CN116216829A - Flue gas waste heat utilization cold and light combined supply system and working method thereof - Google Patents
Flue gas waste heat utilization cold and light combined supply system and working method thereof Download PDFInfo
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- CN116216829A CN116216829A CN202310138221.4A CN202310138221A CN116216829A CN 116216829 A CN116216829 A CN 116216829A CN 202310138221 A CN202310138221 A CN 202310138221A CN 116216829 A CN116216829 A CN 116216829A
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Abstract
The invention belongs to the technical field of flue gas waste heat utilization, and particularly relates to a flue gas waste heat utilization and frigidity combined supply system and a working method thereof. The invention comprises a refrigeration module and a sea water desalination module, wherein the refrigeration module adopts a double-effect parallel lithium bromide absorption refrigerator, and the sea water desalination module adopts a double-effect distillation type sea water desalination device. The invention can realize two-stage utilization of high-temperature flue gas, and complete cold cogeneration of flue gas waste heat utilization.
Description
Technical Field
The invention belongs to the technical field of flue gas waste heat utilization, and particularly relates to a flue gas waste heat utilization and frigidity combined supply system and a working method thereof.
Background
When the island is constructed, the requirements of island users on power supply, refrigeration and fresh water resources are required to be met under the limited energy, and the current waste heat utilization system in the distributed cogeneration cannot meet the requirements of island users on fresh water.
Disclosure of Invention
The invention aims to provide a flue gas waste heat utilization frigidity combined supply system.
The smoke waste heat utilization and dilution combined supply system comprises a refrigeration module and a sea water desalination module; the refrigeration module comprises a high-pressure generator, a low-pressure generator, a first condenser, a third evaporator, an absorber, a low-temperature solution heat exchanger and a high-temperature solution heat exchanger; the seawater desalination module comprises a flue gas heat exchanger, a first evaporator, a second condenser and a light storage device;
the high-temperature flue gas inlet of the high-pressure generator is connected to a high-temperature flue gas emission source, the low-temperature flue gas outlet of the high-pressure generator is connected to the flue gas inlet of the flue gas heat exchanger, the high-temperature refrigerant vapor outlet of the high-pressure generator is connected to the high-temperature refrigerant vapor inlet of the low-pressure generator, the high-temperature lithium bromide dilute solution inlet of the high-pressure generator is connected to the high-temperature lithium bromide dilute solution outlet of the high-temperature solution heat exchanger, and the high-temperature lithium bromide concentrated solution outlet of the high-pressure generator is connected to the high-temperature lithium bromide concentrated solution inlet of the high-temperature solution heat exchanger;
the low-temperature lithium bromide dilute solution inlet of the low-pressure generator is connected to the low-temperature lithium bromide dilute solution outlet of the low-temperature solution heat exchanger, and the low-temperature lithium bromide concentrated solution outlet of the low-pressure generator is connected to the low-temperature lithium bromide concentrated solution inlet of the low-temperature solution heat exchanger;
the cooling seawater outlet of the first condenser is connected to the preheating seawater inlets of the first evaporator and the second evaporator respectively;
the refrigerant vapor outlet of the third evaporator is connected to the refrigerant vapor inlet of the absorber, and the chilled water inlet and the chilled water outlet of the third evaporator are both connected to the required refrigeration environment;
the lithium bromide concentrated solution inlet of the absorber is respectively connected to the lithium bromide concentrated solution outlets of the low-temperature solution heat exchanger and the high-temperature solution heat exchanger, the lithium bromide dilute solution outlet of the absorber is respectively connected to the lithium bromide dilute solution inlets of the low-temperature solution heat exchanger and the high-temperature solution heat exchanger, and the cooling seawater inlet and the cooling seawater outlet of the absorber are both connected to external seawater;
the flue gas outlet of the flue gas heat exchanger is connected with the outside atmosphere, the low-temperature circulating water inlet of the flue gas heat exchanger is connected to the circulating water outlet of the first evaporator, and the high-temperature circulating water outlet of the flue gas heat exchanger is connected to the circulating water inlet of the first evaporator;
the concentrated brine outlet of the first evaporator is connected to the preheated seawater inlet of the second evaporator, and the water vapor outlet of the first evaporator is connected to the water vapor inlet of the second evaporator;
the fresh water outlet and the vapor outlet of the second evaporator are both connected to the fresh water inlet of the second condenser, and the strong brine outlet of the second evaporator is connected to the outside sea water;
the normal-temperature fresh water outlet of the second condenser is connected to the normal-temperature fresh water inlet of the light storage device, and the cooling sea water inlet and the cooling sea water outlet of the second condenser are both connected to the outside sea water.
Further, the high pressure generator, the low pressure generator, the first condenser, the third evaporator, the absorber, the first evaporator and the second evaporator are independently provided with vacuum pumps to maintain the internal hollowness.
Further, the vacuum degree in the low-pressure generator is higher than that in the high-pressure generator, and the vacuum degree in the second evaporator is higher than that in the first evaporator.
The working method of the flue gas waste heat utilization cold and light combined supply system comprises the following steps:
1. refrigeration cycle process:
the high-temperature flue gas discharged by the high-temperature flue gas discharge source enters a high-pressure generator, after heat exchange is carried out on the high-temperature flue gas and the high-temperature lithium bromide dilute solution, the high-temperature flue gas is changed into low-temperature flue gas, the high-temperature lithium bromide dilute solution is converted into lithium bromide concentrated solution by evaporating water vapor, the lithium bromide concentrated solution flows into a high-temperature solution heat exchanger, and the evaporated water vapor is used as high-temperature refrigerant vapor to be input into a low-pressure generator;
the low-temperature lithium bromide dilute solution is heated by high-temperature refrigerant vapor in the low-pressure generator, the low-temperature lithium bromide solution is boiled and evaporated to obtain low-temperature refrigerant vapor which is changed into low-temperature lithium bromide concentrated solution, the low-temperature lithium bromide concentrated solution flows into the low-temperature solution heat exchanger, the high-temperature refrigerant vapor releases heat and then is changed into high-temperature refrigerant water, the high-temperature refrigerant water and the low-temperature refrigerant vapor are mixed and flow into the first condenser to be cooled into refrigerant water;
the heat absorption of the cooled seawater in the first condenser is increased to a certain temperature and then is used as preheated seawater to be input into the first evaporator and the second evaporator, the refrigerant water is input into the third evaporator to absorb the heat and evaporate to become refrigerant vapor, and the high-temperature chilled water is cooled to be low-temperature chilled water in the third evaporator and is input into a required refrigeration environment to complete refrigeration;
the refrigerant vapor is input into an absorber and is absorbed by the lithium bromide concentrated solution to become lithium bromide dilute solution, and the heat generated by dilution is taken away by cooling seawater; the lithium bromide dilute solution flows into a high-temperature solution heat exchanger and a low-temperature solution heat exchanger respectively, and after heat exchange is carried out with the lithium bromide concentrated solution, the respective temperatures are raised to a certain temperature and are respectively input into a high-pressure generator and a low-pressure generator to complete refrigeration cycle;
2. the sea water desalination process comprises the following steps:
the low-temperature flue gas discharged by the high-pressure generator is input into the flue gas heat exchanger, the low-temperature flue gas heats the circulating water, and the low-temperature flue gas is changed into low-temperature waste gas with lower temperature to be discharged; after the circulating water is heated to a certain temperature, the circulating water is input into a first evaporator to heat and preheat seawater, and when the circulating water is reduced to a certain temperature, the circulating water is input into a flue gas heat exchanger to complete heat transfer;
the preheated seawater is heated to boiling under a certain vacuum degree to generate water vapor which is changed into strong brine, the strong brine is mixed with the preheated seawater from the first condenser according to a certain proportion and is input into the second evaporator, the water vapor is condensed and released into fresh water in the second evaporator, the preheated seawater is heated to boiling under a higher vacuum degree in the second evaporator to generate water vapor again to be changed into strong brine, and the strong brine is discharged; fresh water and steam are both input into the second condenser, and the cooled seawater is condensed to be normal-temperature fresh water which is input into the fresh water storage device for storage.
The invention has the beneficial effects that:
the invention provides a smoke waste heat utilization and dilution combined supply system, which comprises a refrigeration module and a sea water desalination module; the refrigerating module adopts a double-effect parallel lithium bromide absorption refrigerator, and the sea water desalting module adopts a double-effect distillation type sea water desalting device. The invention can realize two-stage utilization of high-temperature flue gas, and complete cold cogeneration of flue gas waste heat utilization.
Drawings
FIG. 1 is a schematic diagram of a flue gas waste heat utilization and dilution co-supply system in the invention.
Detailed Description
The invention is further described below with reference to the accompanying drawings.
Example 1:
as shown in fig. 1, the flue gas waste heat utilization and dilution combined supply system comprises a refrigeration module A and a sea water desalination module B;
the refrigeration module A adopts a double-effect parallel lithium bromide absorption refrigerator and comprises a high-pressure generator 1, a low-pressure generator 2, a first condenser 3, a third evaporator 4, an absorber 5, a low-temperature solution heat exchanger 6 and a high-temperature solution heat exchanger 7;
the sea water desalting module B adopts a double-effect distillation sea water desalting device and comprises a flue gas heat exchanger 8, a first evaporator 9, a second evaporator 10, a second condenser 11 and a light storage device 12;
the high-temperature flue gas inlet of the high-pressure generator 1 is connected to a high-temperature flue gas emission source, the low-temperature flue gas outlet of the high-pressure generator 1 is connected to the flue gas inlet of the flue gas heat exchanger 8, the high-temperature refrigerant vapor outlet of the high-pressure generator 1 is connected to the high-temperature refrigerant vapor inlet of the low-pressure generator 2, the high-temperature lithium bromide dilute solution inlet of the high-pressure generator 1 is connected to the high-temperature lithium bromide dilute solution outlet of the high-temperature solution heat exchanger 7, and the high-temperature lithium bromide concentrated solution outlet of the high-pressure generator 1 is connected to the high-temperature lithium bromide concentrated solution inlet of the high-temperature solution heat exchanger 7; the high-temperature smoke emission source is an exhaust port of power equipment (such as a common diesel engine).
The high-temperature coolant water outlet and the low-temperature coolant vapor outlet of the low-pressure generator 2 are both connected to the internal coolant inlet of the first condenser 3, the low-temperature lithium bromide dilute solution inlet of the low-pressure generator 2 is connected to the low-temperature lithium bromide dilute solution outlet of the low-temperature solution heat exchanger 6, and the low-temperature lithium bromide concentrated solution outlet of the low-pressure generator 2 is connected to the low-temperature lithium bromide concentrated solution inlet of the low-temperature solution heat exchanger 6;
the refrigerant water outlet of the first condenser 3 is connected to the refrigerant water inlet of the third evaporator 4, the cooling seawater inlet of the first condenser 3 is connected to the outside seawater, and the cooling seawater outlets of the first condenser 3 are respectively connected to the preheating seawater inlets of the first evaporator 9 and the second evaporator 10;
the refrigerant vapor outlet of the third evaporator 4 is connected to the refrigerant vapor inlet of the absorber 5, and the chilled water inlet and chilled water outlet of the third evaporator 4 are both connected to the desired refrigeration environment;
the lithium bromide concentrated solution inlets of the absorber 5 are respectively connected to the lithium bromide concentrated solution outlets of the low-temperature solution heat exchanger 6 and the high-temperature solution heat exchanger 7, the lithium bromide dilute solution outlets of the absorber 5 are respectively connected to the lithium bromide dilute solution inlets of the low-temperature solution heat exchanger 6 and the high-temperature solution heat exchanger 7, and the cooling seawater inlet and the cooling seawater outlet of the absorber 5 are both connected to the external seawater;
the flue gas outlet of the flue gas heat exchanger 8 is connected with the outside atmosphere, the low-temperature circulating water inlet of the flue gas heat exchanger 8 is connected to the circulating water outlet of the first evaporator 9, and the high-temperature circulating water outlet of the flue gas heat exchanger 8 is connected to the circulating water inlet of the first evaporator 9;
the strong brine outlet of the first evaporator 9 is connected to the preheated seawater inlet of the second evaporator 10, and the water vapor outlet of the first evaporator 9 is connected to the water vapor inlet of the second evaporator 10;
the fresh water outlet and the water vapor outlet of the second evaporator 10 are both connected to the fresh water inlet of the second condenser 11, and the concentrated brine outlet of the second evaporator 10 is connected to the outside seawater;
the normal temperature fresh water outlet of the second condenser 11 is connected to the normal temperature fresh water inlet of the fresh water storage device 12, and the cooling seawater inlet and the cooling seawater outlet of the second condenser 11 are both connected to the outside seawater.
Example 2:
in the present embodiment, the high pressure generator 1, the low pressure generator 2, the first condenser 3, the third evaporator 4, the absorber 5, the first evaporator 9, and the second evaporator 10 are each independently provided with a vacuum pump to maintain the internal hollowness.
Example 3:
in the present embodiment, the vacuum degree inside the low pressure generator 2 is higher than that of the high pressure generator 1, and the vacuum degree inside the second evaporator 10 is higher than that of the first evaporator 9.
Example 4:
the working method of the flue gas waste heat utilization and dilution combined supply system is as follows:
the high temperature flue gas discharged from the high temperature flue gas discharge source enters the high pressure generator 1, after heat exchange with the high temperature lithium bromide dilute solution, the high temperature flue gas becomes low temperature flue gas, the high temperature lithium bromide dilute solution is heated, boiled and evaporated under certain low pressure condition to obtain water vapor, the water vapor is changed into lithium bromide concentrated solution and flows into the high temperature solution heat exchanger 7, the evaporated water vapor is used as high temperature refrigerant vapor to be input into the low pressure generator 2 for heating the low temperature lithium bromide dilute solution, the low temperature lithium bromide solution is boiled and evaporated under lower pressure to obtain low temperature refrigerant vapor, the low temperature refrigerant vapor is changed into low temperature lithium bromide concentrated solution and flows into the low temperature solution heat exchanger 6, the high temperature refrigerant vapor is mixed with the low temperature refrigerant vapor after heat release, the high temperature refrigerant water and the low temperature refrigerant vapor flow into the first condenser 3 to be cooled into refrigerant water, after the heat absorption of the cooling seawater in the first condenser 3 is raised to a certain temperature (about 40 ℃), the cooling seawater is input into the first evaporator 9 and the second evaporator 10 as preheated seawater, the refrigerant water is input into the third evaporator 4 to absorb heat and evaporate to become refrigerant vapor, the high-temperature chilled water is cooled to be low-temperature chilled water in the third evaporator 4 and is input into a required refrigeration environment to complete refrigeration, the refrigerant vapor is input into the absorber 5 and is absorbed by the lithium bromide concentrated solution to be changed into the lithium bromide dilute solution, the heat generated by dilution is taken away by the cooling seawater, the lithium bromide dilute solution respectively flows into the high-temperature solution heat exchanger 7 and the low-temperature solution heat exchanger 6 to be subjected to heat exchange with the lithium bromide concentrated solution, and then the respective temperatures are raised to a certain temperature and are respectively input into the high-pressure generator 1 and the low-pressure generator 2 to complete refrigeration cycle;
the sea water desalination process, namely, the low-temperature flue gas discharged from the high-pressure generator 1 is input into the flue gas heat exchanger 8 to heat circulating water, the low-temperature flue gas is changed into low-temperature waste gas with lower temperature to be discharged, the circulating water is heated to a certain temperature and then is input into the first evaporator 9 to heat preheated sea water, then is reduced to a certain temperature and then is input into the flue gas heat exchanger 8 to complete heat transfer, the preheated sea water is heated to boiling under a certain vacuum degree to generate steam to become strong brine, the steam and the preheated sea water from the first condenser 3 are mixed according to a certain proportion and input into the second evaporator 10, the steam is condensed and released into fresh water in the second evaporator 10, the preheated sea water is heated to boiling under a higher vacuum degree in the second evaporator 10 to generate steam again to become strong brine to be discharged, the fresh water and the steam are both input into the condenser 11 of the sea water desalination device, and the cooled sea water is condensed to become normal-temperature fresh water to be input into the light storage device 12 for storage.
The above description is only of the preferred embodiments of the present invention and is not intended to limit the present invention, but various modifications and variations can be made to the present invention by those skilled in the art. Any modification, equivalent replacement, improvement, etc. made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (4)
1. Flue gas waste heat utilization frigidity allies oneself with supplies system, its characterized in that: comprises a refrigeration module (A) and a sea water desalination module (B); the refrigeration module (A) comprises a high-pressure generator (1), a low-pressure generator (2), a first condenser (3), a third evaporator (4), an absorber (5), a low-temperature solution heat exchanger (6) and a high-temperature solution heat exchanger (7); the seawater desalination module (B) comprises a flue gas heat exchanger (8), a first evaporator (9), a second evaporator (10), a second condenser (11) and a light storage device (12);
the high-temperature flue gas inlet of the high-pressure generator (1) is connected to a high-temperature flue gas emission source, the low-temperature flue gas outlet of the high-pressure generator (1) is connected to the flue gas inlet of the flue gas heat exchanger (8), the high-temperature refrigerant vapor outlet of the high-pressure generator (1) is connected to the high-temperature refrigerant vapor inlet of the low-pressure generator (2), the high-temperature lithium bromide dilute solution inlet of the high-pressure generator (1) is connected to the high-temperature lithium bromide dilute solution outlet of the high-temperature solution heat exchanger (7), and the high-temperature lithium bromide concentrated solution outlet of the high-pressure generator (1) is connected to the high-temperature lithium bromide concentrated solution inlet of the high-temperature solution heat exchanger (7);
the high-temperature coolant water outlet and the low-temperature coolant vapor outlet of the low-pressure generator (2) are both connected to the internal coolant inlet of the first condenser (3), the low-temperature lithium bromide dilute solution inlet of the low-pressure generator (2) is connected to the low-temperature lithium bromide dilute solution outlet of the low-temperature solution heat exchanger (6), and the low-temperature lithium bromide concentrated solution outlet of the low-pressure generator (2) is connected to the low-temperature lithium bromide concentrated solution inlet of the low-temperature solution heat exchanger (6);
the refrigerant water outlet of the first condenser (3) is connected to the refrigerant water inlet of the third evaporator (4), the cooling seawater inlet of the first condenser (3) is connected to the outside seawater, and the cooling seawater outlets of the first condenser (3) are respectively connected to the preheating seawater inlets of the first evaporator (9) and the second evaporator (10);
the refrigerant vapor outlet of the third evaporator (4) is connected to the refrigerant vapor inlet of the absorber (5), and the chilled water inlet and the chilled water outlet of the third evaporator (4) are both connected to the required refrigeration environment;
the lithium bromide concentrated solution inlet of the absorber (5) is respectively connected to the lithium bromide concentrated solution outlets of the low-temperature solution heat exchanger (6) and the high-temperature solution heat exchanger (7), the lithium bromide dilute solution outlet of the absorber (5) is respectively connected to the lithium bromide dilute solution inlets of the low-temperature solution heat exchanger (6) and the high-temperature solution heat exchanger (7), and the cooling seawater inlet and the cooling seawater outlet of the absorber (5) are both connected to the external seawater;
the flue gas outlet of the flue gas heat exchanger (8) is connected with the outside atmosphere, the low-temperature circulating water inlet of the flue gas heat exchanger (8) is connected to the circulating water outlet of the first evaporator (9), and the high-temperature circulating water outlet of the flue gas heat exchanger (8) is connected to the circulating water inlet of the first evaporator (9);
the strong brine outlet of the first evaporator (9) is connected to the preheated seawater inlet of the second evaporator (10), and the water vapor outlet of the first evaporator (9) is connected to the water vapor inlet of the second evaporator (10);
the fresh water outlet and the water vapor outlet of the second evaporator (10) are both connected to the fresh water inlet of the second condenser (11), and the strong brine outlet of the second evaporator (10) is connected to the outside seawater;
the normal-temperature fresh water outlet of the second condenser (11) is connected to the normal-temperature fresh water inlet of the light storage device (12), and the cooling seawater inlet and the cooling seawater outlet of the second condenser (11) are both connected to the outside seawater.
2. The flue gas waste heat utilization frigidity co-supply system according to claim 1, wherein: the high-pressure generator (1), the low-pressure generator (2), the first condenser (3), the third evaporator (4), the absorber (5), the first evaporator (9) and the second evaporator (10) are all independently provided with vacuum pumps to maintain the internal hollowness.
3. The flue gas waste heat utilization frigidity co-supply system according to claim 1, wherein: the vacuum degree in the low-pressure generator (2) is higher than that in the high-pressure generator (1), and the vacuum degree in the second evaporator (10) is higher than that in the first evaporator (9).
4. The working method of the flue gas waste heat utilization frigidity combined supply system based on claim 1 is characterized by comprising the following steps:
1. refrigeration cycle process:
high-temperature flue gas discharged by a high-temperature flue gas discharge source enters a high-pressure generator (1), after heat exchange is carried out on the high-temperature flue gas and a high-temperature lithium bromide dilute solution, the high-temperature flue gas is changed into low-temperature flue gas, the high-temperature lithium bromide dilute solution is converted into a lithium bromide concentrated solution by evaporating water vapor, the lithium bromide concentrated solution flows into a high-temperature solution heat exchanger (7), and the evaporated water vapor is input into a low-pressure generator (2) as high-temperature refrigerant vapor;
the low-temperature lithium bromide dilute solution is heated by high-temperature refrigerant vapor in the low-pressure generator (2), the low-temperature lithium bromide solution is boiled and evaporated to obtain low-temperature refrigerant vapor which is changed into low-temperature lithium bromide concentrated solution, the low-temperature lithium bromide concentrated solution flows into the low-temperature solution heat exchanger (6), and after the high-temperature refrigerant vapor releases heat, the low-temperature lithium bromide concentrated solution is changed into high-temperature refrigerant water which is mixed with the low-temperature refrigerant vapor and flows into the first condenser (3) to be cooled into refrigerant water;
after the heat absorption of the cooled seawater in the first condenser (3) is raised to a certain temperature, the cooled seawater is input into the first evaporator (9) and the second evaporator (10) as preheated seawater, the refrigerant water is input into the third evaporator (4) to absorb the heat and evaporate the heat to become refrigerant vapor, and the high-temperature chilled water is cooled in the third evaporator (4) to be low-temperature chilled water, and is input into a required refrigeration environment to complete refrigeration;
the refrigerant vapor is input into an absorber (5) and absorbed by the lithium bromide concentrated solution to be changed into the lithium bromide dilute solution, and the heat generated by dilution is taken away by cooling seawater; the lithium bromide dilute solution flows into a high-temperature solution heat exchanger (7) and a low-temperature solution heat exchanger (6) respectively, and after heat exchange with the lithium bromide concentrated solution, the respective temperatures are raised to a certain temperature and are respectively input into a high-pressure generator (1) and a low-pressure generator (2) to complete refrigeration cycle;
2. the sea water desalination process comprises the following steps:
the low-temperature flue gas discharged by the high-pressure generator (1) is input into the flue gas heat exchanger (8), the circulating water is heated by the low-temperature flue gas, and the low-temperature flue gas is changed into low-temperature waste gas with lower temperature to be discharged; after being heated to a certain temperature, the circulating water is input into a first evaporator (9) for heating and preheating seawater, and when the circulating water is reduced to a certain temperature, the circulating water is input into a flue gas heat exchanger (8) for completing heat transfer;
the preheated seawater is heated to boiling under a certain vacuum degree to generate water vapor which is changed into strong brine, the strong brine is mixed with the preheated seawater from the first condenser (3) according to a certain proportion and is input into the second evaporator (10), the water vapor is condensed and heat-released in the second evaporator (10) to become fresh water, the preheated seawater is heated to boiling under a higher vacuum degree in the second evaporator (10) to generate water vapor again to be changed into strong brine to be discharged; fresh water and steam are both input into a second condenser (11), and the cooled seawater is condensed to be normal-temperature fresh water which is input into a light storage device (12) for storage.
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| Application Number | Priority Date | Filing Date | Title |
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| CN202310138221.4A CN116216829A (en) | 2023-02-20 | 2023-02-20 | Flue gas waste heat utilization cold and light combined supply system and working method thereof |
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| CN202310138221.4A CN116216829A (en) | 2023-02-20 | 2023-02-20 | Flue gas waste heat utilization cold and light combined supply system and working method thereof |
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