, and any modifications, equivalent changes and modifications made 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
本发明的蒸馏系统以及蒸馏方法， 由于采用了吸收式热泵循环将蒸熘 塔塔顶馏出物的冷凝热转化为对塔底液升温的热源， 并且本蒸馏系统具有 了吸收剂结晶器，进而吸收器所产生的热量通过热循环回路直接供给发生 器， 因而可以在吸收式热泵循环中基本省去外部驱动热源， 实现驱动热源 基本自供的吸收式热泵循环， 从而有效地节约了能源和水资源， 从而更加 适于实用。  The distillation system and the distillation method of the present invention convert the condensation heat of the distillation column overhead into a heat source for raising the temperature of the bottom liquid by using an absorption heat pump cycle, and the distillation system has an absorbent crystallizer, and further The heat generated by the absorber is directly supplied to the generator through the thermal circulation loop, so that the externally driven heat source can be substantially eliminated in the absorption heat pump cycle, and the absorption heat pump cycle that drives the heat source to be substantially self-supply can be realized, thereby effectively saving energy and water resources. , thus more suitable for practical use.

Claims

权 利 要 求 Rights request
1、 一种蒸馏系统， 其特征在于其包括： A distillation system characterized in that it comprises:
发生器， 其内设有换热器（110 ), 用于浓缩吸收溶液并产生蒸气； 冷凝器， 其内设有换热器（120 );  a generator having a heat exchanger (110) for concentrating the absorption solution and generating a vapor; a condenser having a heat exchanger (120) therein;
蒸发器， 其内设有换热器（130 );  An evaporator having a heat exchanger (130) therein;
吸收器， 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吸收热输送至发生器中； 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， 所述的结晶后吸收溶液输送至发生器， 所述的吸收剂结晶输送至吸收器； 以及  An absorber having a heat exchanger (140) connected thereto, and the heat exchanger (140) is connected to the heat exchanger (110) to form a heat circulation circuit for conveying the heat of absorption generated in the absorber to the generator The absorbent crystallizer receives the absorption solution from the absorber and/or the generator and cools to form an absorption solution after crystallization and crystallization of the absorbent, and the crystallization solution is transported to the generator, the absorbent Crystallization to the absorber;
蒸馏塔， 其设有塔顶馏出物管线连接于换热器（130 )， 形成塔顶馏出 物循环回路， 还设有塔底液管线连接于换热器 （ 120 )， 形成塔底液循环回 路。  a distillation column, which is provided with an overhead line connected to the heat exchanger (130) to form an overhead distillation circuit, and a bottom liquid line connected to the heat exchanger (120) to form a bottom liquid Loop circuit.
2、 根据权利要求 1所述的蒸馏系统， 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 distillation system according to claim 1, further comprising: 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所述的蒸熘系统， 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 evaporating system according to claim 1, further comprising: an absorption solution from the heat exchanger for crystallizing or containing an absorbent from the absorber and an absorbent from the absorbent crystallizer The crystallized absorption solution undergoes heat exchange.
5、 根据权利要求 1所述的蒸爐系统， 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 steaming furnace system according to claim 1, further comprising: an absorption solution from the heat exchanger for absorbing the absorption solution from the absorber with the post-crystallization absorption solution and the absorbent from the absorbent crystallizer The crystallization or absorption solution containing the crystallization of the absorbent is subjected to heat exchange.
6、 根据权利要求 5所述的蒸馏系统， 其特征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。 6. The distillation 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 crystallization solution and the absorption solution from the absorbent crystallizer are Absorbent crystallization or absorption solution containing absorbent crystals Heat exchange.
7、 根据权利要求 1 ~ 6任一项所述的蒸镏系统， 其特征在于其中所迷 的热循环回路上设有外部热源加热装置。  7. A distilling system according to any one of claims 1 to 6, wherein the thermal circuit is provided with an external heat source heating means.
8、 根据权利要求 1 ~ 6任一项所述的蒸馏系统， 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。  The distillation system according to any one of claims 1 to 6, further comprising an crystallization 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.
9、 一种蒸熘方法， 采用权利要求 1-8任一项所述的蒸 系统， 其包括 以下步骤：  9. A method of steaming, using the steaming system of any of claims 1-8, comprising the steps of:
( 1 )在发生器中浓缩吸收溶液同时产生蒸气， 并将上述蒸气输送至冷 凝器， 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 condenser, the concentrated absorption solution being sent to the absorber;
( 2 )将蒸熘塔塔底液输送到冷凝器中加热， 然后输送回蒸馏塔， 来自 发生器的蒸气在冷凝器中冷凝为冷凝水， 并将该冷凝水输送至蒸发器； (2) conveying the bottom of the steaming tower to the condenser for heating, and then returning it to the distillation column, the vapor from the generator is condensed into condensed water in the condenser, and the condensed water is sent to the evaporator;
( 3 )将蒸镏塔的塔顶馏出物输送到蒸发器中放热并冷凝， 然后一部分 回流至蒸馏塔， 来自冷凝器的冷凝水在蒸发器中蒸发为蒸气， 并将该蒸气 输送至吸收器中； (3) conveying the overhead of the distillation column to the evaporator for exotherm and condensation, and then returning a portion to the distillation column, the condensed water from the condenser is evaporated into vapor in the evaporator, and the vapor is sent to In the absorber;
( 4 )来自发生器的吸收溶液吸收来自蒸发器的蒸气并产生吸收热， 同 时吸收溶液浓度降低并被输送至吸收剂结晶器中；  (4) the absorption solution from the generator absorbs the vapor from the evaporator 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与来自发生器的浓缩后的吸收溶 液混合后输送至吸收器中；  (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 mixed with the concentrated absorption solution from the generator and sent 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.
10、 根据权利要求 9 所述的蒸馏方法， 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。  10. The distillation method according to claim 9, further comprising: said absorber output before said crystallization of the absorption solution is sent to the generator before the absorption solution of the absorber is cooled. The absorbing solution exchanges heat with the crystallization solution after the crystallization.
11、 根据权利要求 9 所述的蒸馏方法， 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。 11. The distillation method according to claim 9, further comprising: crystallization or inclusion of said absorbent before said absorbing agent is crystallized and transported to said absorber, and said absorbing solution outputted by said absorber is cooled Absorbent crystallization of the absorption solution and absorption of the absorber output The solution is taken for heat exchange.
12、 根据权利要求 9 所述的蒸馏方法， 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。  12. The distillation method according to claim 9, further comprising: before the crystallization solution is transported to the generator after the crystallization, the crystallization of the absorbent is sent to the absorber, and the absorption solution output from the absorber is cooled. Previously, the absorption solution outputted by the absorber exchanges heat with the crystallization solution and the absorbent crystal or the absorption solution containing the absorber crystal.
1 3、 根据权利要求 12所述的蒸馏方法， 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。  The distillation method according to claim 12, further comprising: cooling the absorption solution output from the absorber before the crystallization of the absorbent is sent to the absorber before the crystallization is sent to the generator after the crystallization is performed. 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.
14、 根据权利要求 9-13任一项所述的蒸條方法， 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偿热量。  The steaming bar method according to any one of claims 9 to 13, characterized in that during the thermal cycle of the step (6), heat is compensated to the generator by an external heat source.
15、 根据权利要求 9- 13任一项所述的蒸榴方法， 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 distilling method according to any one of claims 9 to 13, characterized in that the step (5) of the above-mentioned step (5) is supplied with a cooling amount required for cooling the crystal by a compression refrigeration cycle.
9、 根据权利要求 9-13任一项所述的蒸馏方法， 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 ~ 32 °C。  The distillation method according to any one of claims 9 to 13, characterized in that the temperature at which the absorption solution in the step (5) is cooled and crystallized is -18 to 32 °C.
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