CN105674558A - Gas engine driven steam compressing and absorbing combined type heat pump hot water unit running method - Google Patents
Gas engine driven steam compressing and absorbing combined type heat pump hot water unit running method Download PDFInfo
- Publication number
- CN105674558A CN105674558A CN201610087543.0A CN201610087543A CN105674558A CN 105674558 A CN105674558 A CN 105674558A CN 201610087543 A CN201610087543 A CN 201610087543A CN 105674558 A CN105674558 A CN 105674558A
- Authority
- CN
- China
- Prior art keywords
- ammonia
- heat
- solution
- generator
- absorber
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Classifications
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F24—HEATING; RANGES; VENTILATING
- F24H—FLUID HEATERS, e.g. WATER OR AIR HEATERS, HAVING HEAT-GENERATING MEANS, e.g. HEAT PUMPS, IN GENERAL
- F24H4/00—Fluid heaters characterised by the use of heat pumps
- F24H4/02—Water heaters
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F24—HEATING; RANGES; VENTILATING
- F24H—FLUID HEATERS, e.g. WATER OR AIR HEATERS, HAVING HEAT-GENERATING MEANS, e.g. HEAT PUMPS, IN GENERAL
- F24H9/00—Details
- F24H9/0005—Details for water heaters
-
- 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
- F25B30/00—Heat pumps
- F25B30/04—Heat pumps of the sorption type
Abstract
The invention discloses a gas engine driven steam compressing and absorbing combined type heat pump hot water unit running method. The method includes the following steps that a gas engine drives a compressor to act. A refrigerant is compressed into high-temperature and high-pressure gas, becomes liquid after heat exchange and enters the compressor after absorbing heat and being evaporated into gas, and compression type refrigerant cycling is formed. The method further includes solution cycling and refrigerant cycling, hot user return water is divided into two ways to be heated; the first way of return water is subjected to heat exchange with exhaust fume of the gas engine in an exhaust fume heat exchanger and then enters a first condenser and a cylinder sleeve heat exchanger in sequence to be subjected to heat exchange, and therefore the temperature of the return water can be increased; and the second way of return water absorbs absorbing heat generated in an external cooling absorber, then enters a second condenser, is subjected to heat exchange with ammonia steam in the second condenser and is provided for a user to use after being heated. By means of the method, the primary energy ratio can be increased.
Description
Technical field
The present invention relates to combined heat pump Hot water units operation method, particularly relate to gas engine driving steam compressed with absorption combined heat pump Hot water units operation method.
Background technology
Driving in compression heat pump system at gas engine, with physical properties and the second law of thermodynamics for foundation, gas engine is done work with power driven compressor, coordinate condenser, the equipment such as expansion valve and vaporizer, by changing the state of cold-producing medium, reaches refrigeration and the purpose heated. Meanwhile, gas engine produces substantial amounts of thermal output, including electromotor internal recycle water waste heat and fume afterheat two parts. UTILIZATION OF VESIDUAL HEAT IN has various ways, can assisted evaporative, can defrosting, hot water etc. of also can doing manual labour. But gas engine waste heat is only for auxiliary heating and preparation domestic hot-water, and waste heat quality is not promoted further. And multiple building such as office building, office building etc. are not required to massive life hot water, the suitability is restricted, it is impossible to give full play to the advantage of gas-burning machine heat pump.
Have the driving vapor compression heat pump systems structure of gas engine at present, only with engine exhaust heat hot water preparing, capacity usage ratio andEfficiency is not high, and waste heat quality does not also improve.
Summary of the invention
It is an object of the invention to overcome the deficiencies in the prior art, it is provided that one decreases heat energy input, improve the gas engine of the coefficient of performance of system and primary energy ratio and drive steam compressed with absorption combined heat pump Hot water units operation method.
In order to achieve the above object, the technical solution used in the present invention is:
Gas engine of the present invention drives steam compressed with absorption combined heat pump Hot water units operation method, and it comprises the following steps:
Gas engine-driven compressor work, it is the gaseous state of High Temperature High Pressure by the refrigerant compression of compression heat pump system, gaseous refrigerant first passes through oil eliminator, carry out heat exchange subsequently into the first condenser and first via user's backwater and transfer heat to user's backwater, cold-producing medium is condensed into the high-pressure liquid that temperature is relatively low, enter reservoir, the first vaporizer is entered then through after becoming the liquid of low-temp low-pressure after expansion valve throttling expansion, the first described vaporizer absorbs the heat of external environment and is evaporated to gaseous state, the cold-producing medium of gaseous state enters compressor through gas-liquid separator, it is compressed to the gaseous state of High Temperature High Pressure, it is thusly-formed a compression-type refrigeration agent circulation,
The smoke discharging residual heat of gas engine carries out heat exchange as the driving heat source of the external heat generator of absorption type heat pump system with the ammonia spirit in external heat generator, ammonia spirit in external heat generator is added by smoke discharging residual heat and is thermally generated ammonia steam and temperature is 130～170 DEG C, pressure is 1.5～2.0MPa high temperature ammonia weak solution, described high temperature ammonia weak solution cools to 110～150 DEG C with ammonia spirit heat exchange by entering solution heating generator equipped with the pipeline of the first solution pump, absorber is entered after cooling to 80～140 DEG C then through the decompression of solution choke valve, after ammonia weak solution absorbing ammonia steam in absorber, temperature is reduced to 60～80 DEG C, become denseer ammonia weak solution, subsequently in solution cooling absorption device, further absorbing ammonia steam makes ammonia spirit concentration raise further, finally enter external refrigeration absorber, absorb the low temperature concentrated solution of the ammonia steam formation 40～60-DEG C from subcooler,Ammonia concentrated solution in second solution pumped external refrigeration absorber sends into pipeline, described pipeline enters the ammonia weak solution produced with rectifier again after solution cooling absorption device heats up with the ammonia spirit heat exchange in solution cooling absorption device and mixes, then sequentially enter generator, solution heating generator, external heat generator make ammonia evaporation generate ammonia weak solution, forming solution circulation, the medium circulation by being located in the recycle heat pipeline in generator and described absorber passes to generator by absorbing heat in absorber in the process;
By generator, solution heating generator, the ammonia steam that external heat generator generates enters rectifier, generation ammonia weak solution and mass percent purity are not less than the ammonia steam of 99.5%, described ammonia steam is condensed into the liquid of 40～60 DEG C after the second condenser and second tunnel user's backwater carry out heat exchange, it is further cooled subsequently into subcooler exchanges with-20～5 DEG C of low temperature ammonia heat of steam from the second vaporizer, again through the liquid ammonia becoming-20～5 DEG C of low-temp low-pressures after expansion valve throttling expansion, the liquid ammonia of described low-temp low-pressure absorbs external environment heat subsequently into the second vaporizer and is evaporated, become-20～5 DEG C of low temperature ammonia steams, described low temperature ammonia steam is returned after being heated up by heat exchange heat absorption in described subcooler and is sequentially sent to external refrigeration absorber, solution cooling absorption device and absorber are only absorbed by the water and form ammonia spirit, ammonia spirit in described solution cooling absorption device and absorber eventually enters into external refrigeration absorber, by being provided with the pipeline entrance solution cooling absorption device absorption heat of the first solution pump, the ammonia concentrated solution own temperature in pipeline is raised, then mix with the ammonia weak solution from rectifier, it is sequentially sent to generator, solution heating generator and external heat generator, form the circulation of cold-producing medium,
Heat user backwater is divided into two-way to be heated, and after first via backwater carries out heat exchange with the smoke evacuation of gas engine in exhaust heat exchanger, then sequentially enters the first condenser and cylinder sleeve heat exchanger carries out heat exchange and makes return water temperature raise; Second road backwater enters the second condenser after absorbing the absorption heat produced in external refrigeration absorber, for user after the second described condenser and ammonia steam carry out heat exchange intensification.
Compared with prior art, the method have the advantages that
The present invention can more efficiently improve engine exhaust heat utilization rate, and then improves primary energy ratio.
At absorption type heat pump system, at present adopt lithium bromide device of working mediums to or ammonia-water mixture pair. The absorption type heat pump system of the present invention, for both the above working medium to being suitable for, according to ammonia-water mixture pair, then this combined heat pump goes for the operating mode of lower temperature. No matter adopt which kind of working medium pair, be required for inputting heat energy to generator and carry out the operation of drive system. The present invention adopts absorber, solution cooling absorption device, external refrigeration absorber, generator, solution heating generator and external heat generator that heat energy has carried out cascade utilization fully, decreases heat energy input, improves the coefficient of performance of system.
While the present invention proposes to utilize gas engine power drive compression heat pump system, using the thermal flue gas of the gas engine driving heat source as absorption type heat pump system, high efficiente callback make use of the used heat of gas engine, simultaneously, absorption heat pump circulating system can utilize the heat of low-grade heat source (such as air, sewage, subsoil water etc.), substantially increase system primary energy utilization ratio andEfficiency.
In the present invention, drive in compression heat pump system the smoke discharging residual heat of gas engine as the driving heat energy of absorption type heat pump system using gas engine, this not only efficiently utilizes gas-burning machine heat pump fume afterheat, bigger meaning is in that to utilize absorption type heat pump system again to obtain heat energy from low-grade heat source so that primary energy ratio is improved.
Accompanying drawing explanation
Fig. 1 is that the gas engine of the present invention is driving steam compressed with absorption combined heat pump Hot water units.
1 gas engine in figure, 2 compressors, 3 oil eliminators, 4 first condensers, 5 reservoirs, 6 expansion valves, 7 first vaporizers, 8 gas-liquid separators, 9 external heat generators, 10 solution heating generators, 11 generators, 12 absorbers, 13 solution cooling absorption devices, 14 external refrigeration absorbers, 15 rectifiers, 16 second condensers, 17 subcoolers, 18 second vaporizers, 19 cylinder sleeve heat exchangers, 20 exhaust heat exchangers, 21 second solution pumps, 22 expansion valves, 23 solution choke valves, 24 first solution pumps
Detailed description of the invention
Describe the present invention below in conjunction with the drawings and specific embodiments.
Gas engine of the present invention as shown in Figure 1 drives the steam compressed operation method with absorption combined heat pump Hot water units, and it comprises the following steps:
Gas engine 1 drives compressor 2 to do work, it is the gaseous state of High Temperature High Pressure by the refrigerant compression of compression heat pump system, gaseous refrigerant first passes through oil eliminator 3, carry out heat exchange subsequently into the first condenser 4 with first via user's backwater and transfer heat to user's backwater, cold-producing medium is condensed into the high-pressure liquid that temperature is relatively low, enter reservoir 5, the first vaporizer is entered then through after becoming the liquid of low-temp low-pressure after expansion valve 6 throttling expansion, the first described vaporizer 7 absorbs the heat of external environment and is evaporated to gaseous state, the cold-producing medium of gaseous state enters compressor 2 through gas-liquid separator 8, it is compressed to the gaseous state of High Temperature High Pressure, it is thusly-formed a compression-type refrigeration agent circulation,
The smoke discharging residual heat of gas engine 1 carries out heat exchange as the driving heat source of the external heat generator 9 of absorption type heat pump system with the ammonia spirit in external heat generator 9, ammonia spirit in external heat generator 9 is added by smoke discharging residual heat and is thermally generated ammonia steam and temperature is 130～170 DEG C, pressure is 1.5～2.0MPa high temperature ammonia weak solution, described high temperature ammonia weak solution cools to 110～150 DEG C with ammonia spirit heat exchange by entering solution heating generator 10 equipped with the pipeline of the first solution pump 24, absorber 12 is entered after cooling to 80～140 DEG C then through solution choke valve 23 decompression, after ammonia weak solution absorbing ammonia steam in absorber 12, temperature is reduced to 60～80 DEG C, become denseer ammonia weak solution, subsequently in solution cooling absorption device 13, further absorbing ammonia steam makes ammonia spirit concentration raise further, finally enter external refrigeration absorber 14, absorb the low temperature concentrated solution of the ammonia steam formation 40～60 DEG C from subcooler 17, second solution pump 21 is extracted the ammonia concentrated solution in external refrigeration absorber 14 out and is sent into pipeline, described pipeline enters the ammonia weak solution produced with rectifier 15 again after solution cooling absorption device 13 heats up with the ammonia spirit heat exchange in solution cooling absorption device 13 and mixes, then generator 11 is sequentially entered, solution heating generator 10, external heat generator 9 makes ammonia evaporation generate ammonia weak solution, form solution circulation, medium circulation by being located in the recycle heat pipeline in generator 11 and described absorber 12 passes to generator 11 by absorbing heat in absorber 12 in the process,
The ammonia steam generated by generator 11, solution heating generator 10, external heat generator 9 enters rectifier 15, and generation ammonia weak solution and mass percent purity are not less than the ammonia steam of 99.5%. described ammonia steam is condensed into the liquid of 40～60 DEG C after the second condenser 16 and second tunnel user's backwater carry out heat exchange, it is further cooled subsequently into subcooler 17 exchanges with-20～5 DEG C of low temperature ammonia heat of steam from the second vaporizer 18, again through the liquid ammonia becoming-20～5 DEG C of low-temp low-pressures after expansion valve 22 throttling expansion. the liquid ammonia of described low-temp low-pressure absorbs external environment heat subsequently into the second vaporizer 18 and is evaporated, and becomes-20～5 DEG C of low temperature ammonia steams. described low temperature ammonia steam is returned after being heated up by heat exchange heat absorption in described subcooler 17 and is sequentially sent to external refrigeration absorber 14, solution cooling absorption device 13 and absorber 12 are only absorbed by the water and form ammonia spirit, ammonia spirit in described solution cooling absorption device and absorber eventually enters into external refrigeration absorber 14, enter solution cooling absorption device 13 and absorb heat by being provided with the pipeline of the first solution pump 21 the ammonia concentrated solution own temperature in pipeline is raised, then mix with the ammonia weak solution from rectifier 15, it is sequentially sent to generator 11, solution heating generator 10 and external heat generator 9, form the circulation of cold-producing medium.
Heat user backwater is divided into two-way to be heated, and after first via backwater carries out heat exchange with the smoke evacuation of gas engine 1 in exhaust heat exchanger 20, then sequentially enters condenser 4 and cylinder sleeve heat exchanger 19 carries out heat exchange and makes return water temperature raise; Second road backwater enters condenser 16 after absorbing the absorption heat produced in external refrigeration absorber 14, for user after described condenser 16 carries out heat exchange intensification with ammonia steam, for user after the mixing of final two-way water return pipeline hot water.
A kind of system according to the inventive method, it includes compression heat pump system, absorption type heat pump system and heats water supply and return system;
Described compression heat pump system includes gas engine 1, the output shaft of described gas engine 1 is connected with the rotating shaft of compressor 2, and the refrigerant outlet of described compressor 2 connects pipeline by first and is sequentially connected with the refrigerant inlet of oil eliminator the 3, first condenser 4, reservoir 5, expansion valve the 6, first vaporizer 7, gas-liquid separator 8 and compressor 2;
Described absorption type heat pump system includes rectifier 15, and the ammonia weak solution outlet of described rectifier 15 connects pipeline by second and is sequentially communicated generator 11, solution heating generator 10 and external heat generator 9; The ammonia vapor outlet port at described external heat generator 9 top is sequentially connected with the material inlet of solution heating generator 10, generator 11 and rectifier 15 by ammonia vapor line; High temperature ammonia weak solution outlet bottom described external heat generator 9 enters solution heating generator 10 after connecting the first solution pump 24 by the 3rd connection pipeline, and described the 3rd connects pipeline and be connected with solution choke valve 23, absorber 12, solution cooling absorption device 13 and external refrigeration absorber 14 successively after described solution heating generator 10; Low temperature ammonia concentrated solution outlet bottom described external refrigeration absorber 14 enters solution cooling absorption device 13 after connecting the second solution pump 21 by the 4th connection pipeline, the 4th described connection pipeline is connected pipeline with second the outlet of ammonia weak solution and the generator 11 of rectifier 15 after described solution cooling absorption device 13 and is connected;The ammonia solution vapor outlet port of described rectifier 15 connects pipeline by the 5th and is sequentially connected with the second condenser 16, the liquid ammonia import of subcooler 17, liquid ammonia outlet, expansion valve the 22, second vaporizer 18, described subcooler 17 gaseous ammonia import, gaseous ammonia outlet, described external refrigeration absorber 14, described solution cooling absorption device 13 and described absorber 12; Recycle heat pipeline is located in described generator 11 and absorber 12 so that the ammonia-water mixture in generator 11 and absorber 12 is by the media implementation heat transmission in recycle heat pipeline, is provided with circulating pump on described recycle heat pipeline; The smoke evacuation outlet of described gas engine 1 is connected with one end of flue, and the portions of described flue is located in described external heat generator 9 and the other end is connected with the smoke inlet of exhaust heat exchanger;
The described backwater heating water supply and return system is divided into two-way, wherein a road is sequentially connected with described exhaust heat exchanger the 20, first condenser 4 and cylinder sleeve heat exchanger 19 makes return water temperature be connected with supply channel after raising, another road is connected with the second condenser 16 and supply channel successively after external refrigeration absorber 14, for user after the mixing of final two-way water return pipeline hot water.
Embodiment 1
Gas engine 1 drives compressor 2 to do work, it is the gaseous state of High Temperature High Pressure by the refrigerant compression of compression heat pump system, gaseous refrigerant first passes through oil eliminator 3, carry out heat exchange subsequently into the first condenser 4 with first via user's backwater and transfer heat to user's backwater, cold-producing medium is condensed into the high-pressure liquid that temperature is relatively low, enter reservoir 5, the first vaporizer is entered then through after becoming the liquid of low-temp low-pressure after expansion valve 6 throttling expansion, the first described vaporizer 7 absorbs the heat of external environment and is evaporated to gaseous state, the cold-producing medium of gaseous state enters compressor 2 through gas-liquid separator 8, it is compressed to the gaseous state of High Temperature High Pressure, it is thusly-formed a compression-type refrigeration agent circulation,
The smoke discharging residual heat of gas engine 1 carries out heat exchange as the driving heat source of the external heat generator 9 of absorption type heat pump system with the ammonia spirit in external heat generator 9, ammonia spirit in external heat generator 9 is added by smoke discharging residual heat and is thermally generated ammonia steam and temperature is 170 DEG C, pressure is 2.0MPa high temperature ammonia weak solution, described high temperature ammonia weak solution cools to 150 DEG C with ammonia spirit heat exchange by entering solution heating generator 10 equipped with the pipeline of the first solution pump 24, absorber 12 is entered after cooling to 140 DEG C then through solution choke valve 23 decompression, after ammonia weak solution absorbing ammonia steam in absorber 12, temperature is reduced to 80 DEG C, become denseer ammonia weak solution, subsequently in solution cooling absorption device 13, further absorbing ammonia steam makes ammonia spirit concentration raise further, finally enter external refrigeration absorber 14, absorb the low temperature concentrated solution of the ammonia steam formation 60 DEG C from subcooler 17, second solution pump 21 is extracted the ammonia concentrated solution in external refrigeration absorber 14 out and is sent into pipeline, described pipeline enters the ammonia weak solution produced with rectifier 15 again after solution cooling absorption device 13 heats up with the ammonia spirit heat exchange in solution cooling absorption device 13 and mixes, then generator 11 is sequentially entered, solution heating generator 10, external heat generator 9 makes ammonia evaporation generate ammonia weak solution, form solution circulation, medium circulation by being located in the recycle heat pipeline in generator 11 and described absorber 12 passes to generator 11 by absorbing heat in absorber 12 in the process,
The ammonia steam generated by generator 11, solution heating generator 10, external heat generator 9 enters rectifier 15, and generation ammonia weak solution and mass percent purity are not less than the ammonia steam of 99.5%. described ammonia steam is condensed into the liquid of 60 DEG C after the second condenser 16 and second tunnel user's backwater carry out heat exchange, it is further cooled subsequently into subcooler 17 exchanges with 5 DEG C of low temperature ammonia heat of steam from the second vaporizer 18, again through the liquid ammonia becoming 5 DEG C of low-temp low-pressures after expansion valve 22 throttling expansion. the liquid ammonia of described low-temp low-pressure absorbs external environment heat subsequently into the second vaporizer 18 and is evaporated, and becomes 5 DEG C of low temperature ammonia steams. described low temperature ammonia steam is returned after being heated up by heat exchange heat absorption in described subcooler 17 and is sequentially sent to external refrigeration absorber 14, solution cooling absorption device 13 and absorber 12 are only absorbed by the water and form ammonia spirit, ammonia spirit in described solution cooling absorption device and absorber eventually enters into external refrigeration absorber 14, enter solution cooling absorption device 13 and absorb heat by being provided with the pipeline of the first solution pump 21 the ammonia concentrated solution own temperature in pipeline is raised, then mix with the ammonia weak solution from rectifier 15, it is sequentially sent to generator 11, solution heating generator 10 and external heat generator 9, form the circulation of cold-producing medium.
Heat user backwater is divided into two-way to be heated, and after first via backwater carries out heat exchange with the smoke evacuation of gas engine 1 in exhaust heat exchanger 20, then sequentially enters the first condenser 4 and cylinder sleeve heat exchanger 19 carries out heat exchange and makes return water temperature raise; Second road backwater enters the second condenser 16 after absorbing the absorption heat produced in external refrigeration absorber 14, for user after the second described condenser 16 carries out heat exchange intensification with ammonia steam, for user after the mixing of final two-way water return pipeline hot water.
Adopt this method to make low grade residual heat be fully used, make the coefficient of performance of system be improved significantly, be greatly improved the primary energy ratio of system.
Embodiment 2
Gas engine 1 drives compressor 2 to do work, it is the gaseous state of High Temperature High Pressure by the refrigerant compression of compression heat pump system, gaseous refrigerant first passes through oil eliminator 3, carry out heat exchange subsequently into the first condenser 4 with first via user's backwater and transfer heat to user's backwater, cold-producing medium is condensed into the high-pressure liquid that temperature is relatively low, enter reservoir 5, the first vaporizer is entered then through after becoming the liquid of low-temp low-pressure after expansion valve 6 throttling expansion, the first described vaporizer 7 absorbs the heat of external environment and is evaporated to gaseous state, the cold-producing medium of gaseous state enters compressor 2 through gas-liquid separator 8, it is compressed to the gaseous state of High Temperature High Pressure, it is thusly-formed a compression-type refrigeration agent circulation,
The smoke discharging residual heat of gas engine 1 carries out heat exchange as the driving heat source of the external heat generator 9 of absorption type heat pump system with the ammonia spirit in external heat generator 9, ammonia spirit in external heat generator 9 is added by smoke discharging residual heat and is thermally generated ammonia steam and temperature is 150 DEG C, pressure is 1.8MPa high temperature ammonia weak solution, described high temperature ammonia weak solution cools to 130 DEG C with ammonia spirit heat exchange by entering solution heating generator 10 equipped with the pipeline of the first solution pump 24, absorber 12 is entered after cooling to 110 DEG C then through solution choke valve 23 decompression, after ammonia weak solution absorbing ammonia steam in absorber 12, temperature is reduced to 70 DEG C, become denseer ammonia weak solution, subsequently in solution cooling absorption device 13, further absorbing ammonia steam makes ammonia spirit concentration raise further, finally enter external refrigeration absorber 14, absorb the low temperature concentrated solution of the ammonia steam formation 50 DEG C from subcooler 17,Second solution pump 21 is extracted the ammonia concentrated solution in external refrigeration absorber 14 out and is sent into pipeline, described pipeline enters the ammonia weak solution produced with rectifier 15 again after solution cooling absorption device 13 heats up with the ammonia spirit heat exchange in solution cooling absorption device 13 and mixes, then generator 11 is sequentially entered, solution heating generator 10, external heat generator 9 makes ammonia evaporation generate ammonia weak solution, form solution circulation, medium circulation by being located in the recycle heat pipeline in generator 11 and described absorber 12 passes to generator 11 by absorbing heat in absorber 12 in the process,
The ammonia steam generated by generator 11, solution heating generator 10, external heat generator 9 enters rectifier 15, and generation ammonia weak solution and mass percent purity are not less than the ammonia steam of 99.5%. described ammonia steam is condensed into the liquid of 50 DEG C after the second condenser 16 and second tunnel user's backwater carry out heat exchange, subsequently in subcooler 17 with from the second vaporizer 18, the exchange of-10 DEG C of low temperature ammonia heat of steam and be further cooled, again through the liquid ammonia becoming-10 DEG C of low-temp low-pressures after expansion valve 22 throttling expansion. the liquid ammonia of described low-temp low-pressure absorbs external environment heat subsequently into the second vaporizer 18 and is evaporated, and becomes-10 DEG C of low temperature ammonia steams. described low temperature ammonia steam is returned after being heated up by heat exchange heat absorption in described subcooler 17 and is sequentially sent to external refrigeration absorber 14, solution cooling absorption device 13 and absorber 12 are only absorbed by the water and form ammonia spirit, ammonia spirit in described solution cooling absorption device and absorber eventually enters into external refrigeration absorber 14, enter solution cooling absorption device 13 and absorb heat by being provided with the pipeline of the first solution pump 21 the ammonia concentrated solution own temperature in pipeline is raised, then mix with the ammonia weak solution from rectifier 15, it is sequentially sent to generator 11, solution heating generator 10 and external heat generator 9, form the circulation of cold-producing medium.
Heat user backwater is divided into two-way to be heated, and after first via backwater carries out heat exchange with the smoke evacuation of gas engine 1 in exhaust heat exchanger 20, then sequentially enters the first condenser 4 and cylinder sleeve heat exchanger 19 carries out heat exchange and makes return water temperature raise; Second road backwater enters the second condenser 16 after absorbing the absorption heat produced in external refrigeration absorber 14, for user after the second described condenser 16 carries out heat exchange intensification with ammonia steam, for user after the mixing of final two-way water return pipeline hot water.
Adopt this method to make low grade residual heat be fully used, make the coefficient of performance of system be improved significantly, be greatly improved the primary energy ratio of system.
Embodiment 3
Gas engine 1 drives compressor 2 to do work, it is the gaseous state of High Temperature High Pressure by the refrigerant compression of compression heat pump system, gaseous refrigerant first passes through oil eliminator 3, carry out heat exchange subsequently into the first condenser 4 with first via user's backwater and transfer heat to user's backwater, cold-producing medium is condensed into the high-pressure liquid that temperature is relatively low, enter reservoir 5, the first vaporizer is entered then through after becoming the liquid of low-temp low-pressure after expansion valve 6 throttling expansion, the first described vaporizer 7 absorbs the heat of external environment and is evaporated to gaseous state, the cold-producing medium of gaseous state enters compressor 2 through gas-liquid separator 8, it is compressed to the gaseous state of High Temperature High Pressure, it is thusly-formed a compression-type refrigeration agent circulation,
The smoke discharging residual heat of gas engine 1 carries out heat exchange as the driving heat source of the external heat generator 9 of absorption type heat pump system with the ammonia spirit in external heat generator 9, ammonia spirit in external heat generator 9 is added by smoke discharging residual heat and is thermally generated ammonia steam and temperature is 130 DEG C, pressure is 1.5MPa high temperature ammonia weak solution, described high temperature ammonia weak solution cools to 110 DEG C with ammonia spirit heat exchange by entering solution heating generator 10 equipped with the pipeline of the first solution pump 24, absorber 12 is entered after cooling to 80 DEG C then through solution choke valve 23 decompression, after ammonia weak solution absorbing ammonia steam in absorber 12, temperature is reduced to 60 DEG C, become denseer ammonia weak solution, subsequently in solution cooling absorption device 13, further absorbing ammonia steam makes ammonia spirit concentration raise further, finally enter external refrigeration absorber 14, absorb the low temperature concentrated solution of the ammonia steam formation 40 DEG C from subcooler 17,Second solution pump 21 is extracted the ammonia concentrated solution in external refrigeration absorber 14 out and is sent into pipeline, described pipeline enters the ammonia weak solution produced with rectifier 15 again after solution cooling absorption device 13 heats up with the ammonia spirit heat exchange in solution cooling absorption device 13 and mixes, then generator 11 is sequentially entered, solution heating generator 10, external heat generator 9 makes ammonia evaporation generate ammonia weak solution, form solution circulation, medium circulation by being located in the recycle heat pipeline in generator 11 and described absorber 12 passes to generator 11 by absorbing heat in absorber 12 in the process,
The ammonia steam generated by generator 11, solution heating generator 10, external heat generator 9 enters rectifier 15, and generation ammonia weak solution and mass percent purity are not less than the ammonia steam of 99.5%. described ammonia steam is condensed into the liquid of 40 DEG C after the second condenser 16 and second tunnel user's backwater carry out heat exchange, it is further cooled subsequently into subcooler 17 exchanges with-20 DEG C of low temperature ammonia heat of steam from the second vaporizer 18, again through the liquid ammonia becoming-20 DEG C of low-temp low-pressures after expansion valve 22 throttling expansion. the liquid ammonia of described low-temp low-pressure absorbs external environment heat subsequently into the second vaporizer 18 and is evaporated, and becomes-20 DEG C of low temperature ammonia steams. described low temperature ammonia steam is returned after being heated up by heat exchange heat absorption in described subcooler 17 and is sequentially sent to external refrigeration absorber 14, solution cooling absorption device 13 and absorber 12 are only absorbed by the water and form ammonia spirit, ammonia spirit in described solution cooling absorption device and absorber eventually enters into external refrigeration absorber 14, enter solution cooling absorption device 13 and absorb heat by being provided with the pipeline of the first solution pump 21 the ammonia concentrated solution own temperature in pipeline is raised, then mix with the ammonia weak solution from rectifier 15, it is sequentially sent to generator 11, solution heating generator 10 and external heat generator 9, form the circulation of cold-producing medium.
Heat user backwater is divided into two-way to be heated, and after first via backwater carries out heat exchange with the smoke evacuation of gas engine 1 in exhaust heat exchanger 20, then sequentially enters the first condenser 4 and cylinder sleeve heat exchanger 19 carries out heat exchange and makes return water temperature raise; Second road backwater enters the second condenser 16 after absorbing the absorption heat produced in external refrigeration absorber 14, for user after the second described condenser 16 carries out heat exchange intensification with ammonia steam, for user after the mixing of final two-way water return pipeline hot water.
Adopt this method to make low grade residual heat be fully used, make the coefficient of performance of system be improved significantly, be greatly improved the primary energy ratio of system.
Schematically the present invention and embodiment thereof being described above, this description does not have restricted, and shown in accompanying drawing is also one of embodiments of the present invention, and actual structure is not limited thereto. So; if those skilled in the art is enlightened by it, when without departing from the invention objective, element moulding, connected mode are without creationary design; the frame mode similar to this technical scheme and embodiment, all should belong to protection scope of the present invention.
Claims (1)
1. gas engine drives steam compressed with absorption combined heat pump Hot water units operation method, it is characterised in that it comprises the following steps:
Gas engine-driven compressor work, it is the gaseous state of High Temperature High Pressure by the refrigerant compression of compression heat pump system, gaseous refrigerant first passes through oil eliminator, carry out heat exchange subsequently into the first condenser and first via user's backwater and transfer heat to user's backwater, cold-producing medium is condensed into the high-pressure liquid that temperature is relatively low, enter reservoir, the first vaporizer is entered then through after becoming the liquid of low-temp low-pressure after expansion valve throttling expansion, the first described vaporizer absorbs the heat of external environment and is evaporated to gaseous state, the cold-producing medium of gaseous state enters compressor through gas-liquid separator, it is compressed to the gaseous state of High Temperature High Pressure, it is thusly-formed a compression-type refrigeration agent circulation,
The smoke discharging residual heat of gas engine carries out heat exchange as the driving heat source of the external heat generator of absorption type heat pump system with the ammonia spirit in external heat generator, ammonia spirit in external heat generator is added by smoke discharging residual heat and is thermally generated ammonia steam and temperature is 130～170 DEG C, pressure is 1.5～2.0MPa high temperature ammonia weak solution, described high temperature ammonia weak solution cools to 110～150 DEG C with ammonia spirit heat exchange by entering solution heating generator equipped with the pipeline of the first solution pump, absorber is entered after cooling to 80～140 DEG C then through the decompression of solution choke valve, after ammonia weak solution absorbing ammonia steam in absorber, temperature is reduced to 60～80 DEG C, become denseer ammonia weak solution, subsequently in solution cooling absorption device, further absorbing ammonia steam makes ammonia spirit concentration raise further, finally enter external refrigeration absorber, absorb the low temperature concentrated solution of the ammonia steam formation 40～60 DEG C from subcooler, ammonia concentrated solution in second solution pumped external refrigeration absorber sends into pipeline, described pipeline enters the ammonia weak solution produced with rectifier again after solution cooling absorption device heats up with the ammonia spirit heat exchange in solution cooling absorption device and mixes, then sequentially enter generator, solution heating generator, external heat generator make ammonia evaporation generate ammonia weak solution, forming solution circulation, the medium circulation by being located in the recycle heat pipeline in generator and described absorber passes to generator by absorbing heat in absorber in the process,
By generator, solution heating generator, the ammonia steam that external heat generator generates enters rectifier, generation ammonia weak solution and mass percent purity are not less than the ammonia steam of 99.5%, described ammonia steam is condensed into the liquid of 40～60 DEG C after the second condenser and second tunnel user's backwater carry out heat exchange, it is further cooled subsequently into subcooler exchanges with-20～5 DEG C of low temperature ammonia heat of steam from the second vaporizer, again through the liquid ammonia becoming-20～5 DEG C of low-temp low-pressures after expansion valve throttling expansion, the liquid ammonia of described low-temp low-pressure absorbs external environment heat subsequently into the second vaporizer and is evaporated, become-20～5 DEG C of low temperature ammonia steams, described low temperature ammonia steam is returned after being heated up by heat exchange heat absorption in described subcooler and is sequentially sent to external refrigeration absorber, solution cooling absorption device and absorber are only absorbed by the water and form ammonia spirit, ammonia spirit in described solution cooling absorption device and absorber eventually enters into external refrigeration absorber, by being provided with the pipeline entrance solution cooling absorption device absorption heat of the first solution pump, the ammonia concentrated solution own temperature in pipeline is raised, then mix with the ammonia weak solution from rectifier, it is sequentially sent to generator, solution heating generator and external heat generator, form the circulation of cold-producing medium,
Heat user backwater is divided into two-way to be heated, and after first via backwater carries out heat exchange with the smoke evacuation of gas engine in exhaust heat exchanger, then sequentially enters the first condenser and cylinder sleeve heat exchanger carries out heat exchange and makes return water temperature raise; Second road backwater enters the second condenser after absorbing the absorption heat produced in external refrigeration absorber, for user after the second described condenser and ammonia steam carry out heat exchange intensification.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610087543.0A CN105674558B (en) | 2016-02-16 | 2016-02-16 | Gas engine drives steam compressed and absorption combined heat pump Hot water units operation method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610087543.0A CN105674558B (en) | 2016-02-16 | 2016-02-16 | Gas engine drives steam compressed and absorption combined heat pump Hot water units operation method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN105674558A true CN105674558A (en) | 2016-06-15 |
| CN105674558B CN105674558B (en) | 2018-05-08 |
Family
ID=56305681
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201610087543.0A Active CN105674558B (en) | 2016-02-16 | 2016-02-16 | Gas engine drives steam compressed and absorption combined heat pump Hot water units operation method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN105674558B (en) |
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106595122A (en) * | 2016-12-07 | 2017-04-26 | 天津城建大学 | Series connection and parallel connection switching type heat supplying method of compressing absorbing hybrid heat pump of gas engine |
| CN106895603A (en) * | 2017-02-28 | 2017-06-27 | 天津城建大学 | Compression/absorb enclosed parallel connection composite fuel gas heat pump operation method |
| CN107461799A (en) * | 2017-07-07 | 2017-12-12 | 清华大学 | A kind of heating equipment and heat supply method |
| CN108731295A (en) * | 2018-06-13 | 2018-11-02 | 成都爱信智能技术有限责任公司 | A kind of recuperation of heat Gas Air Conditioner System |
| CN113686051A (en) * | 2021-08-16 | 2021-11-23 | 山东大学 | Open type compression absorption heat pump system for recovering water heat in high-temperature and high-humidity gas |
| CN113847753A (en) * | 2021-08-23 | 2021-12-28 | 深圳市燃气集团股份有限公司 | Natural gas cold and heat cogeneration system |
| CN113865143A (en) * | 2021-08-23 | 2021-12-31 | 深圳市燃气集团股份有限公司 | Refrigerating system powered by gas internal combustion engine |
| CN116907119A (en) * | 2023-07-12 | 2023-10-20 | 中国科学院高能物理研究所 | Superconductive accelerator waste heat recycling platform |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109579105B (en) * | 2018-10-30 | 2020-10-27 | 中国科学院理化技术研究所 | Gas absorption heat pump system |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0836058A1 (en) * | 1996-04-25 | 1998-04-15 | The Chugoku Electric Power Co., Inc. | Compression absorption heat pump |
| KR20030073942A (en) * | 2002-03-14 | 2003-09-19 | 진금수 | Heat pump type hot water heating apparatus |
| CN1804511A (en) * | 2006-01-23 | 2006-07-19 | 李华玉 | Compression-absorption combined heat pump heating system |
| CN101440998A (en) * | 2007-11-22 | 2009-05-27 | 海尔集团公司 | Heat pump water heater |
| CN201561564U (en) * | 2009-11-06 | 2010-08-25 | 清华大学 | Direct combustion air source absorption type heat pump hot water device |
-
2016
- 2016-02-16 CN CN201610087543.0A patent/CN105674558B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0836058A1 (en) * | 1996-04-25 | 1998-04-15 | The Chugoku Electric Power Co., Inc. | Compression absorption heat pump |
| KR20030073942A (en) * | 2002-03-14 | 2003-09-19 | 진금수 | Heat pump type hot water heating apparatus |
| CN1804511A (en) * | 2006-01-23 | 2006-07-19 | 李华玉 | Compression-absorption combined heat pump heating system |
| CN101440998A (en) * | 2007-11-22 | 2009-05-27 | 海尔集团公司 | Heat pump water heater |
| CN201561564U (en) * | 2009-11-06 | 2010-08-25 | 清华大学 | Direct combustion air source absorption type heat pump hot water device |
Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106595122A (en) * | 2016-12-07 | 2017-04-26 | 天津城建大学 | Series connection and parallel connection switching type heat supplying method of compressing absorbing hybrid heat pump of gas engine |
| CN106595122B (en) * | 2016-12-07 | 2019-03-08 | 天津城建大学 | The gas engine compression absorption composite heat pump heat supply method switched in series and parallel |
| CN106895603A (en) * | 2017-02-28 | 2017-06-27 | 天津城建大学 | Compression/absorb enclosed parallel connection composite fuel gas heat pump operation method |
| CN107461799A (en) * | 2017-07-07 | 2017-12-12 | 清华大学 | A kind of heating equipment and heat supply method |
| CN108731295A (en) * | 2018-06-13 | 2018-11-02 | 成都爱信智能技术有限责任公司 | A kind of recuperation of heat Gas Air Conditioner System |
| CN108731295B (en) * | 2018-06-13 | 2023-04-18 | 成都爱信智能技术有限责任公司 | Heat recovery gas air conditioning system |
| CN113686051A (en) * | 2021-08-16 | 2021-11-23 | 山东大学 | Open type compression absorption heat pump system for recovering water heat in high-temperature and high-humidity gas |
| CN113847753A (en) * | 2021-08-23 | 2021-12-28 | 深圳市燃气集团股份有限公司 | Natural gas cold and heat cogeneration system |
| CN113865143A (en) * | 2021-08-23 | 2021-12-31 | 深圳市燃气集团股份有限公司 | Refrigerating system powered by gas internal combustion engine |
| CN116907119A (en) * | 2023-07-12 | 2023-10-20 | 中国科学院高能物理研究所 | Superconductive accelerator waste heat recycling platform |
Also Published As
| Publication number | Publication date |
|---|---|
| CN105674558B (en) | 2018-05-08 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN105674558A (en) | Gas engine driven steam compressing and absorbing combined type heat pump hot water unit running method | |
| CN105089726B (en) | A kind of cooling heating and power generation system based on double pressure organic Rankine bottoming cycles | |
| CN106895603B (en) | Compression/absorption enclosed parallel connection composite fuel gas heat pump system operation method | |
| CN102650478B (en) | Trans-critical-compression/absorption composite refrigeration device utilizing low-grade heat | |
| CN103542597B (en) | A kind of power and refrigeration cogeneration system being suitable for recovery temperature-variable heat source | |
| CN105042931A (en) | Combined heat pump system adopting trans-critical circulation and absorption heat pump co-production | |
| CN106595122A (en) | Series connection and parallel connection switching type heat supplying method of compressing absorbing hybrid heat pump of gas engine | |
| CN103868278B (en) | Low-grade energy drives CO2absorption type cold-hot chp system | |
| CN110500910B (en) | Thermal mass decoupling method of thermal mass decoupling heat exchanger | |
| CN104963732A (en) | Combined circulating energy supplying system | |
| CN102155815A (en) | Steam jet refrigeration system based on double-fluid | |
| CN103673384A (en) | Refrigeration system using waste heat of engine | |
| CN105004095A (en) | Compound heat pump system for co-production by adopting trans-critical circle and two-stage absorption type heat pump cycle | |
| CN207741379U (en) | A kind of absorption deep refrigerating system of industrial waste heat driving | |
| CN110552749A (en) | Transcritical carbon dioxide circulation waste heat power generation system of coupling lithium bromide absorption refrigeration | |
| CN102384604B (en) | Double-temperature-heat-source injection-type refrigeration system | |
| CN102052801B (en) | Refrigeration and heat pump device driven by using high-temperature flue gas | |
| CN205383781U (en) | Compression of driving vapour of gasengine and absorption combined type heat pump water heater group | |
| CN109506391A (en) | Thermal drivers are without the Trans-critical cycle CO for pumping absorption auxiliary supercooling2Refrigeration system | |
| CN206755651U (en) | Compression/absorption enclosed parallel connection composite fuel gas heat pump assembly | |
| CN206131515U (en) | A air -cooled absorbed refrigeration machine for car | |
| CN210089181U (en) | Absorption type transcritical carbon dioxide two-stage compression refrigeration system | |
| CN204902309U (en) | Multistage plate type evaporation absorbed refrigeration device | |
| CN205102453U (en) | Solar energy doublestage ejector refrigeration system | |
| KR101038249B1 (en) | Air cooling apparustus for gas turbine |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |