CN113694553A - Printing and dyeing weak alkali solution absorption type heat pump multi-effect distillation system and working method thereof - Google Patents
Printing and dyeing weak alkali solution absorption type heat pump multi-effect distillation system and working method thereof Download PDFInfo
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- CN113694553A CN113694553A CN202110948187.8A CN202110948187A CN113694553A CN 113694553 A CN113694553 A CN 113694553A CN 202110948187 A CN202110948187 A CN 202110948187A CN 113694553 A CN113694553 A CN 113694553A
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
- B01D3/143—Fractional distillation or use of a fractionation or rectification column by two or more of a fractionation, separation or rectification step
- B01D3/146—Multiple effect distillation
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
- B01D3/32—Other features of fractionating columns ; Constructional details of fractionating columns not provided for in groups B01D3/16 - B01D3/30
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
- F25B15/00—Sorption machines, plants or systems, operating continuously, e.g. absorption type
- F25B15/02—Sorption machines, plants or systems, operating continuously, e.g. absorption type without inert gas
- F25B15/06—Sorption machines, plants or systems, operating continuously, e.g. absorption type without inert gas the refrigerant being water vapour evaporated from a salt solution, e.g. lithium bromide
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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- Y02B—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO BUILDINGS, e.g. HOUSING, HOUSE APPLIANCES OR RELATED END-USER APPLICATIONS
- Y02B30/00—Energy efficient heating, ventilation or air conditioning [HVAC]
- Y02B30/52—Heat recovery pumps, i.e. heat pump based systems or units able to transfer the thermal energy from one area of the premises or part of the facilities to a different one, improving the overall efficiency
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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Abstract
The invention discloses a printing and dyeing weak alkali solution absorption heat pump multi-effect distillation system and a working method thereof. The method comprises the following steps: the waste heat of the medium-temperature wastewater is used for driving an absorption heat pump, the evaporator of the absorption heat pump is used for recovering the condensation heat of the last-effect steam of the multi-effect distillation system, and the high-temperature lithium bromide solution from the absorber is used for evaporating the condensation water again to obtain the high-temperature steam driven multi-effect distillation system. By arranging the energy storage device, the heat energy recovered by the absorption heat pump can be stored when no water treatment is required, and then the heat is released to drive the multi-effect distillation system when no intermediate-temperature wastewater exists, so that peak staggering use is realized. The invention recovers the heat of the medium-temperature wastewater, can greatly reduce the energy consumption in the evaporation process of the printing and dyeing light alkali, and can effectively reduce the energy waste and the environmental influence caused by the discharge of the wastewater into the environment.
Description
Technical Field
The invention relates to a printing and dyeing weak alkali solution absorption heat pump multi-effect distillation system and a working method thereof, in particular to a method for recovering intermediate-temperature waste water waste heat by utilizing a second-type absorption heat pump system to drive a double-effect distillation system to carry out distillation and concentration on weak alkali solution.
Background
China is the first major country of textile printing and dyeing industry, and the textile printing and dyeing industry is a waste water discharge household, which accounts for about 35 percent of the whole industrial waste water discharge amount, and the printing and dyeing waste water discharge amount is about 3 multiplied by 10 every day6m3～4×106m3. The water temperature of different process flows in the printing and dyeing industry is different, the water temperature of the desizing process is 98 ℃, the discharge temperature of the waste water is 95 ℃, the water temperature of the cleaning process is 80-90 ℃, the discharge temperature of the waste water is 75-85 ℃, and the medium-temperature waste water contains a large amount of waste heat. In the process of utilizing energy, a large part of the energy is not effectively utilized, and the part of the energy which is not utilized is often released into the atmosphere or a water body in the form of heat, so that the environment is thermally polluted. The waste heat of the printing and dyeing industrial wastewater is fully utilized, and the method is the most main measure for reducing the thermal pollution of the printing and dyeing industry. The recovery and utilization of light alkali liquor in the dyeing process in the printing and dyeing industry is always an important technological problem for the printing and dyeing industry and environmental protection, and the conventional method is to heat, concentrate and recycle the light alkali liquor. The traditional single-effect distillation concentration method has the disadvantages of large steam consumption, high equipment investment cost and poor economy.
Disclosure of Invention
The invention provides a printing and dyeing weak alkali solution absorption type heat pump multi-effect distillation system aiming at the problems.
In order to realize the purpose of the invention, the technical scheme adopted by the invention is as follows:
a printing and dyeing weak lye absorption heat pump multi-effect distillation system comprises a multi-effect distillation circulation system and an absorption heat pump circulation system, wherein the multi-effect distillation circulation system comprises: a first centrifugal pump 101, a first preheater 102, a second preheater 103, a third preheater 104, a first evaporator 105 and a second evaporator 106, wherein the printing and dyeing weak lye is communicated with the inlet of the first centrifugal pump 101 through a pipeline, the outlet of the first centrifugal pump 101 is connected with the inlet a1 of the first preheater 102 through a pipeline, the outlet a2 of the first preheater 102 is connected with the inlet b1 of the second preheater 103 through a pipeline, the outlet b2 of the second preheater 103 is connected with the inlet c1 of the third preheater 104 through a pipeline, the outlet c2 of the third preheater 104 is connected with the solution inlet d1 of the first evaporator 105 through a pipeline, the solution outlet d2 of the first evaporator 105 is connected to the solution inlet e1 of the second evaporator 106 through a first pressure reducing valve 107 by a pipeline, the outlet of the condensed water d4 of the first evaporator 105 is connected to the inlet c3 of the third preheater 104 by a pipeline, and the steam outlet d5 of the first evaporator 105 is connected to the steam inlet e3 of the second evaporator 106 by a pipeline; the solution outlet e2 of the second evaporator 106 is connected to the inlet a3 of the first preheater 102 by a pipeline, and the condensed water outlet e4 of the second evaporator 106 is connected to the inlet b3 of the second preheater 103 by a pipeline;
the absorption heat pump circulation system comprises: a generator 201, a condenser 202, a second centrifugal pump 203, a third evaporator 204, a fourth evaporator 205, an absorber 206, a fifth evaporator 207, an accumulator 208, a fourth preheater 209, and a third centrifugal pump 210; the medium-temperature waste water is connected with an inlet o1 of the generator 201 through a pipeline, an outlet o2 of the generator 201 is connected to an inlet j4 of the first evaporator 204 through a pipeline, an outlet j3 of the first evaporator 204 is connected with a discharge pipeline, a steam outlet o4 of the generator 201 is connected with an inlet k1 of the condenser 202 through a pipeline, an outlet k2 of the condenser 202 is connected to an inlet j6 of the first evaporator 204 through a pipeline by the second centrifugal pump 203, an outlet j5 of the first evaporator 204 is connected to an inlet f5 of the second evaporator 205 through a pipeline, and an outlet f6 of the second evaporator 205 is connected to a steam inlet m2 of the absorber 206 through a pipeline; the concentrated lithium bromide solution outlet o5 of the generator 201 is connected to the inlet i4 of the fourth preheater 209 through a pipeline via the third centrifugal pump 210, and the outlet i3 of the fourth preheater 209 is connected to the concentrated solution inlet m1 of the absorber 206 through a pipeline; a lithium bromide dilute solution outlet m3 of the absorber 206 is connected to an inlet h3 of the third evaporator 207 through a pipeline, an outlet h4 of the third evaporator 207 is connected to a heat storage pipeline inlet n1 of the energy accumulator 208 through a pipeline, an outlet n2 of the energy accumulator 208 is connected to an inlet i1 of the fourth preheater 209 through a pipeline, and an outlet i2 of the fourth evaporator 209 is connected to a lithium bromide dilute solution inlet o3 of the generator 201 through a pipeline and a second pressure reducing valve 211;
the top secondary steam outlet e5 of the second evaporator 106 is connected to the inlet f1 of the fourth evaporator 205 through a pipeline, the outlet f2 of the fourth evaporator 205 is connected to the inlet of the fourth centrifugal pump 301 through a pipeline, the outlet of the fourth centrifugal pump 301 is connected to the inlet h1 of the fifth evaporator 207 through a pipeline by the first stop valve 303, the outlet h2 of the fifth evaporator 207 is connected to the inlet g1 of the gas-liquid separator 302 through a pipeline by the second stop valve 304, the steam outlet g2 of the gas-liquid separator 302 is connected to the steam inlet d3 of the first evaporator 105 through a pipeline, and the water outlet g3 of the gas-liquid separator 302 is connected to the inlet pipeline of the fourth centrifugal pump 301 through a pipeline by the third stop valve 305;
the system make-up water is connected to an inlet j1 of the third evaporator 204 through a pipeline sequentially through an electric regulating valve 401 and a fifth centrifugal pump 402, an outlet j2 of the third evaporator 204 is connected to an inlet f3 of the second evaporator 205 through a pipeline, and an outlet f4 of the second evaporator 205 is connected to an inlet pipeline of the fourth centrifugal pump 301 through a pipeline;
further, the outlet of the fourth centrifugal pump 301 is also connected to the inlet n3 of the accumulator 208 through a fourth stop valve 306 by a pipeline, and the outlet n4 of the accumulator 208 is connected to the inlet g1 of the gas-liquid separator 302 through a fifth stop valve 307 by a pipeline;
further, a liquid level controller 308 is arranged in the gas-liquid separator 302, a temperature controller 309 is arranged on an outlet pipeline of the gas-liquid separator 302, and the liquid level controller 308 and the temperature controller 309 are connected with an electric regulating valve 401 through signal lines;
further, the energy storage phase change material used by the energy storage 208 is Mg (NO)3)·2H2O or NaNO3─LiNO3A graphite composite energy storage material;
further, the multi-effect distillation circulating system is arranged into a two-effect distillation circulating system, a three-effect distillation circulating system or a four-effect distillation circulating system according to the concentration of the weak alkali liquor;
further, the first preheater 102 is also provided with a concentrated solution outlet a 4; the second preheater 103 is also provided with a condensed water outlet b 4; the third preheater 104 is also provided with a condensed water outlet c 4; the condenser 202 is also provided with a cooling water outlet k3 and a low-temperature cooling water inlet k 4;
the working method of the printing and dyeing weak alkali solution absorption type heat pump multi-effect distillation system comprises a combined operation mode, an energy storage mode and a distillation treatment mode;
firstly, a combined operation mode:
when medium-temperature wastewater exists in a printing and dyeing mill and weak alkali liquor needs to be treated, a combined operation mode is started, and the specific method comprises the following steps: opening a first stop valve 303, a second stop valve 304, a third stop valve 305 and an electric control valve 401, closing a fourth stop valve 306 and a fifth stop valve 307, enabling the dilute light alkali solution to enter the first centrifugal pump 101 for pressurization, then sequentially passing through the first preheater 102, the second preheater 103 and the third preheater 104 for preheating, then entering the first evaporator 105, enabling the steam generated after the dilute light alkali solution in the first evaporator 105 is heated to flow into the second evaporator 106 from an outlet d5 at the top of the first evaporator 105, enabling the dilute light alkali solution to flow out from an outlet d2 of the first evaporator 105, reducing the pressure by a first pressure reducing valve 107, then continuing entering the second evaporator 106 for heat exchange, and enabling the condensed water to flow into the third preheater 104 for heat exchange from an outlet d4 of the first evaporator 105; the weak alkali concentrated solution in the second evaporator 106 flows into the first preheater 102 from the inlet of the outlet e2 of the second evaporator 106 for heat exchange, the condensed water flows into the second preheater 103 for heat exchange from the outlet e4 of the second evaporator 106, the secondary steam flows into the fourth evaporator 205 from the outlet e5 of the second evaporator 106 for heat exchange, the liquefied condensed water enters the second centrifugal pump 301 for pressure rise, then enters the fifth evaporator 207 for heat absorption and vaporization into saturated steam, and enters the gas-liquid separator 302 through the second stop valve 304, and the water vapor flows into the first evaporator 105 from the outlet g2 of the gas-liquid separator 302 to continue the next cycle; the reheated secondary steam cannot meet the operation of the two-effect distillation circulation system, the steam needs to be supplemented, the make-up water enters the fifth centrifugal pump 402 through the electric regulating valve 401, is preheated through the third evaporator 204 and the fourth evaporator 205 in sequence after being boosted, is mixed with the condensed water flowing out of the outlet f2 of the fourth evaporator 205, and enters the second centrifugal pump 301 for pressurization.
The medium-temperature wastewater enters the generator 201 for heat exchange, then enters the third evaporator 204 for continuous heat exchange, and then is discharged from an outlet j3 of the third evaporator 204; dilute lithium bromide solution in the generator 201 is heated to generate low-pressure working medium water vapor, the water vapor flows into the condenser 202 from an outlet o4 of the generator 201, exchanges heat with low-temperature cooling water and is condensed into saturated water, the saturated water enters the third evaporator 204 after being boosted by the fourth centrifugal pump 203 to exchange heat with medium-temperature wastewater and then enters the fourth evaporator 205 to exchange heat with secondary steam, and the saturated water enters the absorber 206 after being boosted to exchange heat and mass; the concentrated lithium bromide solution flows into the third centrifugal pump 210 from the outlet o5 of the generator 201 to be boosted, then enters the fourth preheater 209 to exchange heat, and enters the absorber 206 to exchange heat and mass after the temperature is increased; in the absorber 206, the high-pressure working medium steam is absorbed by the concentrated solution to generate a large amount of absorption heat, so that the temperature of the lithium bromide solution in the absorber 206 is increased rapidly; the heated dilute lithium bromide solution enters a fifth evaporator 207 for heat exchange, the dilute lithium bromide solution with the reduced temperature enters an energy storage device 208 for heat exchange with an energy storage phase-change material, then the dilute lithium bromide solution enters a fourth preheater 209 for heat exchange, and finally the dilute lithium bromide solution enters a generator 201 for next circulation after being reduced in pressure by a second pressure reducing valve 211.
Second, energy storage mode
When medium-temperature wastewater exists in a printing and dyeing mill but no weak alkali liquor treatment requirement exists, an energy storage mode is started, and the specific method comprises the following steps: the first stop valve 303, the second stop valve 304, the third stop valve 305, the fourth stop valve 306, the fifth stop valve 307 and the electric control valve 401 are closed, the double-effect distillation cycle system is not operated, the absorption heat pump cycle system is operated alone, the process is the same as the combined operation mode, and the energy accumulator 208 is used for storing high-temperature heat for standby.
Third, distillation processing mode
When no medium temperature waste water is discharged from a printing and dyeing mill but light alkali liquor treatment is needed, a distillation treatment mode is started, and the specific method comprises the following steps: the third stop valve 305, the fourth stop valve 306, the fifth stop valve 307 and the electric control valve 401 are opened, the first stop valve 303 and the second stop valve 304 are closed, the absorption heat pump circulation system does not operate, the double-effect distillation circulation system operates independently, the treatment process of the weak base solution and the make-up water is the same as the combined operation mode, the difference is that the secondary steam generated in the second evaporator 106 enters the fourth evaporator 205 for heat exchange, then is mixed with the make-up water flowing out of the outlet f4 of the fourth evaporator 205 and enters the fourth centrifugal pump 301 for pressurization, then flows into the energy storage 208 through the fourth stop valve 306 for heat exchange with the energy storage phase change material, flows into the gas-liquid separator 302 through the fifth stop valve 307 after the temperature is increased, the separated liquid water is mixed with the secondary steam and the make-up water through the third stop valve 305, the water flows into the first evaporator 105 through the outlet g2 of the gas-liquid separator 302 for heat exchange, the generated water vapor flows into the second evaporator 106 for the next cycle.
Further, the opening degree of the electric regulating valve 401 is in inverse proportional regulating relation with the liquid level height in the gas-liquid separator 302, and the opening degree of the electric regulating valve 401 is in direct proportional regulating relation with the steam temperature at the outlet of the gas-liquid separator 302;
the second type of absorption heat pump belongs to a heating type heat pump, the temperature of output heat is higher than that of a driving heat source, but the output heat is less than that of the driving heat source. The multi-effect distillation system utilizes the pressure difference of the evaporator to recover the latent heat of the steam of the system per se so as to realize multiple times of evaporation and condensation, and is combined with the second-class absorption heat pump system to heat up and recycle the secondary steam generated by the final-stage evaporator of the multi-effect distillation system, so that the energy consumption in the evaporation process can be greatly reduced, the heat of a large amount of low-temperature wastewater generated in the printing and dyeing process can be effectively recovered, and the energy efficiency of the system is improved.
Drawings
FIG. 1 is a flow chart of the present invention.
In the figure: 101 is a first centrifugal pump, 102 is a first preheater, 103 is a second preheater, 104 is a third preheater, 105 is a first evaporator, 106 is a second evaporator, 107 is a first pressure reducing valve, 201 is a generator, 202 is a condenser, 203 is a second centrifugal pump, 204 is a third evaporator, 205 is a fourth evaporator, 206 is an absorber, 207 is a fifth evaporator, 208 is an accumulator, 209 is a fourth preheater, 210 is a third centrifugal pump, 301 is a fourth centrifugal pump, 302 is a gas-liquid separator, 303 is a first stop valve, 304 is a second stop valve, 305 is a third stop valve, 306 is a fourth stop valve, 307 is a fifth stop valve, 308 is a liquid level controller, 309 is a temperature controller, 401 is an electric control valve, 402 is a fifth centrifugal pump
Detailed Description
In order to make the aforementioned objects, features and advantages of the present invention comprehensible, embodiments accompanied with figures are described in further detail below.
A printing and dyeing weak lye absorption heat pump multi-effect distillation system comprises a multi-effect distillation circulation system and an absorption heat pump circulation system, wherein the multi-effect distillation circulation system comprises: a first centrifugal pump 101, a first preheater 102, a second preheater 103, a third preheater 104, a first evaporator 105 and a second evaporator 106, wherein the printing and dyeing weak lye is communicated with the inlet of the first centrifugal pump 101 through a pipeline, the outlet of the first centrifugal pump 101 is connected with the inlet a1 of the first preheater 102 through a pipeline, the outlet a2 of the first preheater 102 is connected with the inlet b1 of the second preheater 103 through a pipeline, the outlet b2 of the second preheater 103 is connected with the inlet c1 of the third preheater 104 through a pipeline, the outlet c2 of the third preheater 104 is connected with the solution inlet d1 of the first evaporator 105 through a pipeline, the solution outlet d2 of the first evaporator 105 is connected to the solution inlet e1 of the second evaporator 106 through a first pressure reducing valve 107, the outlet of the condensed water d4 of the first evaporator 105 is connected to the inlet c3 of the third preheater 104 through a pipeline, and the steam outlet d5 of the first evaporator 105 is connected to the steam inlet e3 of the second evaporator 106 through a pipeline; the solution outlet e2 of the second evaporator 106 is connected to the inlet a3 of the first preheater 102 by a pipeline, and the condensed water outlet e4 of the second evaporator 106 is connected to the inlet b3 of the second preheater 103 by a pipeline;
the absorption heat pump circulation system comprises: a generator 201, a condenser 202, a second centrifugal pump 203, a third evaporator 204, a fourth evaporator 205, an absorber 206, a fifth evaporator 207, an accumulator 208, a fourth preheater 209, and a third centrifugal pump 210; the medium-temperature waste water is connected with an inlet o1 of the generator 201 through a pipeline, an outlet o2 of the generator 201 is connected to an inlet j4 of the first evaporator 204 through a pipeline, an outlet j3 of the first evaporator 204 is connected with a discharge pipeline, a steam outlet o4 of the generator 201 is connected with an inlet k1 of the condenser 202 through a pipeline, an outlet k2 of the condenser 202 is connected to an inlet j6 of the first evaporator 204 through a pipeline by the second centrifugal pump 203, an outlet j5 of the first evaporator 204 is connected to an inlet f5 of the second evaporator 205 through a pipeline, and an outlet f6 of the second evaporator 205 is connected to a steam inlet m2 of the absorber 206 through a pipeline; the concentrated lithium bromide solution outlet o5 of the generator 201 is connected to the inlet i4 of the fourth preheater 209 through a pipeline via the third centrifugal pump 210, and the outlet i3 of the fourth preheater 209 is connected to the concentrated solution inlet m1 of the absorber 206 through a pipeline; a lithium bromide dilute solution outlet m3 of the absorber 206 is connected to an inlet h3 of the third evaporator 207 through a pipeline, an outlet h4 of the third evaporator 207 is connected to a heat storage pipeline inlet n1 of the energy accumulator 208 through a pipeline, an outlet n2 of the energy accumulator 208 is connected to an inlet i1 of the fourth preheater 209 through a pipeline, and an outlet i2 of the fourth preheater 209 is connected to a lithium bromide dilute solution inlet o3 of the generator 201 through a pipeline and a second pressure reducing valve 211;
the top secondary steam outlet e5 of the second evaporator 106 is connected to the inlet f1 of the fourth evaporator 205 through a pipeline, the outlet f2 of the fourth evaporator 205 is connected to the inlet of the fourth centrifugal pump 301 through a pipeline, the outlet of the fourth centrifugal pump 301 is connected to the inlet h1 of the fifth evaporator 207 through a pipeline by the first stop valve 303, the outlet h2 of the fifth evaporator 207 is connected to the inlet g1 of the gas-liquid separator 302 through a pipeline by the second stop valve 304, the steam outlet g2 of the gas-liquid separator 302 is connected to the steam inlet d3 of the first evaporator 105 through a pipeline, and the water outlet g3 of the gas-liquid separator 302 is connected to the inlet pipeline of the fourth centrifugal pump 301 through a pipeline by the third stop valve 305;
the system make-up water is connected to an inlet j1 of the third evaporator 204 through a pipeline sequentially through an electric regulating valve 401 and a fifth centrifugal pump 402, an outlet j2 of the third evaporator 204 is connected to an inlet f3 of the second evaporator 205 through a pipeline, and an outlet f4 of the second evaporator 205 is connected to an inlet pipeline of the fourth centrifugal pump 301 through a pipeline;
the outlet of the fourth centrifugal pump 301 is also connected to the inlet n3 of the accumulator 208 through a fourth stop valve 306 by a pipeline, the outlet n4 of the accumulator 208 is connected to the inlet g1 of the gas-liquid separator 302 through a fifth stop valve 307 by a pipeline, and when no intermediate-temperature wastewater is available, heat can be provided by using the energy-storage phase-change material in the accumulator 208;
a liquid level controller 308 is arranged in the gas-liquid separator 302, a temperature controller 309 is arranged on an outlet pipeline of the gas-liquid separator 302, and the liquid level controller 308 and the temperature controller 309 are connected with an electric regulating valve 401 through signal lines;
the energy storage phase-change material used by the energy storage 208 is Mg (NO)3)·2H2O or NaNO3─LiNO3The graphite composite energy storage material can store surplus heat generated by the absorption heat pump system;
the multi-effect distillation circulating system is arranged into a two-effect distillation circulating system, a three-effect distillation circulating system or a four-effect distillation circulating system according to the concentration of the light alkali liquor;
the first preheater 102 is also provided with a concentrated solution outlet a 4; the second preheater 103 is also provided with a condensed water outlet b 4; the third preheater 104 is also provided with a condensed water outlet c 4; the condenser 202 is also provided with a cooling water outlet k3 and a low-temperature cooling water inlet k 4;
a working method of a printing and dyeing weak alkali solution absorption type heat pump multi-effect distillation system comprises a combined operation mode, an energy storage mode and a distillation treatment mode;
firstly, a combined operation mode:
when medium-temperature wastewater exists in a printing and dyeing mill and weak alkali liquor needs to be treated, a combined operation mode is started, and the specific method comprises the following steps: opening a first stop valve 303, a second stop valve 304, a third stop valve 305 and an electric control valve 401, closing a fourth stop valve 306 and a fifth stop valve 307, enabling the dilute light alkali solution to enter the first centrifugal pump 101 for pressurization, then enter the first preheater 102 for preheating by the concentrated solution, enter the second preheater 103 and the third preheater 104 for preheating by the condensed water, enabling the dilute light alkali solution entering the first evaporator 105 to exchange heat with high-temperature steam, enabling the generated secondary steam to flow into the second evaporator 106 from an outlet d5 at the top of the first evaporator 105, enabling the dilute alkali solution to flow out from an outlet d2 of the first evaporator 105, enabling the dilute alkali solution to continue to enter the second evaporator 106 for heat exchange after being depressurized by a first pressure reducing valve 107, and enabling the condensed water to flow into the third preheater 104 for heat exchange through an outlet d4 of the first evaporator 105; the weak base concentrated solution in the second evaporator 106 flows into the first preheater 102 from the outlet e2 of the second evaporator 106 to exchange heat with the weak base dilute solution, the condensed water flows into the second preheater 103 from the outlet e4 of the second evaporator 106 to exchange heat, the secondary steam flows into the fourth evaporator 205 from the outlet e5 of the second evaporator 106 to release heat, the liquefied condensed water enters the second centrifugal pump 301 to be boosted, then enters the fifth evaporator 207 to absorb heat and vaporize into saturated steam, and enters the gas-liquid separator 302 through the second stop valve 304, and the water vapor flows into the first evaporator 105 from the outlet g2 of the gas-liquid separator 302 to continue the next cycle; the reheated secondary steam cannot meet the operation of the two-effect distillation circulation system, the steam needs to be supplemented, make-up water enters the fifth centrifugal pump 402 through the electric regulating valve 401, is preheated through the third evaporator 204 and the fourth evaporator 205 in sequence after being boosted, is mixed with condensed water flowing out of an outlet f2 of the fourth evaporator 205, and enters the second centrifugal pump 301 for pressurization;
the medium-temperature wastewater enters the generator 201 to exchange heat with a lithium bromide solution, then enters the third evaporator 204 to exchange heat with saturated water and make-up water, and then is discharged from an outlet j3 of the third evaporator 204; dilute lithium bromide solution in the generator 201 exchanges heat with medium-temperature wastewater to generate low-pressure working medium water vapor, the water vapor flows into the condenser 202 from an outlet o4 of the generator 201, exchanges heat with low-temperature cooling water and is condensed into saturated water, the saturated water enters the third evaporator 204 after being boosted by the fourth centrifugal pump 203 to exchange heat with the medium-temperature wastewater to form wet saturated vapor, then enters the fourth evaporator 205 to exchange heat with secondary vapor to form dry saturated vapor, and enters the absorber 206 after the temperature is raised to exchange heat and mass; dilute lithium bromide solution in the generator (201) is heated by medium-temperature wastewater to evaporate part of water to become concentrated lithium bromide solution, the concentrated lithium bromide solution flows into the third centrifugal pump 210 from an outlet o5 of the generator 201 to be boosted, then enters the fourth preheater 209 to exchange heat with the dilute solution, and enters the absorber 206 to exchange heat and mass after the temperature is raised; in the absorber 206, the high-pressure working medium steam is absorbed by the concentrated solution to generate a large amount of absorption heat, so that the temperature of the lithium bromide solution in the absorber 206 is increased rapidly; the heated dilute lithium bromide solution enters a fifth evaporator 207 for heat exchange, the dilute lithium bromide solution with the reduced temperature enters an energy storage device 208 for heat exchange with an energy storage phase-change material, part of heat is stored in the phase-change material, heat is provided in other working modes, the dilute lithium bromide solution enters a fourth preheater 209 for heat exchange with the concentrated lithium bromide solution, and finally the dilute lithium bromide solution is subjected to pressure reduction through a second pressure reducing valve 211 and then enters a generator 201 for next circulation;
second, energy storage mode
When medium-temperature wastewater exists in a printing and dyeing mill but no weak alkali liquor treatment requirement exists, an energy storage mode is started, and the specific method comprises the following steps: the first stop valve 303, the second stop valve 304, the third stop valve 305, the fourth stop valve 306, the fifth stop valve 307 and the electric control valve 401 are closed, and the double-effect distillation cycle system is not operated, and the absorption heat pump cycle system is operated alone, and the process thereof is the same as the above-mentioned combined operation mode, in order to use Mg (NO) (NO) for the purpose of using Mg (NO)3)·2H2An O accumulator for storing the high-temp heat generated by the absorber, Mg (NO)3)·2H2The phase transition temperature of O is 130 ℃, and the requirement that the steam temperature of a first evaporator of the two-effect distillation system is 127 ℃ can be met;
third, distillation processing mode
When no medium temperature waste water is discharged from a printing and dyeing mill but light alkali liquor treatment is needed, a distillation treatment mode is started, and the specific method comprises the following steps: the third stop valve 305, the fourth stop valve 306, the fifth stop valve 307 and the electric control valve 401 are opened, the first stop valve 303 and the second stop valve 304 are closed, the absorption heat pump circulating system does not operate, the two-effect distillation circulating system operates independently, the treatment process of the weak alkaline solution and the make-up water is the same as the combined operation mode, the difference is that the secondary steam generated in the second evaporator 106 enters the fourth evaporator 205 to exchange heat with the make-up water, then the secondary steam and the make-up water flowing out of the outlet f4 of the fourth evaporator 205 are mixed and enter the fourth centrifugal pump 301 to be pressurized, then the secondary steam flows into the energy storage 208 through the fourth stop valve 306, the energy storage phase change material generates a large amount of heat through phase change, the water solution changes into wet saturated steam after absorbing the heat, then the wet saturated steam flows into the gas-liquid separator 302 through the fifth stop valve 307 to separate liquid drops, the separated liquid water is mixed with the secondary steam and the make-up water through the third stop valve 305 to be circulated in the next step, the water vapor flows into the first evaporator 105 from the outlet g2 of the gas-liquid separator 302 to exchange heat with the weak base solution, and the generated water vapor flows into the second evaporator 106 to be circulated next time.
The opening of the electric control valve 401 is in inverse proportional adjustment relation with the liquid level height in the gas-liquid separator 302, when the liquid level height in the gas-liquid separator 302 is high, the liquid water quantity is sufficient, at the moment, the valve opening of the electric control valve 401 needs to be reduced, the make-up water flow is reduced, the opening of the electric control valve 401 is in direct proportional adjustment relation with the steam temperature at the outlet of the gas-liquid separator 302, when the steam temperature at the outlet of the gas-liquid separator 302 is increased, the system can use abundant heat, the valve opening of the electric control valve 401 needs to be increased, the make-up water flow is increased, and therefore the steam temperature is reduced.
Although the present invention is disclosed above, the present invention is not limited thereto. Various changes and modifications may be effected by one skilled in the art without departing from the spirit and scope of the invention, and it is intended that the scope of the invention be limited only by the claims appended hereto.
Claims (8)
1. A printing and dyeing weak lye absorption heat pump multi-effect distillation system comprises a multi-effect distillation circulation system and an absorption heat pump circulation system, and is characterized in that the multi-effect distillation circulation system comprises: a first centrifugal pump (101), a first preheater (102), a second preheater (103), a third preheater (104), a first evaporator (105) and a second evaporator (106), wherein the printing and dyeing weak lye is communicated with the inlet of the first centrifugal pump (101) through a pipeline, the outlet of the first centrifugal pump (101) is connected with the inlet a1 of the first preheater (102) through a pipeline, the outlet a2 of the first preheater (102) is connected with the inlet b1 of the second preheater (103) through a pipeline, the outlet b2 of the second preheater (103) is connected with the inlet c1 of the third preheater (104) through a pipeline, the outlet c2 of the third preheater (104) is connected with the solution inlet d1 of the first evaporator (105) through a pipeline, the solution outlet d2 of the first evaporator (105) is connected to the solution inlet e1 of the second evaporator (106) through a first pressure reducing valve (107) through a pipeline, the condensed water outlet d4 of the first evaporator (105) is connected to the inlet c3 of the third preheater (104) through a pipeline, the steam outlet d5 of the first evaporator (105) is connected to the steam inlet e3 of the second evaporator (106) through a pipeline; the solution outlet e2 of the second evaporator (106) is connected to the inlet a3 of the first preheater (102) through a pipeline, and the condensed water outlet e4 of the second evaporator (106) is connected to the inlet b3 of the second preheater (103) through a pipeline;
the absorption heat pump circulation system comprises: the system comprises a generator (201), a condenser (202), a second centrifugal pump (203), a third evaporator (204), a fourth evaporator (205), an absorber (206), a fifth evaporator (207), an energy storage device (208), a fourth preheater (209) and a third centrifugal pump (210); the medium-temperature wastewater is connected with an inlet o1 of a generator (201) through a pipeline, an outlet o2 of the generator (201) is connected to an inlet j4 of a first evaporator (204) through a pipeline, an outlet j3 of the first evaporator (204) is connected with a discharge pipeline, a steam outlet o4 of the generator (201) is connected with an inlet k1 of a condenser (202) through a pipeline, an outlet k2 of the condenser (202) is connected to an inlet j6 of the first evaporator (204) through a pipeline by a second centrifugal pump (203), an outlet j5 of the first evaporator (204) is connected to an inlet f5 of a second evaporator (205) through a pipeline, and an outlet f6 of the second evaporator (205) is connected to a steam inlet m2 of an absorber (206) through a pipeline; the concentrated lithium bromide solution outlet o5 of the generator (201) is connected to the inlet i4 of the fourth preheater (209) through a third centrifugal pump (210) by a pipeline, and the outlet i3 of the fourth preheater (209) is connected to the concentrated solution inlet m1 of the absorber (206) by a pipeline; a lithium bromide dilute solution outlet m3 of the absorber (206) is connected to an inlet h3 of a third evaporator (207) through a pipeline, an outlet h4 of the third evaporator (207) is connected to a heat storage pipeline inlet n1 of an energy storage device (208) through a pipeline, the outlet n2 of the energy storage device (208) is connected to an inlet i1 of a fourth preheater (209) through a pipeline, and an outlet i2 of the fourth preheater (209) is connected to a lithium bromide dilute solution inlet o3 of the generator (201) through a pipeline through a second pressure reducing valve (211);
the top secondary steam outlet e5 of the second evaporator (106) is connected to the inlet f1 of the fourth evaporator (205) through a pipeline, the outlet f2 of the fourth evaporator (205) is connected to the inlet of the fourth centrifugal pump (301) through a pipeline, the outlet of the fourth centrifugal pump (301) is connected to the inlet h1 of the fifth evaporator (207) through a pipeline by the first stop valve (303), the outlet h2 of the fifth evaporator (207) is connected to the inlet g1 of the gas-liquid separator (302) through a pipeline by the second stop valve (304), the steam outlet g2 of the gas-liquid separator (302) is connected to the steam inlet d3 of the first evaporator (105) through a pipeline, and the water outlet g3 of the gas-liquid separator (302) is connected to the inlet pipeline of the fourth centrifugal pump (301) through a pipeline by the third stop valve (305);
the system make-up water is connected to an inlet j1 of the third evaporator (204) through a pipeline sequentially through an electric regulating valve (401) and a fifth centrifugal pump (402), an outlet j2 of the third evaporator (204) is connected to an inlet f3 of the second evaporator (205) through a pipeline, and an outlet f4 of the second evaporator (205) is connected to an inlet pipeline of the fourth centrifugal pump (301) through a pipeline.
2. The multiple-effect distillation system of the dyeing weak lye absorption heat pump according to claim 1, characterized in that the outlet of the fourth centrifugal pump (301) is further connected to the inlet n3 of the energy accumulator (208) through a fourth stop valve (306) by a pipeline, and the outlet n4 of the energy accumulator (208) is connected to the inlet g1 of the gas-liquid separator (302) through a fifth stop valve (307) by a pipeline.
3. The multiple-effect distillation system of the printing and dyeing weak lye absorption heat pump according to claim 1, characterized in that a liquid level controller (308) is arranged in the gas-liquid separator (302), a temperature controller (309) is arranged on an outlet pipeline of the gas-liquid separator (302), and the liquid level controller (308) and the temperature controller (309) are connected with an electric regulating valve (401) through signal lines.
4. The multiple-effect distillation system of the absorption heat pump for the printing and dyeing weak lye as claimed in claim 1, wherein the energy storage phase change material used by the energy storage device (208) is Mg (NO)3)·2H2O or NaNO3─LiNO3A graphite composite energy storage material.
5. The multiple-effect distillation system of the printing and dyeing weak lye absorption heat pump according to claim 1, wherein the multiple-effect distillation circulating system is arranged as a two-effect distillation circulating system, a three-effect distillation circulating system or a four-effect distillation circulating system according to the concentration of the weak lye.
6. The multiple-effect distillation system of the absorption heat pump for the printing and dyeing weak lye as claimed in claim 1, wherein the first preheater (102) is further provided with a concentrated solution outlet a 4; the second preheater (103) is also provided with a condensed water outlet b 4; the third preheater (104) is also provided with a condensed water outlet c 4; the condenser (202) is also provided with a cooling water outlet k3 and a low-temperature cooling water inlet k 4.
7. The working method of the multiple-effect distillation system of the printing and dyeing weak lye absorption heat pump is characterized by comprising a combined operation mode, an energy storage mode and a distillation treatment mode:
firstly, a combined operation mode:
when medium-temperature wastewater exists in a printing and dyeing mill and weak alkali liquor needs to be treated, a combined operation mode is started, and the specific method comprises the following steps: opening a first stop valve (303), a second stop valve (304), a third stop valve (305) and an electric control valve (401), closing a fourth stop valve (306) and a fifth stop valve (307), enabling the dilute light alkali solution to enter a first centrifugal pump (101) for pressurization, then sequentially passing through a first preheater (102), a second preheater (103) and a third preheater (104) for preheating, and then entering a first evaporator (105), enabling steam generated after the dilute light alkali solution in the first evaporator (105) is heated to flow into a second evaporator (106) from a top outlet d5 of the first evaporator (105), enabling the dilute alkali solution to flow out from an outlet d2 of the first evaporator (105), reducing the pressure by a first pressure reducing valve (107), and then continuing to enter the second evaporator (106) for heat exchange, and enabling the dilute alkali solution to flow into a third preheater (104) from an outlet d4 of the first evaporator (105) for heat exchange; the weak base concentrated solution in the second evaporator (106) flows into the first preheater (102) from an outlet e2 of the second evaporator (106) for heat exchange, condensed water flows into the second preheater (103) for heat exchange from an outlet e4 of the second evaporator (106), secondary steam flows into the fourth evaporator (205) for heat exchange from an outlet e5 of the second evaporator (106), the liquefied condensed water enters the second centrifugal pump (301) for pressure rise, then enters the fifth evaporator (207) for heat absorption and vaporization into saturated steam, and enters the gas-liquid separator (302) through the second stop valve (304), and the water vapor flows into the first evaporator (105) from an outlet g2 of the gas-liquid separator (302) for the next circulation; the secondary steam after being reheated can not meet the operation of the two-effect distillation circulating system, the steam needs to be supplemented, make-up water enters a fifth centrifugal pump (402) through an electric regulating valve (401), is preheated through a third evaporator (204) and a fourth evaporator (205) in sequence after being boosted, is mixed with condensed water flowing out of an outlet f2 of the fourth evaporator (205), and enters a second centrifugal pump (301) for pressurization;
the medium-temperature wastewater enters a generator (201) for heat exchange, then enters a third evaporator (204) for continuous heat exchange, and then is discharged from an outlet j3 of the third evaporator (204); dilute lithium bromide solution in the generator (201) is heated to generate low-pressure working medium water vapor, the water vapor flows into the condenser (202) from an outlet o4 of the generator (201), exchanges heat with low-temperature cooling water and is condensed into saturated water, the saturated water enters the third evaporator (204) to exchange heat with medium-temperature wastewater after being boosted by the fourth centrifugal pump (203), then enters the fourth evaporator (205) to exchange heat with secondary steam, and enters the absorber (206) to exchange heat and mass after the temperature is raised; concentrated lithium bromide solution flows into a third centrifugal pump (210) from an outlet o5 of a generator (201) to be boosted, then enters a fourth preheater (209) to exchange heat, and enters an absorber (206) to be subjected to heat and mass exchange after the temperature is raised; in the absorber (206), high-pressure working medium steam is absorbed by the concentrated solution to generate a large amount of absorption heat, so that the temperature of the lithium bromide solution in the absorber (206) is increased rapidly; the heated dilute lithium bromide solution enters a fifth evaporator (207) for heat exchange, the dilute lithium bromide solution with the reduced temperature enters an energy storage device (208) for heat exchange with an energy storage phase-change material, then the dilute lithium bromide solution enters a fourth preheater (209) for heat exchange, and finally the dilute lithium bromide solution enters a generator (201) for next circulation after being reduced in pressure by a second pressure reducing valve (211);
second, energy storage mode
When medium-temperature wastewater exists in a printing and dyeing mill but no weak alkali liquor treatment requirement exists, an energy storage mode is started, and the specific method comprises the following steps: closing the first stop valve (303), the second stop valve (304), the third stop valve (305), the fourth stop valve (306), the fifth stop valve (307) and the electric regulating valve (401), wherein the double-effect distillation circulating system does not operate, and the absorption heat pump circulating system operates independently, the process of the double-effect distillation circulating system is the same as the combined operation mode, and the energy accumulator (208) is used for storing high-temperature heat for standby;
third, distillation processing mode
When no medium temperature waste water is discharged from a printing and dyeing mill but light alkali liquor treatment is needed, a distillation treatment mode is started, and the specific method comprises the following steps: opening a third stop valve (305), a fourth stop valve (306), a fifth stop valve (307) and an electric regulating valve (401), closing a first stop valve (303) and a second stop valve (304), not operating the absorption heat pump circulating system, operating the two-effect distillation circulating system independently, wherein the treatment process of the weak alkaline solution and the make-up water is the same as the combined operation mode, except that secondary steam generated in the second evaporator (106) enters the fourth evaporator (205) for heat exchange, then is mixed with the make-up water flowing out of an outlet f4 of the fourth evaporator (205), enters the fourth centrifugal pump (301) for pressurization, then flows into the energy storage device (208) through the fourth stop valve (306) for heat exchange with the energy storage phase change material, flows into the gas-liquid separator (302) through the fifth stop valve (307) after the temperature is increased, and the separated liquid water is mixed with the secondary steam and the make-up water through the third stop valve (305), the steam flows into the first evaporator (105) from the outlet g2 of the gas-liquid separator (302) for heat exchange, and the generated steam flows into the second evaporator (106) for the next circulation.
8. The working method of the multiple-effect distillation system of the printing and dyeing weak lye absorption heat pump according to claim 7, characterized in that the opening degree of the electric control valve (401) is in inverse proportion to the liquid level height in the gas-liquid separator (302); the opening degree of the electric regulating valve (401) is in direct proportion regulation relation with the temperature of steam at the outlet of the gas-liquid separator (302).
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