CN101514642A - Residual heat reclaiming method, residual heat reclaiming system and used working fluid of absorption liquid - Google Patents
Residual heat reclaiming method, residual heat reclaiming system and used working fluid of absorption liquid Download PDFInfo
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- CN101514642A CN101514642A CNA2008100096530A CN200810009653A CN101514642A CN 101514642 A CN101514642 A CN 101514642A CN A2008100096530 A CNA2008100096530 A CN A2008100096530A CN 200810009653 A CN200810009653 A CN 200810009653A CN 101514642 A CN101514642 A CN 101514642A
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Abstract
The invention discloses an absorption-type residual heat power generation or heat acquisition and drive power using method under condition of a low-temperature heat source. The invention also relates to an absorption-type residual heat reclaiming system and a used gas-salt working fluid. The low-temperature heat source obtained from industrial waste heat is used as a heating working medium so that a working fluid of absorption liquid consisting of a salt absorbent and ammonia gas or carbon dioxide absorbed agent from an absorber forms an absorbent and a high-pressure overheated absorbed agent in a regenerator through the heat exchange process under the heating condition; the gasified overheated absorbed agent enters a turbine machine to provide energy for producing power through a turbine expansion step; the produced power can directly drive a power generating unit for power generation or connection with other power drive equipment for providing the needed power; and the produced power can be also used as a heat source and is transported to heat exchange equipment for heating. The low pressure absorbed agent completing the heat release process is exhausted from the turbine step, returns the absorption step and is re-contacted with the absorbent from the regeneration step to form the absorption liquid; and the absorption liquid reenters the next thermodynamic circulation process.
Description
Technical field
The present invention relates to absorption exhaust heat recovering method, relate in particular to absorption cogeneration under the low-temperature heat source condition or heat collection and as the method that drives power.The invention still further relates to this absorption residual neat recovering system and employed gas-salt work fluid, as ammonia-salt work fluid.
Background technique
All have a large amount of industrial waste heats to produce every day in the industrial production, as flue gas and process waste heat etc.It is low-grade that this heat is considered to usually, technically exists suitable difficulty and can't realize because of it is recovered in, and therefore usually has a large amount of residual heat resources to be wasted.At petrochemical enterprise the discharging of a large amount of low-temperature waste heat is just arranged, as the hot water of the big flow that discharges in the heavy-oil catalytic device, water temperature is about 120 ℃ usually.For the heat recovery of such low-temperature heat source, water vapor system commonly used in the prior art is because water vapor pressure is not enough and low equipment and the system of making of energy density is huge, and existence moves and safeguard the problems of aspect; With regard to other lower boiling working medium such as hydrocarbon fluids such as butane, pentane, also there is the problem be difficult for condensation, inflammable and environmental protection aspect, and because low enthalpy characteristics, just require big pressure ratio, need multistage large equipment, this must increase the investment and the operation cost of equipment, thereby usually is difficult to be utilized effectively.
Once proposed to absorb mixed working fluid to form in the prior art and be used for energy acquisition and utilization such as circulating generation class low-temperature heat sources such as Kalina with ammonia-water.As US 4,346,561 disclose and have a kind ofly produced system with ammonia and water as the low-temperature heat source circulating energy of working medium, and this method is particularly useful for the application in sea water heat energy conversion field.US 5,029, and 444 also relate to method and the relevant device that carries out the low-temperature heat source circulating generation with ammonia and water mixed working fluid, and its heat source temperature is generally 230-400 °F.Have equally in these inventions above propose owing to those problems that water is produced, and essential use separator separation of ammonia-water, equipment cost and energy-output ratio height.
The objective of the invention is to overcome or alleviate prior art described to the small part shortcoming or provide the replacement scheme of usefulness.
Summary of the invention
The present inventor absorbs the [thermodynamic principle of adsorptive process based on gas such as ammonia or carbon dioxide and salt mixture, is used for the low temperature heat energy recycling, has realized heat recoveries such as low temperature heat energy generating, has finished the present invention.
According to a first aspect of the invention, provide a kind of absorption exhaust heat recovering method, to carry out the heat recovery of high efficient cryogenic thermal source, this method comprises the following steps:
A) in the future the self absorption device by absorbing agent and be absorbed absorption liquid that agent forms and from the heating working medium of low-temperature heat source in regenerator heat exchange to form absorbing agent and high pressure superheater is absorbed agent;
B) high pressure superheater that step a) is produced is absorbed agent and is transported to turbine engine to produce power or to be transported to heat transmission equipment so that thermal source to be provided;
C) will in adsorber, contact and form absorption liquid with the agent that is absorbed behind step b) turbine engine or heat transmission equipment from the absorbing agent of step a).
According to a second aspect of the invention, provide the recovery waste heat system of the absorption exhaust heat recovering method of a kind of the present invention of being applicable to, this system comprises:
A) regenerator, be used for self absorption device in the future by absorbing agent and be absorbed absorption liquid that agent forms and from the heating working medium heat exchange of low-temperature heat source to form absorbing agent and high pressure superheater is absorbed agent;
B) turbine engine or heat transmission equipment use regenerator to produce high pressure superheater and are absorbed agent generation power or thermal source is provided,
C) adsorber is used for absorbing agent that regenerator is produced to contact with the formation absorption liquid with the agent that is absorbed behind turbine engine or heat transmission equipment.
D) solution pump is used for absorption liquid is failed back regenerator.
Exhaust heat recovering method of the present invention and described recovery waste heat system are advisable with the heat recovery that is used for low-temperature heat source, and general heat source temperature is lower than 200 ℃, but is not less than 70 ℃, is suitably 90 ℃-120 ℃.These thermals source comprise the low-temperature water heating of the big flow that discharges as petroleum chemical enterprises such as heavy-oil catalytic devices etc.
According to a third aspect of the invention we, what be provided for above-mentioned exhaust heat recovering method or recovery waste heat system is inorganic salts with the absorbing agent, as lithium nitrate, sodium thiocyanate, potassium rhodanide, potassium carbonate etc. or for organic and inorganic absorption or sorbent or mixture be absorbed the absorption liquid that agent is gas such as ammonia or carbon dioxide or steam or mixture composition.
The absorption liquid of forming based on gas such as ammonia of the present invention or carbon dioxide and salt, except having advantages such as transformation efficiency height, equipment are simple, also owing to the use of ammonia or carbon dioxide etc. have inexpensive relatively, nonflammable, be different from greenhouse gases and advantages such as relative environmental protection.And, comparing with traditional water steam, ammonia absorption system of the present invention has the high advantage of energy density, is example as the waste heat source with 110 ℃, and the energy density of water vapor system is 1200kJ/m
3, and the ammonia absorption system energy density of the same terms is designed to 2600-2800kJ/m
3Even for example gas leakage meeting such as ammonia is detrimental to health, but, pungent smell when slight the effusion, just can in time avoid escaping injury owing to can making people's vigilance.And ammonia of the present invention-salt absorption process is compared with the ammonia-water absorption process of prior art, saved in the prior art the essential separator that uses, both saved equipment investment, saved again and separated required energy.
Description of drawings
Fig. 1 is for using the [thermodynamic process of the absorption liquid of forming with ammonia-inorganic salts to carry out the schematic representation of low-temperature heat source cogeneration flow process based on the present invention;
Fig. 2 is the schematic representation of the low-temperature heat source cogeneration flow process of one embodiment of this invention, has wherein increased cooler and reheater;
Fig. 3 is the schematic representation of the low-temperature heat source cogeneration flow process of yet another embodiment of the invention, has wherein increased molten brilliant condenser.
Embodiment
In order to provide the new method that is suitable for the low-temperature heat source heat recovery with relevant reclaiming system and be applicable to that the gas of this method and salt mix the absorption liquid of forming, the inventor has developed new [thermodynamic process, this process comprises unit such as absorption, regeneration, turbine expansion and heat exchange as shown in Figure 1.In the absorption step of this [thermodynamic, as the absorption liquid of working medium by absorbing agent be absorbed agent and form, thereafter in regeneration step this absorbent solution through pipeline enter regenerator with from the heating working medium heat exchange of low-temperature heat source, form absorbing agent and high pressure superheater and be absorbed agent; In this step, can use solution pump to increase the pressure of fluid working substance.And the heating of the heat exchange in the regenerator makes being absorbed the agent vaporization and reaching overheated in this fluid working substance.This vaporization is overheated is absorbed agent and enters turbine engine and provide energy to produce power through the turbine expansion step, and the power of this generation can directly drive generator set and be used for generating or be connected with other power drive device, and required drive is provided; Also can be used as thermal source be transported to heat transmission equipment be used for the heating.Finish low pressure after the heat release process and be absorbed and be back to absorption step after agent is discharged contact formation absorbent solution again from the turbine step, enter [thermodynamic process next time again with absorbing agent from regeneration step.
Any temperature is not higher than 200 ℃ low-temperature heat source, as all applicable thermals source of doing heat recovery of the present invention such as the useless flue gas of industry, process waste heats, but be that 90 ℃-110 ℃ the low-temperature waste heat of factory of petrochemical refining discharging is as the thermal source of heat recovery of the present invention as serviceability temperature.
Consideration according to the selection of employed low-temperature heat source and above new [thermodynamic process, the present inventor absorbs the principle of adsorptive process based on gas and saline admixture, developed new absorbing agent-be absorbed agent working fluid through test of many times, absorbing agent wherein is selected from conventional organic and inorganic absorbent or sorbent, inorganic salts, especially low inorganic salts of water content, should be lower than 0.3wt% as water content, especially be lower than 0.2wt%, as lithium nitrate, sodium thiocyanate, potassium rhodanide and potassium carbonate etc., or their mixture, as at least a non-volatile inorganic salts; And form the gas or the steam that agent correspondingly can be high evaporation under the low temperature that be absorbed of working fluid of absorption liquid with absorbing agent, or the mixture of the two, be preferably selected from ammonia or carbon dioxide, or the mixed gas of the two.As being to be absorbed in the embodiment of agent with ammonia, the absorbing agent of selecting for use should have big absorptive capacity as far as possible, and it is not high again comparatively suitable to finish parsing and absorption temperature under relatively lower temp.Its action principle is at a lower temperature, and absorbing agent absorbs ammonia and is made into rich ammonia solution, with pump rich ammonia solution is transported in the regenerator, at high temperature ammonia is parsed.The ammonia of High Temperature High Pressure enters the turbine engine adiabatic expansion, and heat energy is changed into kinetic energy, realizes the purpose that heat energy utilizes again.Conveniently be with ammoniacal liquor and inorganic salts by 25-36wt%, as, the ammonia content of 27-30wt% shifts to an earlier date premix, is mixed with absorption liquid premixed liquid stream and adds adsorber, press the excessive mol ratio adding ammonia that can be up to 30: 1 of ammonia then.Temperature and pressure is measured the ratio situation that can determine ammonia-salt in the system.
This absorbing agent-be absorbed and also can contain other conventional component known in the art in the agent working fluid, as remove the siccative of moisture content in the system, corrosion inhibitor and surface active agent etc.; With respect to the absorbing agent solid weight meter, siccative can be as silica gel, molecular sieve, calcium oxide or its mixture etc., and its consumption is generally 0-6wt%, is preferably 0.1-5.5wt%, more preferably 2-5wt%; The consumption of corrosion inhibitor such as metal surface corrosion inhibitor can be 0-2wt%, is preferably 0.01-1wt%; Can be organic alcohols with surface active agent, as 2-Ethyl Hexanol etc., its consumption is generally 0-2wt% with respect to the absorbing agent solid weight meter, is preferably 0.01-1wt%, as is 50-500ppm.Should be lower than 25wt% but these add the components contents summation with respect to the absorbing agent solid weight meter, preferably be lower than 22wt%; The content of corresponding fertile absorber should account for more than the 52wt% of absorbing agent solid mixture weight, preferably more than 55wt%.And everywhere absorbing agent salinity can change to some extent according to thermal source is corresponding with ambient temperature in the system, with 110 ℃ temperature waste heat sources is example, the import salinity of regenerator for example is 55-65wt%, and the adsorber ingress is 60-68wt%, with respect to salt and ammoniacal liquor and other additive gross weight meter.
Provide the capital equipment of an embodiment that is used to implement [thermodynamic process of the present invention with reference to figure 1, comprised adsorber, regenerator, turbine engine and generator.Wherein the low-temperature heat source that obtains from industrial waste heat as heating working medium regenerator by heat transfer process make from adsorber by above-mentioned absorbing agent and be absorbed that working fluid of absorption liquid that agent forms forms absorbing agent under heating condition and high pressure superheater is absorbed agent.
From the absorbing agent of regenerator be absorbed agent steam from the low pressure of turbine engine and in adsorber, combine and form working fluid of absorption liquid.Also can fresh be absorbed agent and make and be absorbed the agent steam content in the adsorber and should significantly be in excess in Absorbed dose by replenishing.The ratio of the two is generally 10: 1-30: 1 mol ratio.In order to make absorbing agent and to be absorbed agent and to reach abundant mixing and contact and be convenient to heat discharge, the design of adsorber should be selected liquid distribution trough and herringbone baffle arrangement for use, can in adsorber, install filler additional, and adopt two-stage indirect heat exchange form that absorption process institute liberated heat is taken away by cooling medium, the optional water of transition flow body, water vapor, hexylene glycol solution, heat conduction wet goods medium in the middle of it.Absorbing agent should be controlled at 25 ℃-70 ℃ with the temperature that is absorbed agent in the adsorber, is preferably 30 ℃-40 ℃, and pressure then is 0.1-0.51MPa (1-5 barometric pressure), is preferably 0.2-0.41MPa (2-4 barometric pressure).
Enter the optional regenerator that is provided with of to flow through before the regenerator from the absorption liquid of adsorber, as shell-and-tube heat exchanger, carry out abundant heat exchange, to improve systematic function; Also can increase solution pump and be used to make the pressure of fluid working substance to be improved, make its operation smooth and easy more balanced with systemic circulation.The absorption liquid temperature that send this moment is 90 ℃-120 ℃, is preferably 105-110 ℃, and makes system pressure reach 1.01-3.04MPa (10-30 barometric pressure), is preferably 1.52-2.23MPa (15-22 barometric pressure), as is 1.72-1.93MPa (17-19 barometric pressure).
Adsorber is in operation excessive and may produce undesirable fixed gas in system and go wrong owing to being absorbed agent, can relief opening be set in absorber overhead for this reason, in time gets rid of the fixed gas that is produced.
The absorption liquid that regenerator is sent near threshold state enters regenerator, with the middle transition fluid of industrial waste heat heating in regenerator fully heat exchange heat this fluid working substance as method through countercurrent flow, make being absorbed the agent vaporization and reaching overheated wherein.This moment, this superheat steam temperature can reach 130 ℃, as be 90-120 ℃, be preferably 105-110 ℃, and pressure can reach 1.01-3.04MPa (10-30 barometric pressure), be suitably 1.52-2.23MPa (15-22 barometric pressure), as be 1.72-1.93MPa (17-19 barometric pressure).The type of regenerator comprises multiple different conventional heater, as shell-and-tube heat exchanger, standard standup reboiler etc.Regenerator is advisable to be designed to two-stage indirect heat exchange form equally.Employed middle transition fluid can be selected from water, water vapor, hexylene glycol solution and heat conduction wet goods heat transferring medium.
The superheated vapor that regenerator is sent is through pipeline, reach and enter turbo machine after optional exsiccator that is provided with such as spreading type exsiccator are removed the moisture content that may exist, by reducing vapor pressure and enthalpy, from this superheated vapor, extract available energy, and flow to the output of generator realization electric power; This power also can directly be used, as driven pump and compressor etc. except that being used for generating.
Fig. 2 is the operation schematic representation about the capital equipment of another embodiment of implementing [thermodynamic process of the present invention.For Fig. 1, increased the cooler that is absorbed agent and the reheater that makes the steam superheat raising that enters turbine engine of cooling outflow turbine engine in this system.This cooler and reheater can be provided with simultaneously or only setting is wherein a kind of all can.Increase reheater and also can play the effect that assurance has only single phase gas to enter turbine engine, thereby can improve the efficient of system.And, except that the effect that has improved exhaust heat recovery power generation of the present invention, also can be designed to the cogeneration of heat and power process owing to increased additional heat transmission equipment, benefit is further improved.Can collect heat by cooler and/or adsorber as cooling water or medium, collected heat is used for the utilization of domestic water, heating and farming, animal husbandry and fishery etc.
And, also can in system, increase fluid pressure merit reclaiming system, this system is used for absorbent stream that the high-pressure regeneration device the is produced pressure to the adsorber will can be delivered to solution pump by whirligig (as the hydraulic turbine machine etc.) in it, solution pump is moved, and need not external impetus.Make thus from the energy of system's output and utilized more fully.
In system equipment running illustrated in figures 1 and 2, the pipeline of system and parts such as irregular cleaning will be stopped up.Therefore also should increase the detergent line parts, as the valve that cleans usefulness is set, manage the operation of these parts with sensory-control system.Also can utilize hydrothermal solution ammonia to wash easy plugging road, dissolve the crystal that may form.Show in system with reference to figure 3 for this reason the connection that makes the condenser that crystal dissolves is set.
Above through with reference to the accompanying drawings embodiment of the present invention being described in detail.The manufacturing of the method and apparatus of heat recovery of the present invention and running cost are extremely low, are applicable to low-temperature heat source, and absorption liquid concentration can adjust according to heat source temperature, efficient is higher, provide the simplification power generation system that increases benefit, and cooling water can be used for cogeneration of heat and power, raising energy recovery rate.
The present invention will be further described below in conjunction with specific embodiment.These embodiments only are the explanations to the present invention's possibility method, and should not think limitation of the scope of the invention.
Embodiment:
The Annual output of present embodiment employing North China petro-chemical corporation is that 90 ℃-120 ℃ low-temperature waste heat of the oil refining apparatus discharging of 5,000,000 tons of oil products is introduced the heat recovery circulatory system of the present invention as thermal source.Equipment and operating conditions thereof that this system uses are as follows:
1. as the heater of regenerator: shell-and-tube heat exchanger, absorption liquid are that anhydrous ammonia-sodium thiocyanate salt solution is walked tube side.
The type selecting parameter:
1) the thermal source inlet temperature is that 120 ℃-130 ℃, thermal source outlet temperature are 90 ℃;
2) NH
3-sodium thiocyanate salt solution inlet/outlet temperature is respectively 86 ℃, 110 ℃;
3) heat exchange quantity 〉=425.18kW;
4) fixed tube sheet type, design pressure 2.5MPa, Maximum operating pressure is at 1.8MPa;
5) heater surface is long-pending: 37m
2
2. exsiccator
Adopt the bucket formula to huddle siccative, can switch use by two exsiccators.
The experiment operating conditions:
1) the highest pressure-bearing 3.0MPa, the real work maximum pressure is at 1.2MPa;
2) it allows forward voltage drop p≤1kg/cm
2
3) the specified water absorption rate of drying medium is 31 (mass ratioes);
4) rate-of flow 570kg/h; Working medium: overheated ammonia steam.
5) two exsiccators switch use, and the exsiccator volume is 0.005m
3
3. adsorber
Select liquid distribution trough and herringbone baffle arrangement for use, and load filler, absorption temperature is 40 ℃.
4. absorber cooler
1) heat exchange quantity 680kW;
2) cooling water is respectively 32 ℃, 42 ℃ into and out of the temperature of adsorber;
3) total heat and mass area is about 57m
2
5. solution circulation pump
Any minute leakage all can cause the leak crystal to separate out badly damaged rotating component.
Adopt canned motorpump, the pump head design pressure should reach more than the 3.0MPa.The medium contact position must not have copper and Cuprum alloy member.
Lift 10bar, flow 900kg/s, two of quantity, wherein one standby.
6. solution regenerator
Select shell-and-tube heat exchanger for use
The type selecting parameter:
1) poor ammonia solution inlet temperature is 110 ℃, and rich ammonia solution inlet temperature is 40 ℃.
2) heat exchange quantity 167kW.
3) design pressure 3MPa, the real work maximum pressure is at 1.2MPa.
4) heat exchange area 15m
2
7. ammonia-salt solution expansion valve is selected pressure regulator valve for use.
8. solution pump: lift 20bar, flow 4234kg/hr, two of quantity, wherein one standby.
9. turbine engine
Select Elliott AYRT Turbine turbine engine for use.
This turbine engine design medium is a water vapor; Generated output is 22.4kW;
Operating conditions:
Inlet: 1080kPa; 294 ℃
Outlet: 350kPa
Maximum operating conditions: the 4827kPa that allows; 399 ℃; 689kPa (outlet).
Rotating speed: 2900rpm; 3045rpm (the highest); 3502 (trip)
Be working medium with ammonia steam in the present embodiment, inlet still selects 1080kPa, outlet 350kPa.
With reference to the [thermodynamic process of figure 2, the following cycling of carrying out present embodiment:
Rich ammonia solution from regenerator is heated to 110 ℃ by coal heating and water in heat exchanger, enter knockout drum, isolates overheated ammonia and poor ammonia solution.Enter the turbine engine acting after the overheated ammonia drying device drying.Poor ammonia solution after weary gas (40 ℃, 0.48MPa) and the step-down is mixed into adsorber.
110 ℃ of poor ammonia solutions are cooled to 45 ℃ through regenerator and the rich ammonia solution heat exchange of circulation, enter adsorber through the throttle valve step-down.Rich ammonia solution behind the absorbing ammonia (40 ℃) enters regenerator and is heated to 86 ℃ after solution pump boosts, enter regenerator, repeats above-mentioned circulation.
With ammonia steam and water vapor respectively as the ratio of the generated output of medium:
P
a/P
w＝(ΔH
aV
aρ
a)/(ΔH
wV
wρ
w)＝1.4
Experimental result demonstration ammonia system can be generated electricity:
1.4×22.4＝31.36Kw
This embodiment shown that the present invention has and has been applicable to that low-temperature heat source carries out the characteristics of exhaust heat recovery power generation, and can adjust absorption liquid concentration according to heat source temperature, and the suitable ammonia degree of superheat is provided, and do not need extra afterburning fuel, and equipment is simple, safety; Also satisfy turbine engine simultaneously and import and export the designing requirement that all is higher than dew point, can effectively prevent the problem of droplet erosion infringement turbine blade.
Claims (35)
1. the method for recovery waste heat comprises the following steps:
A) the comprising absorbing agent and be absorbed the anhydrous absorption liquid of agent and be absorbed agent to form absorbing agent and high pressure superheater of self absorption device in the future with heating working medium heat exchange in regenerator from low-temperature heat source;
B) high pressure superheater that step a) is produced is absorbed agent and is transported to turbine engine to produce power or to be transported to heat transmission equipment so that thermal source to be provided;
C) will in adsorber, contact and form this anhydrous absorption liquid with the agent that is absorbed behind step b) turbine engine or heat transmission equipment from the absorbing agent of step a).
2. the process of claim 1 wherein that the step b) turbine engine connects generator with generating.
3. the process of claim 1 wherein that the step b) turbine engine connects the power-actuated equipment that needs.
4. the method for claim 3 wherein needs power-actuated equipment to comprise pump or compressor.
5. according to the absorbing agent preheating that the process of claim 1 wherein that the anhydrous absorption liquid that forms in the step c) was produced by step a) before reentering regenerator.
6. according to the process of claim 1 wherein that the high pressure superheater that step a) produces is absorbed agent drying device drying before entering turbine engine.
7. according to the process of claim 1 wherein that the agent that is absorbed of coming out from turbine engine was cooled before entering adsorber.
8. according to the method for claim 6, wherein the high pressure superheater of drying is absorbed agent and was heated before entering turbine engine to improve temperature.
9. according to the process of claim 1 wherein that described regenerator is the two-stage indirect heat exchange, the middle transition fluid is water, water vapor, hexylene glycol solution or conduction oil.
10. according to the process of claim 1 wherein that adsorber is the two-stage indirect heat exchange, the middle transition fluid is water, water vapor, hexylene glycol solution or conduction oil.
11. the process of claim 1 wherein that absorbing agent is made up of at least a non-volatile inorganic salts.
12. the method for claim 11, wherein inorganic salts comprise lithium nitrate, sodium thiocyanate, potassium rhodanide, potassium carbonate or their mixture.
13. the method for claim 11, wherein based on absorption liquid gross weight meter inorganic salt content greater than 52wt%.
14. each method of claim 1-13 also comprises the siccative based on absorption liquid gross weight meter 0-5wt% in the wherein said anhydrous absorption liquid.
15. the method for claim 14, wherein said siccative are any or its mixture in calcium oxide, silica gel, the molecular sieve.
16. each method of claim 1-13 also comprises the surface active agent of counting 0-2wt% based on the absorption liquid gross weight in the wherein said anhydrous absorption liquid.
17. the method for claim 16, wherein said surface active agent are 2-Ethyl Hexanol.
18. each method of claim 1-13, wherein being absorbed agent is anhydrous ammonia.
19. the recovery waste heat system comprises
A) regenerator, be used for self absorption device in the future by absorbing agent and be absorbed absorption liquid that agent forms and from the heating working medium heat exchange of low-temperature heat source to form absorbing agent and high pressure superheater is absorbed agent;
B) turbine engine or heat transmission equipment use regenerator to produce high pressure superheater and are absorbed agent generation power or thermal source is provided,
C) adsorber is used for absorbing agent that regenerator is produced to contact with the formation absorption liquid with the agent that is absorbed behind turbine engine or heat transmission equipment.
D) solution pump is used for absorption liquid is failed back regenerator.
20. the recovery waste heat system of claim 19 further comprises the generator that is connected on the turbine engine.
21. the recovery waste heat system of claim 19 further comprises the power-actuated equipment of the need that are connected on the turbine engine.
22. the recovery waste heat system of claim 21 wherein needs power-actuated equipment to comprise pump or compressor.
23. the recovery waste heat system of claim 19 comprises that further preheating enters the regenerator preheater of adsorber before.
24. the recovery waste heat system of claim 19 further comprises exsiccator.
25. the recovery waste heat system of claim 19 further comprises cooler.
26. the recovery waste heat system of claim 19 further comprises fluid pressure merit reclaiming system, the pressure of the absorbent stream that this system produces the high-pressure regeneration device to the adsorber will can be delivered to solution pump in it by whirligig.
27. the recovery waste heat system of claim 26, wherein said whirligig is the hydraulic turbine machine.
28. the recovery waste heat system of claim 19, solution pump is driven by turbine engine, need not external impetus.
29. anhydrous working fluid of absorption liquid, comprise absorbing agent and be absorbed agent, wherein said absorbing agent is for being selected from lithium nitrate, the non-volatile inorganic salts of sodium thiocyanate, potassium rhodanide, potassium carbonate or their mixture, and it is described that to be absorbed agent be anhydrous ammonia or carbon dioxide or the mixture of the two.
30。The anhydrous absorption liquid working liquid body of claim 29, wherein based on absorption liquid gross weight meter, described non-volatile inorganic salt content is greater than 52wt%.
31. the anhydrous working fluid of absorption liquid of claim 1 also comprises the siccative based on absorption liquid gross weight meter 0-5wt% in the wherein said anhydrous absorption liquid.
32. the anhydrous working fluid of absorption liquid of claim 31, wherein said siccative are any or its mixture in calcium oxide, silica gel, the molecular sieve.
33. the anhydrous working fluid of absorption liquid of claim 1 also comprises the surface active agent of counting 0-2wt% based on the absorption liquid gross weight in the wherein said anhydrous absorption liquid.
34. the anhydrous working fluid of absorption liquid of claim 33, wherein said surface active agent are 2-Ethyl Hexanol.
35. each described anhydrous working fluid of absorption liquid of claim 29-34, wherein said to be absorbed agent be anhydrous ammonia.
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