CN103403476A

CN103403476A - Thermally activated pressure booster for heat pumping and power generation

Info

Publication number: CN103403476A
Application number: CN2012800103350A
Authority: CN
Inventors: 徐建国
Original assignee: Individual
Current assignee: Individual
Priority date: 2011-02-23
Filing date: 2012-02-23
Publication date: 2013-11-20
Also published as: WO2012116174A1; US20140053594A1

Abstract

Thermally activated systems and related processes for raising the pressure of a gaseous working fluid are described. The systems and processes can be used for both winter heating and summer cooling with increased efficiency. They can also be used for other applications in need of an efficient thermally driven compressor, such as a power generation process.

Description

The supercharging device that is used for the heat driving of pump heat and generating

Cross

This application is according to 35USC § 119(e) to enjoy the application number of submitting to on February 23rd, 2011 be that 61/446,010 U.S. Provisional Patent Application and the application number submitted on June 23rd, 2011 are 61/500,594 the corresponding priority of U.S. Provisional Patent Application.Above-mentioned U.S. Provisional Patent Application integral body is included into this paper as a reference.

The statement of concession power

The approval number that the present invention is issued by little company of the National Science Foundation innovation item of U.S. government is 1113100 fund assistance.U.S. government has certain right in the present invention.

Background technology

Heating in building and cooling can be at more than 20% of american energy total amount consumed.Vehicle air conditioning has also consumed the part transport fuel.In addition, in process industrial, be especially in chemical industry and power generation industries, also need material is carried out heating and cooling.Along with the rising of energy prices, the hope that drives the heating and cooling system with solar thermal energy becomes more and more stronger.Maximum in the demand to air-conditioning, in the summer of the sweltering heat that network load peaks, solar energy is just in time very abundant.Solar water heater be applied in many places, comprise south of europe and SOUTHERN CHINA, just in develop rapidly.In the summer of sweltering heat, the heat that solar water heater provides is often superfluous.The heat of this surplus being used for driving air-conditioning in such,, to meet the high demand of this moment to cooling, is the good scheme of suiting measures to differing conditions in terms of time.

Yet heat pump (TAHP) system that the heat of present state-of-the-art lithium bromide (LiBr) water absorption type drives can not be suitable for house and coml is cooling for warming up because it make water as cold-producing medium, salting liquid as absorbent.The vapour pressure of water is very low, and the heating and cooling system in any living space must be at a quite high vacuumizing while making water as working medium (cold-producing medium), and this makes this systems bulky.In addition, lithium bromide is a kind of salt, and it has corrosivity, if operating condition is well controlled, may not freeze.This means that these TAHP systems need the experienced operator to operate.In addition, lithium bromide-water absorption system is not suitable for the heating during lower than the solidification point of water when environment temperature, because at 0 ℃ of lower water, can freeze.Therefore, lithium bromide-water sorption type heat pump is commonly called " the cooling machine of lithium bromide ", and namely they are used to be only applicable to cooling.Lithium bromide-water absorption system need to, greater than the heat of 88 ℃,, to avoid the problem of freezing, therefore can not drive with general solar water heater usually.

The heating Energy Efficiency Ratio of TAHP (heating COP) is greater than 1, and the heating COP of traditional combustion gas or oil burner is less than 1.The heating COP of a good single-action TAHP in theory can be greater than 1.7, and the TAHP of economic benefits and social benefits in theory has a higher heating COP.Therefore, can reduce more than 40% with the needed heat energy of TAHP system heating of a single-action.The energy-saving effect of the TAHP system of economic benefits and social benefits can be more remarkable.Because heating energy consumption is huge, the TAHP that is used for space heating is very attractive.

Regrettably, after years of researches and development, the higher technology of the thermal efficiency of this goose hangs high is not also by commercialization.Some reasons are the TAHP technology in default of a safety and efficiently.The TAHP system that present lithium bromide-water absorbs or it is derivative uses pure water as working medium.When they can not be used to need most, namely the space heating when environment temperature is near or below 0 ℃, icing because water is understood under 0 ℃.

Theoretically, ammonia can be used for the heat pump of vapor compression heat pump and heat driving as working medium.Yet one of problem of ammonia is that its tool is highly toxic, is not therefore to be applicable to house and vehicle.In order to alleviate the problem of toxicity, the secondary loop is necessary.This has increased the cost of system.In addition, the heat of the absorption of ammonia in water is the latent heat of vaporization that is far longer than ammonia.The heat exchange duty that these needs are larger is used for heavily boiling at the cooling and destilling tower of the absorption process of ammonia absorption heat pump.This means the cost of a very large heat exchanger and the larger heat energy degradation in heat exchanger.This increased again conversely TAHP cost, reduced its COP value.Even use so-called GAX system, it adopts the heat of emitting in more effective absorption process to be used for the method for separated, the single-action of ammonia-aqueous systems heating COP is still only approximately 1.6, or about 0.6 cooling COP, significantly lower than 0.75 the COP value of being about of lithium bromide absorption system.Ammonia also has other problems, comprises it to copper and these two corrosivity for the manufacture of the optimal material of heat exchanger of aluminium, and needs very clean heating surface without oil etc.These problems have greatly limited the application of the heat pump that ammonia drives as the heat of the heating of working medium and idle call.

Murphy and Phillips have proposed one and have used CClF ₂CHClF is working medium, and with the ETFE(ethyl tetrahydrofurfuryl ether, a kind of high boiling molecular weight is 130 organic oxygen-containing compound), heat driving type heat pump as solvent (is seen Kevin P.Murphy and Benjamin A.Phillips, " DEVELOPMENT OF ARESIDENTIAL GAS-ABSORPTION HEAT PUMP ", submitted for presentation at the18th Intersociety Energy Conversion Engineering Conference August21-26,1983, Orlando, Florida).Such system does not have freezing of lithium-bromide absorption-type refrigerating machine and ammonia absorption heat pump, some shortcomings of corrosion and toxicity aspect.Based on the development to them, Murphy and Phillips estimate that its cooling COP is 0.65, heating COP is 1.50.Yet such process is also by commercialization, and wherein in part because of them, having adopted viscosity and the higher solvent of thermal capacity and used is not best heat-exchange system.In addition, working fluid, CClF ₂CHClF, have the ability of destroying ozone, is therefore worthless.

Therefore, be improved the demand of efficiency in the heating and cooling field.This is using the TAHP heating, greatly reduces thereby replace fuel burning heater and resistance heater the energy consumption aspect that is used for heating, thereby and with the hot of solar water heater or from the heat of the cooling water of vehicle motor, freezing and greatly reducing especially outstanding for aspect cooling energy consumption.The present invention is by the pressure charging system of the gaseous working medium that a kind of heat is provided drives, i.e. booster that heat drives, and at aspects such as TAHP, should be used for meeting such unsatisfied demand.Such system also can be used for generating with the heat of low energy position.

Summary of the invention

One total aspect in, the present invention relates to the pressure charging system of the gaseous working medium that a heat drives.This system comprises that one has under 1 atmospheric pressure bubble point less than the working medium (working fluid) of 20 ℃, and molecule contains at least one oxygen atom (O), and contain nitrogen (N), sulphur (S), phosphorus (P), at least a atom in fluorine (F), the dew point under 1 atmospheric pressure is at the organic oxygen-containing compound solvent more than 130 ℃, and their combination.

According to one embodiment of present invention, the system that heat drives comprises:

During absorbing solvent, the working medium that will be essentially gaseous state under lower pressure forms the absorber of liquid solution;

Remove the cooler of heat from absorber;

A supercharging device that increases the pressure of liquid solution, to obtain highly pressurised liquid solution; And

One is separated at least one high-pressure working medium stream that basically gasifies and the generator of a highly pressurised liquid absorbent stream with high-pressure solution;

The bubble point of working medium wherein under an atmospheric pressure is below 20 ℃; Absorbent is comprised of the component of working medium and solvent, and solvent molecule is to contain at least one oxygen atom (O), and contains nitrogen (N), sulphur (S), phosphorus (P), at least a atom in fluorine (F), the dew point under 1 atmospheric pressure is at the organic oxygen-containing compound more than 130 ℃.

In another embodiment, the present invention relates to the pressure of the system of a heat driving for increasing gaseous working medium, its feature comprises:

Described working medium is selected from R134a, dimethyl ether, R152a, CH ₃I(R13I1), propane, isopropyl alkane, propylene, iso-butane normal butane, HFO1234yf, and their combination; Absorbent comprises the component of described working medium and is selected from METHYLPYRROLIDONE (NMP), methyl-sulfoxide (DMSO), dimethyl formamide (DMF), dimethylacetylamide (DMAc), and the solvent of their combination composition;

Remove the cooler of heat from absorber;

A liquid solution supercharging device that makes the pressure increase of at least a portion liquid solution;

The generator of the working medium stream of a gasification basically that high-pressure solution is separated at least one high pressure and the liquid absorbent stream of a high pressure;

A high-pressure working medium that at least a portion is evaporated basically flows the condenser of condensation basically;

Basically the working medium stream of condensation is cooling with at least a portion, has got cold working medium stream, and with the heat exchanger of another material flow heating;

The excessively cold working medium flowing pressure of at least a portion is reduced, to obtain a decompressor of low pressure working fluid stream;

Evaporate at least in part at least a portion low pressure working fluid stream, obtain the working medium stream of vaporization at least partly, remove simultaneously the evaporimeter of the heat of other thermals source, its feature comprises:

When hot drive system was used for heating, other thermals source wherein were the environment in the space of a sealing; When hot drive system was used for the space of cooling sealing or process flow, wherein other thermals source were space or the process flow of sealing;

Unclassified stores stream in heat exchanger comprises the working medium stream of the described at least part of vaporization of at least a portion; It becomes the low pressure working fluid stream that is essentially gaseous state after being heated, wherein at least a portion is sent to absorber;

Be used for cooling at least a portion high pressure absorbent liquid stream, thereby obtain second heat exchanger of supercooled liquid absorbent liquid stream; And

Second pressure decreased that makes at least a portion subcooled liquid absorbent stream, obtain the dropping equipment of low pressure liquid absorbent stream, and wherein the described low pressure liquid absorbent stream of at least a portion is transported to absorber.

Of the present invention another total aspect, the present invention relates to the technique of the pressure of the increase gaseous working medium that a kind of heat drives.This technique comprises that its bubble point of using under 1 atmospheric pressure is less than the working medium of 20 ℃, and molecule contains at least one oxygen atom (O), and contain nitrogen (N), sulphur (S), phosphorus (P), at least a atom or its combination in fluorine (F), the dew point under 1 atmospheric pressure is at the solvent molecule of the organic oxygen-containing compound more than 130 ℃.

According to one embodiment of present invention, the technique that heat drives comprises:

The working medium that under low pressure will be essentially gaseous state absorbs in solvent and forms liquid solution;

Reduce phlegm and internal heat from absorber;

Increase the pressure of liquid solution to obtain highly pressurised liquid solution; And

Described high-pressure solution is divided into high-pressure working medium stream and highly pressurised liquid absorbent stream that at least one gasifies basically in generator, the bubble point of working medium wherein under 1 atmospheric pressure is less than 20 ℃, absorbent contains this working medium and molecule contains at least one oxygen atom (O), and contain nitrogen (N), sulphur (S), phosphorus (P), at least a atom or its combination in fluorine (F), the dew point under 1 atmospheric pressure is at the solvent molecule of the organic oxygen-containing compound more than 130 ℃.

According to another embodiment, the supercharging technique of the gaseous working medium that the heat that the present invention relates to drives, its feature comprises:

To be under low pressure that the working medium stream of gas absorbs in liquid absorbent stream and obtains liquid solution basically in absorber.Wherein said working medium is selected from and comprises R134a, dimethyl ether, R152a, CH ₃I(R13I1), propane, isopropyl alkane, propylene, iso-butane, normal butane, HFO1234yf, and their combination; Absorbent contains the component of working medium and is selected from METHYLPYRROLIDONE (NMP), dimethyl sulfoxide (DMSO) (DMSO), dimethyl formamide (DMF), dimethylacetylamide (DMAc), and the solvent that forms of their combination;

Remove and reduce phlegm and internal heat from absorber;

Increase the pressure of at least a portion liquid solution to obtain highly pressurised liquid solution with a supercharging device;

Described high-pressure solution is separated into high-pressure working medium stream and a highly pressurised liquid absorbent stream that at least one gasifies basically in generator;

Basically the high-pressure working medium stream that condensation at least a portion is vaporized basically in condenser, the working medium that obtains condensation basically flows;

Cooling at least a portion working medium stream of condensation basically, must be cold working medium stream in heat exchanger, heats simultaneously another material flow;

Be reduced by at least the pressure of a part of working medium stream, to obtain the overcooled working medium stream of low pressure;

Vaporization at least a portion low pressure working fluid stream,, to obtain the working medium stream of vaporization at least partly, remove heat from another thermal source simultaneously in evaporimeter, and its feature comprises:

When hot drive system was used for heating, other thermals source wherein were the environment in the space of a sealing; When hot drive system was used for the space of cooling sealing or process flow, wherein other thermals source were space or the process flow of sealing; And

Unclassified stores stream in heat exchanger comprises the working medium stream of part vaporization in evaporimeter at least, obtains being essentially the low pressure working fluid stream of gaseous state after being heated;

Basically deliver to absorber for the low pressure working fluid stream of gaseous state at least partly with described;

Cooling at least a portion highly pressurised liquid absorbent stream obtains an overcooled liquid absorbent stream in the second heat exchanger;

Reduction at least a portion is crossed the pressure of cold absorbent liquid stream and is obtained low pressure absorbent liquid stream;

At least a portion low pressure liquid absorbent stream is sent into absorber.

Other side of the present invention, feature and advantage, can be apparent after narration below.This narration comprises detailed description and the appending claims of invention and preferred embodiments thereof.

Description of drawings

The general introduction of front, and following detailed description of the present invention, when read in conjunction with the accompanying drawings, can understand better.In order to set forth the present invention, accompanying drawing has been showed presently preferred embodiment.Yet, should be appreciated that definite arrangement and the means shown in the present invention is not limited to.

In the accompanying drawings:

Fig. 1 shows an example of a single-action system according to an embodiment of the invention;

Fig. 2 shows an example of double effect system according to an embodiment of the invention;

Fig. 3 illustrates an example of electricity generation system according to an embodiment of the invention.

The specific embodiment

Various publications, article and patent are cited or describe in background and specification.Each in these lists of references is all quoted and is made it to become one with the latter with integral body.Miscellaneous Documents, behavior, material, equipment, article or similarly comprised that discussion in this manual is to be for this patent provides the purpose of taking over from the past and setting a new course for the future.Such discussion is not meaned and is admitted that any or all these items form the disclosure of relevant any invention or a part of prior art of claim.

Unless otherwise defined, all scientific and technical terminologies used herein with those skilled in the art the relevant term with the present invention usually understood have identical implication.In addition, some term separately has definition in specification.All patents of quoting in this specification, disclosed patent application and publication are quoted seemingly and are comprised in the present invention fully by integral body.Must be pointed out, used herein, in appending claims, singulative " ", " one " and " being somebody's turn to do " also comprise plural number, unless context is clearly pointed out not to be like this.

Lexical or textual analysis

Absorbent: absorbent is that a kind of some gas that can absorb in absorber forms the liquid of liquid solution.Absorption process need to be followed heat extraction usually.

Absorber: absorber is a kind of process equipment, is used for gas dissolution forming liquid solution in absorbent.

Bubble point: the temperature during the liquid start vaporizer., for pure component, at 1 atmospheric bubble point, be its boiling point.

Energy Efficiency Ratio (COP) or cooling COP: the producible amount from the low-temperature heat source heat absorption of a energy consumption in the pump thermal process.

Heating COP: the heat of the heating use that a energy consumption that is used for heating produces.

COP is related by following formula with heating COP: heating COP=1+COP

Cooling water: refer in the context of the present invention for cooling heat transfer medium.Mainly comprise water, also can comprise other component such as ethylene glycol, alcohols, and salt etc.

Counterflow heat exchanger: the heat exchanger that heat exchange both sides fluid flows in the opposite direction, wherein, the fluid that is heated and is cooled in described fluid is separated by the good solid material thin layer of heat conductivity.

Desuperheating a: steam higher than dew point is cooled to or near its dew-point temperature.

The dew-point temperature of fluid: the gas at this temperature starts to condense.The dew point of pure component is identical with the boiling point of pure component under 1 atmospheric pressure.

Generator: the process equipment that is used for mixture is separated into the material flow of two (or a plurality of) composition.In this patent, the principle of the separation of generator is the volatile difference between different component.Also can be called as desorption device or distilling apparatus or evaporation element or evaporimeter with the cell process equipment of generator same principle in this patent in other places.It is different from generates the Dian Ji – latter and refers to a kind of device that mechanical energy is converted to electric energy.

Heat pump: heat can be delivered to the process system of higher temperature from lower temperature.The conventional air-conditioning machine is the example of a heat pump in the present invention, traditional refrigerator and to be used for the conventional heat pump for space that heats during lower than heated space when outdoor temperature as the same.

Pump heat: heat is got to higher temperature from a lower temperature.

HFC: fluorohydrocarbon, a class chemical compound, is characterized in that, at its molecule, comprises hydrogen (H), carbon (C), fluorine (F).

Organic oxygen-containing compound: the organic compound that contains one or more oxygen atoms (O) in its molecule.

Polyalcohol: the alcohol that contains a plurality of-OH base in its molecule.The example of polyalcohol includes, but not limited to ethylene glycol, diethylene glycol, and propane diols.

Solvent: the liquid that can dissolve liquid and/or gas componant.

Subcooler: liquid cools is arrived the heat exchanger of temperature lower than its bubble point temperature.

Overheated: with dew point or near the steam heated of its dew-point temperature to higher temperature.

The heat pump (TAHP) that heat drives: mainly by the heat pump of the thermal source from a higher temperature to the hot-fluid driving of the lower hot trap of temperature.For example, traditional lithium bromide refrigerator is the heat pump that a kind of heat drives.

Working medium: be used for heat pump, electricity generation system, or the fluid that changes its phase states of the booster of heat driving.In heat supply, in air-conditioning and refrigeration application, working medium is also referred to as cold-producing medium.Working medium can contain nearly 5% solvent in some embodiment of this patent.

Embodiments of the invention adopt working medium and the solvent that does not destroy or basically do not damage the ozone layer, and have improved the supercharging device performance of hot driving, and it can be used for TAHP or power generator etc.The present invention relates to heat pump and the air-conditioning system of a low cost and heat driving efficiently, its operating pressure is higher than traditional lithium bromide cooling-water machine.They can operate below the solidification point of water, the heat of available relatively low energy position, as from the business solar water heater out hot water and from the hot cooling water that vehicular engine is returned, drive.The supercharging device of heat driving does not use acrid material according to an embodiment of the invention, and the freezing potential problems of absorbent do not occur in operating process.

One total aspect in, the present invention relates to the pressure charging system of the gaseous working medium that a heat drives.The system that this heat drives comprises:

Remove the cooler of heat from absorber;

The bubble point of working medium wherein under an atmospheric pressure is below 20 ℃; Absorbent is comprised of the component of working medium and solvent, and solvent molecule is for containing at least one oxygen atom (O), and contains nitrogen (N), sulphur (S), phosphorus (P), at least a atom in fluorine (F), the dew point under 1 atmospheric pressure is at the organic oxygen-containing compound more than 130 ℃.

According to another embodiment of the invention, the system that heat drives also comprises:

One will be at least a portion of the high-pressure working medium stream of evaporation basically condenser of condensation basically;

At least a portion of the working medium of condensation basically stream is cooling, got cold working medium stream, and with the heat exchanger of another material flow heating;

When hot drive system was used for heating, other thermals source wherein were the environment in the space of a sealing; When hot drive system was used for the space of cooling sealing or process flow, wherein other thermals source were space or the process flow of sealing.

Those of ordinary skill in the art is readily appreciated that the system that drives when a heat is used for space or the process fluid of a sealing of heating, it can be used for direct-fired confined space or process fluid, or by the fluid that is used for heating confined space or process fluid or medium, carries out indirect.Therefore, the thermal source of other in evaporimeter can be the heat that directly or indirectly obtains from environment.

Equally, when hot drive system is used for the space of a cooling sealing or process fluid, it can be used directly to cooling confined space or process fluid, or central fluid or the cooling medium by cooling space for cooling sealing or process fluid carries out indirectly.Therefore, the thermal source of other in evaporimeter can be to come from directly or indirectly confined space or process fluid.

The example of confined space or process fluid includes, but not limited to the space in a room or building or vehicle, or the process fluid in factory or device.The environment of the space of a sealing or a process fluid can be the space of confined space process fluid outside.

In another embodiment, the system that heat drives also comprises for cooling at least a portion working medium stream of condensation basically, has got cold working medium stream, and heated simultaneously the heat exchanger of another fluid.Then at least a portion is crossed cold working medium stream and be sent to dropping equipment to obtain low pressure working fluid stream.Other fluids that heat in heat exchanger comprise the described working medium stream of vaporizing at least partly in evaporimeter of at least a portion, obtain being essentially the low pressure working fluid stream of gaseous state, and wherein at least a portion is sent in absorber.

In another embodiment, the system that heat drives also comprises with absorber and being connected, the second dropping equipment that the pressure that the high pressure absorbent liquid that comes from generator for reducing at least a portion flows flows to obtain low pressure absorbent liquid.The described low pressure absorbent of at least a portion liquid stream is used for absorber.

In another embodiment, the system that heat drives also comprises that fluid passage is arranged at bottom with the middle part of supercharging device, generator and generator, out high pressure absorbent liquid stream is must be cold absorbent liquid stream from the generator bottom to be used for cooling at least a portion, and the highly pressurised liquid solution that comes from supercharging device of heating and partial gasification at least a portion is to obtain the second heat exchanger of a high-pressure two-phase stream simultaneously.Then the high-pressure two-phase stream of gained be sent to the middle part of generator; The excessively cold absorbent liquid stream of at least a portion is sent to the second decompressor to obtain low pressure absorbent liquid stream.

The middle part of described generator may be between the generator top and bottom any one position.

According to one embodiment of present invention, the system of this heat driving can comprise the generator more than.Such as the system that heat according to an embodiment of the invention drives may comprise a high pressure generator, a middle pressure generator lower than high pressure generator pressure, and between the top of high pressure generator and middle pressure generator, hot the interchange can be arranged.

In another embodiment, the present invention relates to comprise the electricity generation system of decompressor according to an embodiment of the invention, it is characterized in that, at least a portion comes the high-pressure working medium of basically the vaporizing stream of the generator of self-heating drive system expand in decompressor and produce mechanical energy, and the consequent decompressor tail gas of at least a portion working medium is absorbed in absorber by described low pressure absorbent liquid stream.

Of the present invention another total aspect, the present invention relates to the technique that a kind of heat of the pressure for increasing gaseous working medium drives.This technique comprises:

Reduce phlegm and internal heat from absorber;

Described high-pressure solution is separated into high-pressure working medium stream and a liquid high pressure absorbent stream that at least one gasifies basically in generator;

The bubble point of working medium wherein under 1 atmospheric pressure less than 20 ℃, absorbent contains this working medium and molecule contains at least one oxygen atom (O), and contain nitrogen (N), sulphur (S), phosphorus (P), at least a atom or its combination in fluorine (F), the dew point under 1 atmospheric pressure is at the solvent molecule of the organic oxygen-containing compound more than 130 ℃.

According to another embodiment of the invention, the technique that heat drives further comprises:

Basically condensation at least a portion is vaporized basically in generator high-pressure working medium stream, the working medium that obtains condensation basically flows;

Reduce at least a portion pressure of the working medium stream of condensation basically, to obtain low pressure working fluid stream;

Vaporization at least a portion low pressure working fluid stream in evaporimeter,, to obtain the working medium stream of vaporization at least partly, remove the heat of other thermals source simultaneously, wherein:

When hot drive system is that other thermals source wherein are the environment in the space of a sealing for when heating; When hot drive system is during for the space of cooling sealing or process flow, wherein other thermals source are space or the process flow of sealing.

The technique that according to another embodiment of the invention heat drives also is included in a heat exchanger cooling at least a portion working medium stream of condensation basically, got cold working medium stream, and heat simultaneously another fluid, it is characterized in that, the overcooled working medium stream of at least a portion is sent to decompressor, and described another fluid comprises at least a portion gasifies at least partly in evaporimeter working medium, and the low pressure working fluid that is essentially gaseous state that the working medium that wherein by at least a portion, is gasified at least partly heats gained is used to absorber.

In another embodiment of the present invention, the technique of heat driving also comprises:

Be reduced by at least a part and obtain low pressure absorbent liquid stream from the pressure of the high pressure absorbent liquid stream of generator;

At least a portion low pressure absorbent liquid stream is delivered in absorber.

At another embodiments of the invention, the technique that heat drives further comprises:

The liquid stream of the high pressure absorbent that cooling at least a portion obtains from the generator bottom in the second heat exchanger, obtain an overcooled absorbent liquid stream, heating and partial gasification at least a portion come from the highly pressurised liquid solution of above-mentioned supercharging device simultaneously, obtain high-pressure two-phase stream;

At least a portion high-pressure two-phase stream is sent into the centre position of generator; And

The overcooled absorbent liquid stream of at least a portion is delivered to the second decompressor to obtain low pressure absorbent liquid stream.

An embodiment in the technique that heat according to the present invention drives, use more than one generator in separating step.For example, an embodiment according to a heat driving technique according to the present invention can comprise high pressure generator of use, a middle pressure generator lower than high pressure generator pressure, is characterized in that, between the top of described high pressure generator and middle pressure generator, heat exchange is arranged.

In another embodiment, the technique of heat driving is used to generating.This technique further comprises:

The high-pressure working medium of basically vaporizing in decompressor expansion at least a portion also produces mechanical energy; And

Absorb the low pressure working fluid stream that at least a portion is discharged from decompressor in absorber.

In one embodiment of the invention, described working medium is selected from R134a(1,1,1,2-HFC-134a), the dimethyl ether, (F of R152a ₂HC-CH ₃), CF ₃I(R13I1), propylene, propane, cyclopropane, iso-butane, normal butane, HFO1234yf, and their combination.

In another embodiment of the present invention, described solvent is to be selected from organic oxygen-containing compound to contain nitrogen (N) in its molecule, phosphorus (P), fluorine (F), in sulphur (S) atom at least one, and their combination, and at 1 its dew point of atmospheric pressure, be greater than 130 ℃, the viscosity in the time of 20 ℃ is lower than 2.5 centipoises.

In one embodiment of the invention, this solvent is selected from METHYLPYRROLIDONE (NMP), methyl-sulfoxide (DMSO), dimethyl formamide (DMF), dimethylacetylamide (in DMAc) and combination thereof.

Absorbent comprises working medium and solvent.Absorbent is also referred to as poor working medium liquid in this application.

Working medium is absorbed and forms rich worker quality liquid solution in absorber or absorption step.This liquid solution is also referred to as weak solution in this application.

In one embodiment of the invention, the highly pressurised liquid solution from above-mentioned supercharging device is divided at least one main flow and one stream.Wherein time stream forms the total flow of highly pressurised liquid solution

(mole), and be transported to the top of generator.And main flow is heated in heat exchanger and the part vaporization, obtains the two-phase logistics, and namely liquid and steam, then be transported to the generator centre position.

In another embodiment of the present invention, with subcooler cooling at least a portion from condenser produce, the working medium stream of condensation basically, and the described working medium stream that carrys out at least part of vaporization of flash-pot of at least a portion that gasifies of going forward side by side of heating simultaneously.The latter may contain

(mole) liquid.

Fig. 1 has shown an example according to a single-effective absorption heat pump embodiment of the present invention.In this process, the low pressure working fluid stream (306) and the low pressure liquid absorbent (314) that are essentially gaseous state are sent to absorber (31), obtain liquid solution (308).Consequent rich working medium solution or weak solution (308) are transported to a pump (32) to obtain solution (309) a little less than high pressure, are divided into again subsequently a main flow (310) and time flow (312).Weak solution main flow (310), be generally 80-99%(mole) weak solution, basically be heated and part vapour in the heat exchanger of adverse current (33), consequent high-pressure two-phase logistics (311) is transported to the entrance in the centre position that is positioned at described generator (34).And the weak solution of high pressure time stream (312) is generally

(mole), be not heated a higher entrance that just is sent to described generator (34).Described generator (34) is a destilling tower, liquid (313), the i.e. absorbent of poor working medium component at the bottom of generation high-pressure working medium steam (301) and tower.

The high-pressure working medium steam (301) of tower top is condensed in condenser (35), releases heat.This condensate liquid is divided into two material flow: get back to the backflow (315) at generator top, and carry out overcooled remainder (303) in the heat exchanger that is essentially adverse current or subcooler (30).The backflow of this system (315) is the very little part in condenser working medium stream out, usually less than 10%(mole).Offer the heat Q of the bottom section of generator (34) _GIt is the reboiling heat that is used to provide destilling tower.This heat exchange can be carried out in inside or the outside of generator.

Basically the working medium of condensation (303), by all the low pressure working fluids of gasification streams (305a) are namely roughly cooling in counterflow heat exchanger at subcooler (30) basically in evaporimeter (13).Resulting overcooled working medium (304) is in choke valve (12) step-down.Produced thus temperature lower two phase flow (305).This temperature lower two phase flow (305) heat in evaporimeter (13) and basically be evaporated.Outside heat (110) is used for evaporation this two phase flow (305).This outside heat can be to obtain from environment when system is used to heat; , when system is used to may come from room air or process flow (110) when cooling, produce the material flow (112) under lower temperature.The temperature of the material flow at lower temperature (112) is lower than 303 temperature.Substantially fully the working medium (305a) of vaporization further heats and basically is gasified totally in subcooler (30).Then, the low pressure gaseous working medium (306) of consequent gasification is basically absorbed by vapor (314) in absorber (31), release heat (Q at the temperature of the temperature higher than material flow 112 _b).The removal of this heat, can carry out in the one or more heat exchangers in absorber.

High pressure absorbent (313) is cooling in the heat exchanger of adverse current (33) roughly, and step-down in choke valve (36),, to produce low pressure absorbent (314), absorbs in absorber (31).

The heat exchange scheme of the uniqueness in this technique makes efficiency obviously improve.Because the pressure in lithium bromide refrigerator is very low, at least some special according to an embodiment of the invention hot swapping schemes of the inapplicable employing of lithium bromide refrigerator.

For the simplification system, the backflow (315) at the top of described generator (34) can be taken away.This moment, time stream (312) was transported to the top of the generator (34) that backflow gets back to usually.In this case, working medium (301) can contain some a small amount of solvents.In order to alleviate this situation, allow to comprise some liquid from evaporimeter (13) working medium (305) out, usually exist (mole) in scope.We find when using the subcooler of adverse current (30) basically to be used for the working medium (303) of cooling condensation basically, and to from condenser out be further vaporization and when heating of the working medium 305a of steam basically, the remaining liq in all working medium (305a) all can evaporate in subcooler (30) basically.From our analog study, we are surprised to find, and such simplification not only can not cause decrease in efficiency, and on the contrary, cooling COP value increases approximately 1%.Therefore, we think that this is a preferred embodiment.

Embodiments of the invention also comprise the heat pump of economic benefits and social benefits or multiple-effect and their application.

Fig. 2 has demonstrated an example of a double effect system.This technique and show that in Fig. 1 the difference between technique is as follows:

Be divided into two strands from pump (55) highly pressurised liquid solution out.Process flow (409) be depressured in choke valve (67) than the pressure of the solution (408) of pump (55) upstream high at middle pressure.The middle pressure solution liquid of gained is further divided into major part (410) and less important part (412).The major part (410) that is essentially the middle pressure solution liquid in the middle pressure heat exchanger (56) of adverse current is heated and the part vaporization, and the middle pressure two-phase flow (411) that obtains is sent to charging aperture under middle pressure generator (57).Middle pressure solution liquid time stream (412) is directly sent into the upper feeding mouth of middle pressure generator (57).Middle pressure generator (57) top produces the middle pressure working medium stream (431) that is essentially gas.From bottom also produce contain working medium few pressure absorbent (413).Then press absorbent (413) cooling in the middle pressure subcooler (56) that is basically a contra-flow heat exchanger in.What obtain excessively cold contains the further step-down in choke valve (59) of the few middle press liquid of working medium.

At first basically be heated the high pressure heat exchanger of adverse current (68) from pump (55) high-pressure solution (420) out.Take out effluent (422) from heat exchanger (68), and deliver to the top charging aperture of high pressure generator (69).The remainder of highly pressurised liquid solution roughly is being further heated and the part vaporization in the high pressure heat exchanger of adverse current (68).Resulting high-pressure two-phase flows (421), is sent to the lower end charging aperture of high pressure generator (69).High pressure generator (69) in bottom or lower position heated by heat Qg.It is the high steam stream (423) of working medium basically that high pressure generator (69) produces from top, and contains the few absorbent of working medium amount (425) from the bottom output.

The steam flow of high pressure tower top (423) is in reboiler/condensor (60) condensation of the bottom section that is arranged in medium pressure column (57).The consequent cold high pressure condensate of pure working medium basically is divided into two strands: be sent back to the backflow (433) at high pressure generator (69) top, remaining part can the subcooler (61) in middle pressure generator (57) in by further supercooling.Cross cold high-pressure working medium and then, in choke valve 62 step-downs, produce one two phase flow, mix with the refrigerant vapor (431) that comes from middle pressure generator (57) top subsequently.

By medium pressure column top refrigerant vapor out and the two phase flow of coming from valve (62) mixed form pressure refrigerant vapor (401) be sent to condenser (68), emit heat.Consequent working medium condensate liquid is divided into two strands: the backflow (432) that is sent back to middle pressure generator (57) top be sent to the further excessively cold liquid working substance (403) of middle pressure subcooler (50) that is essentially contra-flow heat exchanger.

The absorbent stream (425) that produces from high pressure generator (69) the hp heat exchanger of adverse current (68) basically by excessively cold.With the cold absorbent stream of the mistake of gained (426) at first in choke valve (63) step-down.The low pressure absorbent stream (427) of gained, mix with the low pressure absorbent stream (428) that forms at choke valve (59) thus, then is sent to absorber (54) and reuses.

The remainder of this flow process and the flow process in Fig. 1 are as good as.

Similarly, the backflow of high and medium voltage generator (433) and (432) also can be taken away, and inferior incoming flow (422) and (412) are delivered to respectively height, the top of middle pressure generator.In this case, the working medium at generator top stream (431) and (423) will contain some solvents, usually in the scope of 10ppm to 5%.In this case, the working medium stream 305a that leaves evaporimeter (53) preferably contains 0.1-5%(mole) liquid, then allow it in subcooler (50) evaporation fully basically.

In this article, those skilled in the art can easily know, system and technique can be used for heating or space or the process-stream of a cooling sealing according to an embodiment of the invention, as the process flow in interior of building or vehicle or industrial process.When this type systematic is used for when cooling, what remove in evaporimeter is the heat of confined space or process-stream, and the heat of condenser and absorber is discharged in environment.When being used for heating system, evaporimeter absorbs heat from environment, and condenser and absorber provide heat for confined space or process stream.Also can cause this type systematic to use same system along with the variation in season, such as the function by conversion condenser and evaporimeter be used for warming and cooling in summer.

For the global warming potential (GWP) that reduces working medium, and still keep the incombustibility of working medium, in a preferred embodiment, working medium can comprise one or more organic principles, as R134a, and CF ₃I, dimethyl formamide, or the compound of HFO1234yf.Dimethyl ether is due to its good macroscopic property, and cost is low, and is nontoxic, low GWP character, and the boiling point of a slightly high R134a is than the selected example of doing.Mixing of R134a makes working medium nonflammable.Because the boiling point of two components is very approaching, the behavior of this mixture is the spitting image of azeotropic mixture.CF ₃The GWP value of I is 1.Therefore, CF ₃In the mixture of I and dimethyl ether, the low-down global warming value GWP that dives is arranged.On the other hand, although it consumes ozone latent energy value very little (less than 0.008, likely less than 0.0001), CF ₃The mixture of I and dimethyl ether, be considered to have certain ODP (ODP).The GWP of HFO1234yf is in 4 left and right, and is more much smaller than 1430 values of R134a, but inflammable a little.

Many hydro carbons and organic oxygen-containing compound have required performance: have boiling point higher than 130 ℃ (or for mixed solvent 1 atmospheric pressure dew-point temperature greater than 130 ℃), and relatively cheap, and with above-mentioned working medium, mix, thereby can be used as solvent.The base oil of lubricating oil for example, polyalcohol, as ethylene glycol, triethylene glycol, propane diols, DPG, tetraethylene glycol dimethyl ether, and product of the condensation reaction between glyme or ethylene glycol and aldehydes or ketones etc.The base oil of lubricating oil, tetraethylene glycol dimethyl ether (or as using the glyme that combines in the Solexol process), ethylene glycol, the general goods chemicals unit prices such as triethylene glycol are lower and toxicity is also low, therefore, by us, paid the utmost attention to.

We have used a lot of solvents, comprise hexadecane, ethylene glycol, and diethylene glycol (DEG), triethylene glycol, tetraethylene glycol dimethyl ether has carried out analog computation to this system.Found that, contain and be selected from N, P, F, and S, its boiling point is greater than the low-molecular-weight organic oxygen-containing compound of 130 ℃, as METHYLPYRROLIDONE (NMP), and dimethyl sulfoxide (DMSO) (system of DMSO atom), dimethyl formamide (DMF), dimethylacetylamide (DMAc), as solvent, has higher COP value and much lower heat exchanger UA value, and this because of its less molecular mass (for example is, NMP is 99 g/mols, DMSO is 78 g/mols, and dimethyl formamide is 73 g/mols, and DMAc is 87 g/mols.Tetraethylene glycol dimethyl ether is 280 g/mols by comparison), specific heat (specific heat as NMP is 0.40, and the specific heat of tetraethylene glycol dimethyl ether is 0.49).They also should have larger heat transfer coefficient and relative low viscosity (at 20 ℃, NMP:1.65 centipoise, DMSO:2.0 centipoise, DMF:0.92 centipoise, DMAc:2.0 centipoise.By comparison, tetraethylene glycol dimethyl ether: 5.8 centipoises).

For example, the physics of other of NMP, health and fire resistance are as shown below:

Boiling point: 396 °F (202 degree Celsius)

Freezing point :-11 °F (-24 degree Celsius)

Flash-point: 199 °F (93 ℃)

Spontaneous combustion: 518 °F (270 ℃)

Explosion limit: lower limit: 0.99%, UEL: 3.9%

Toxicity data: the 3914 oral rat LD50 of mg/kg

Those of DMSO are as follows:

Boiling point: 372 °F (189 ℃)

Freezing point: 66 °F (19 ℃)

Flash-point: 192 °F (89 ℃)

Spontaneous combustion: 419 °F (215 ℃)

Explosion limit: lower limit: 2.6%, UEL: 42%

Toxicity data: acute oral toxicity (LD50): 7920 mg/kg [mouse]

Acute dermal toxicity (LD50): 40000 mg/kg [rat]

DMF's is as follows:

Boiling point: 307 °F (153 ℃)

Freezing point :-78 °F (61 ℃)

Flash-point: 136.4 °F (58 ℃)

Spontaneous combustion: 833 °F (445 ℃)

Explosion limit: lower limit: 2.2%, UEL:15.2%

Toxicity data: ORL rat LD50 is 2800 mg/kg

IPR rat LD50 is 1400 mg/kg

IVN rat LD502000 mg/kg

IPR rat LD50 is 1000 mg/kg

DMAc's is as follows:

Boiling point: 325.4 °F (165 ℃)

Freezing point: 1.5 °F (18.6 ℃)

Flash-point: 150.8 °F (66 degree Celsius)

Spontaneous combustion: 914 °F (490 ℃)

Explosion limit: lower limit: 1.8%, UEL: 11.5%

Toxicity data: acute oral toxicity (LD50): 7920 mg/kg [mouse].

Rat acute percutaneous toxicity (LD50): 40000 mg/kg.

In a preferred embodiment, in the following description NMP because its superior solvent that is chosen as of combination property.Yet other members in table also may have the value of preferable some attribute.Therefore, comprise, but be not limited to, dimethyl sulfoxide (DMSO), dimethyl formamide, acetamide, NMP, the combination of one or more such component, may can become preferred solvent in some specific condition.

Although by with incoming flow, carrying out heat exchange in the counterflow heat exchanger basically outside generator, these material flow also can be cooling by dropping liq in generator inside at the liquid of the bottom of generator illustrated in figures 1 and 2.In absorber, from the bottom rich working medium solution out on absorption tower can be used for after supercharging by with absorber in the material flow heat exchange absorb the heat that some are emitted from absorber.

Heat pump according to an embodiment of the invention is to be suitable for the cooling of living space or heating, in the application of house and vehicle, and in the business application.Use in such system and be used for heating, can reduce widely fuel consumption, and for air conditioning applications, it can use the cooling water of solar water heater or car engine, thereby can reduce widely summer in sweltering heat when need for electricity reaches peak value to the electricity needs of air-conditioning and expensive, and the electric power that produces of the liquid fuel combustion that becomes more expensive.

It should be noted that the principle of the system of a heat driving according to an embodiment of the invention according to this absorption system, can be used as the compressor that a kind of heat drives.Such thermocompressor also can have other purposes.For example, say in principle, with decompressor, replace in condenser-reboiler and can be used for generating.

Fig. 3 has shown such flow process.In this flow process, identical in absorption-separating component and Fig. 1.Difference is that the vapor stream in this process (501) directly takes out the top of described generator (34), and at decompressor (70), expands.The merit that obtains from decompressor (70) can be mechanically connected to a generator (72) generating from decompressor (70).Then consequent low-pressure steam (502) is delivered to absorber (31), for further use.From generator out steam flow (501) can be sent to decompressor (70) before further the heating.This is unshowned in Fig. 3.

This heat pump may have following assembly: condenser, subcooler, pressure-reducing valve, evaporimeter, and in parallel decompressor and transfer valve with it, so that system can be used as the heat pump that a kind of heat drives when needing heating or when cooling, when not needing to heat and when cooling, can be used as an electricity generation system, use as heat pump and electricity generation system even simultaneously.

The following examples provide and make those skilled in the art can implement the present invention, are used for illustrating of the present invention.Example used should not be understood to defined scope in the claims of the present invention is produced restriction.

Example:

Simulation with NMP as solvent and the R134a-DME system of following Fig. 1 as mixed working fluid, for heating and cooling.It the results are shown in table 1.

In table 1, subscript b represents absorber cooler, and c is the generator condenser, and e is evaporimeter, and g is the generator heater.Note 3 blocks of column plates of (comprise bottom) of heat load distribution in feed tray and stripping section of generator, so most heat absorption occurs at the following temperature of Tg.Provide if heat is the form with sensible heat, this point is very important.Wherein the value of CCOP and HCOP is the COP value of heat energy: CCOP=Load Evaporator/reboiler load, HCOP=(condenser duty+absorbent cooler load)/the reboiler load.

Table 1. absorber cooler, condenser, evaporimeter, and the reboiler of generator, pressure, working medium forms, and the temperature of CCOP and HCOP value

The composition of the weak absorbent of four cases of table 2. and strong absorbent

Other condition used in simulation is as follows: generator has 6 theoretical stages (2 grades of rectifying sections, 4 grades of stripping sections, be included in feed zone), and absorber only has one-level (being that it is a blender).Research afterwards shows, when from evaporimeter working medium out, allowing to contain the liquid of a few percent, the progression of generator can reduce to 3 to 4 and affect indistinctively the performance of system.This a small amount of liquid is evaporation fully basically in the subcooler of adverse current basically.The value of pump merit (supposition the efficiency of pump 60%, electric efficiency 95%) be respectively generator reboiler load 0.8%, 2.1%, 1.4% and 2.3%.

The strong absorption of four kinds of situations and the composition of weak absorption are shown in table 2.

Can find out, when evaporator temperature is 40.4 °F (4.7 ℃), approximately 81 °F of condenser and absorber cooler temperature (27 degree Celsius), while being used for heating when generator reboiler temperature is 188 ℃ (87 ℃), the HCOP value can reach 1.90, when environment temperature is low, for example when the temperature of evaporimeter was 17 degree (8 ℃), HCOP diminished, and the temperature of the reboiler of generator is brought up to 226.5 °F (108 ℃).When the machine is used for coolingly, if the temperature of evaporimeter is 57.7 °F (14.3 ℃), the chiller temperature of condenser and absorber is at 98 °F (37 ℃), as the reboiler of generator, is 170 °F (76.7 ℃), and CCOP is 0.83; If the reboiler of generator is that CCOP is 0.78 at 160 °F (71 ℃).

Rear two kinds of situations show, such refrigeration machine can use the hot water of flat-plate solar collector cheaply to drive, this moment, this system still can obtain the CCOP value more much bigger than the typical 0.6-0.75CCOP value of lithium-bromide absorption-type refrigerating machine, and is also much bigger than the ammonia water absorbing heat pump of the driving of the thermal source with higher temperature.

Those of skill in the art in the art can understand, and the above embodiments can be made the variation that does not break away from its inventive concept widely.Therefore, the present invention is not limited to the specific embodiment of this paper, and is intended to cover the change in the spirit and scope of the present invention that defined by claims.

Claims

1. hot drive system for increasing gaseous working medium pressure, described system comprises working medium, described working medium has under 1 atmospheric pressure the bubble point less than 20 ℃, and solvent, and described solvent is included in its molecule and contains at least one oxygen atom (O), with select free nitrogen (N), sulphur (S), phosphorus (P), at least one atom in the group that fluorine (F) forms, and their combination, and the dew point under 1 atmospheric pressure is at the organic oxygen-containing compound more than 130 ℃.

2. hot drive system as claimed in claim 1 comprises:

Absorber, in described absorber, will be essentially than low pressure working fluid stream, absorbing than forming liquid solution in the absorbent liquid of low pressure stream of gaseous state, and wherein said absorbent comprises solvent and working medium component;

Cooler, described cooler is removed the heat from absorber;

Supercharging device, described supercharging device increases the pressure of the liquid solution of at least a portion, to obtain higher pressure liquid solution; And

Generator, described generator is separated at least one working medium of higher pressure at least stream that basically is evaporated and a higher pressure absorbent liquid stream with the higher pressure solution of at least a portion.

3. according to claim 2 hot drive system further comprises:

Condenser, the higher pressure working medium that described condenser is evaporated at least a portion basically flow condensation basically to obtain the working medium that basically is condensed stream;

Decompressor, described decompressor reduce the working medium flowing pressure that at least a portion is condensed basically, to obtain more low pressure working fluid stream; And

Evaporimeter, described evaporimeter evaporates at least in part at least a portion and flows than low pressure working fluid, to obtain the working medium that is evaporated at least partly stream in the heat removing other thermals source,

Wherein, when hot drive system was used to heat enclosure space or process flow, other thermals source in described evaporimeter were the heats from the environment of process flow or enclosure space; When hot drive system was used to the space of cooling sealing or process flow, wherein other thermals source came self-enclosed space or the heat of process flow.

4. according to claim 3 hot drive system further comprises: heat exchanger, and the working medium stream that described heat exchanger will be condensed basically from least a portion of described condenser is cooling, to obtain cold working medium, flows, and heats simultaneously another stream; Wherein the cold workflow of the mistake of at least a portion is supplied to described pressure regulating equipment to obtain than the workflow of low pressure subsequently, and other streams in heat exchanger comprise that at least a portion carrys out the working medium that is evaporated at least partly stream of flash-pot; The heating of the described working medium stream that is evaporated causes being essentially than low pressure working fluid, flowing of gaseous state, and wherein at least a portion is supplied to described absorber.

5. hot drive system as claimed in claim 3, wherein, described working medium is selected free R134a, dimethyl ether, R152a, CH ₃I(R13I1), propane, isopropyl alkane, propylene, iso-butane, normal butane, the group that HFO1234yf and combination thereof form, and also the viscosity of described solvent in the time of 20 ℃ is lower than 2.5 centipoises.

6. hot drive system as claimed in claim 3, wherein, described solvent is selected from METHYLPYRROLIDONE (NMP), dimethyl sulfoxide (DMSO) (DMSO), dimethyl formamide (DMF), dimethylacetylamide (DMAc) and their combination.

7. the system that drives of the heat for increasing the pressure of gaseous working medium comprises:

Absorber, in described absorber, absorb the working medium than low pressure that is essentially gaseous state than forming liquid solution in low pressure absorbent liquid stream, and wherein, described working medium is selected free R134a, dimethyl ether, R152a, CH ₃I(R13I1), propane, isopropyl alkane, propylene, iso-butane normal butane, HFO1234yf, and the group of their combination composition; And described absorbent comprises and selects free METHYLPYRROLIDONE (NMP), methyl-sulfoxide (DMSO), dimethyl formamide (DMF), dimethylacetylamide (DMAc), and the solvent of the group that forms of their combination and the component of described working medium;

Cooler, described cooler is removed the heat from absorber;

Supercharging device, described supercharging device make the pressure of at least a portion liquid solution increase to obtain higher pressure liquid solution;

Generator, described generator is separated at least one higher pressure working medium stream that basically is evaporated and a higher pressure absorbent liquid stream with higher pressure solution;

Condenser, described condenser flows condensation basically with the higher pressure working medium that at least a portion is evaporated basically;

Heat exchanger, described heat exchanger is cooling with the working medium stream that at least a portion is condensed basically,, with in another stream of heating, has got cold working medium stream;

Decompressor, described decompressor reduce the excessively cold working medium flowing pressure of at least a portion, with acquisition, than low pressure working fluid, flow;

Evaporimeter, described evaporimeter evaporates at least in part at least a portion and flows than low pressure working fluid,, with the working medium stream that obtains to be evaporated at least partly, removes simultaneously the heat of other thermals source, wherein

When hot drive system was used to heat enclosure space or process flow, other thermals source were the heat from the environment in the space of a sealing; When hot drive system was used for the space of cooling sealing or process flow, other thermals source came self-enclosed space or the heat of process flow;

Other streams in heat exchanger comprise the described working medium stream that is evaporated at least partly of at least a portion; The heating of the described working medium stream that is evaporated causes being essentially than low pressure working fluid, flowing of gaseous state, and at least a portion wherein is supplied to absorber;

The second heat exchanger, described the second heat exchanger are used for cooling at least a portion higher pressure absorbent liquid stream, thereby obtain supercooled liquid absorbent liquid stream; And

The second dropping equipment, described the second dropping equipment make at least a portion cross the pressure decreased of cold absorbent liquid stream, obtain than low pressure absorbent liquid stream, and wherein the described low pressure absorbent liquid of at least a portion stream is supplied to absorber.

8. the system that drives of according to claim 7 heat, wherein, described the second cools down comes from least a portion higher pressure absorbent liquid stream of generator bottom and receives agent liquid stream must be enfleurage, heating simultaneously and part evaporation come from least a portion higher pressure liquid flux of supercharging device to obtain the higher pressure two phase flow, and it is supplied to the centre position of described generator subsequently.

9. the system that drives of according to claim 1 heat, comprise more than one generator.

10. electrical power generation system, comprise hot drive system as claimed in claim 2 and expander, wherein, basically the higher pressure working medium stream that is evaporated from least a portion of described generator expands and produces mechanical energy in decompressor, and at least a portion flows and absorbed by the described low pressure absorbent liquid in described absorber from the working medium waste stream of described decompressor.

11. technique that the heat for increasing the pressure of gaseous working medium drives, described technique comprises uses working medium and solvent, described working medium its bubble point under 1 atmospheric pressure is less than 20 ℃, described solvent comprises that its molecule contains at least one oxygen atom (O), and choosing freely contains nitrogen (N), sulphur (S), phosphorus (P), at least a atom in the group that fluorine (F) forms, and their combination, and the dew point under 1 atmospheric pressure is at the organic oxygen-containing compound more than 130 ℃.

12. described heat drives technique according to claim 11, comprising:

To be than low pressure working fluid stream, absorbing than obtaining liquid solution, the component of wherein said absorbent solvent and working medium in low pressure absorbent liquid stream of gaseous state basically in absorber;

Remove the heat from absorber;

Increase the pressure of at least a portion liquid solution to obtain higher pressure liquid solution;

Described higher pressure solution is separated to obtain at least one higher pressure working medium stream that basically is evaporated and a higher pressure absorbent liquid stream in generator.

13. heat according to claim 12 drives technique, further comprises:

Basically the higher pressure working medium stream that condensation at least a portion is evaporated basically in condenser, the working medium that obtains basically being condensed stream;

Reduce basically the be condensed pressure of working medium stream of described at least a portion, flow than low pressure working fluid obtaining; And

Evaporation at least a portion flows than low pressure working fluid in evaporimeter,, with the working medium stream that obtains to be evaporated at least partly, removes simultaneously the heat from another thermal source,

Wherein, when hot drive system was used for heating enclosure space or process flow, other thermals source in evaporation step were the heat from the environment of enclosure space or process flow; When hot drive system was used for cooling enclosed spaces or process flow, wherein other thermals source came self-enclosed space or the heat of process flow.

14. described heat drives technique according to claim 13, further comprises:

The working medium stream that cooling at least a portion is condensed basically in heat exchanger,, to obtain cold working medium stream, heat another stream simultaneously; Wherein the stream of other in heat exchanger comprises the working medium stream that at least a portion from described evaporimeter is evaporated; The heating of the described working medium stream that is evaporated causes being essentially than low pressure working fluid, flowing of gaseous state;

Be supplied to described absorber with what at least a portion was essentially gaseous state than low pressure working fluid stream;

Be reduced by at least a part and cross the pressure of cold working medium stream, with acquisition, than the working medium of low pressure, flow.

15. the heat for increasing gaseous working medium pressure drives technique, comprising:

To be than low pressure working fluid stream, absorbing than obtaining liquid solution in low pressure absorbent liquid stream of gas basically in absorber.Wherein said working medium is selected free R134a, dimethyl ether, R152a, CH ₃I(R13I1), propane, isopropyl alkane, propylene, iso-butane, normal butane, HFO1234yf, and the group of their combination composition; And described absorbent comprises the component of working medium and selects free METHYLPYRROLIDONE (NMP), dimethyl sulfoxide (DMSO) (DMSO), dimethyl formamide (DMF), dimethylacetylamide (DMAc), and the solvent of the group that forms of their combination;

Remove the heat from absorber;

Increase the pressure of at least a portion liquid solution by supercharging device to obtain higher pressure liquid solution;

In generator, described higher pressure solution is separated, to obtain at least one higher pressure working medium stream that basically is evaporated and a higher pressure absorbent liquid stream;

The working medium stream that cooling at least a portion is condensed basically in heat exchanger,, to obtain cold working medium stream, heat another stream simultaneously;

Be reduced by at least the pressure of the excessively cold working medium stream of a part, with acquisition, than low pressure working fluid, flow;

Evaporation at least a portion flows than low pressure working fluid in evaporimeter, and the working medium stream to obtain to be evaporated at least partly, remove and reduce phlegm and internal heat from another thermal source simultaneously, wherein:

When hot drive system was used for heating enclosure space or process flow, other thermals source were the heat from the environment of enclosure space or process flow; When hot drive system was used for cooling enclosed spaces or process flow, wherein other thermals source were the heat from enclosure space or process flow; And

Other streams in heat exchanger comprise coming the working medium that is evaporated at least partly stream of flash-pot, and the heating of the described working medium stream that is evaporated causes being essentially than low pressure working fluid, flowing of gaseous state;

With at least partly described be essentially gaseous state be supplied to described absorber than low pressure working fluid stream;

Cooling at least a portion higher pressure absorbent liquid stream in the second heat exchanger, to obtain an overcooled absorbent liquid stream;

The pressure that reduction at least a portion is crossed cold absorbent liquid stream flows than the low pressure absorbent liquid with acquisition; And

At least a portion is supplied to described absorber than low pressure absorbent liquid stream.

16. described heat drives technique according to claim 15, wherein, the second cools down is from least a portion higher pressure absorbent liquid stream of generator bottom, to obtain overcooled absorbent liquid stream, heating simultaneously and part evaporation are from least a portion higher pressure liquid solution of institute's supercharging device,, to obtain the higher pressure two phase flow, subsequently at least a portion higher pressure two phase flow is supplied to the centre position of generator.

17. described heat drives technique according to claim 16, wherein, be heated and the higher pressure liquid solution that is evaporated of part accounts for the 80-99%(mole of higher pressure liquid solution), and be not heated and 1-20%(mole that part is evaporated) higher pressure liquid solution be supplied to the top of generator.

18. described technique according to claim 17, wherein, the higher pressure working medium stream that basically is evaporated that obtains from described generator contains up to 5%(mole) solvent, and the described working medium stream that is evaporated at least partly that acquires from condenser contains 0.1-5%(mole) liquid.

19. the technique that drives of described heat according to claim 11, wherein separating step utilizes more than one generator.

20. an electricity generation system comprises:

A) heat as claimed in claim 12 drives technique,

B) the higher pressure working medium stream that in decompressor, at least a portion is evaporated basically expands to produce mechanical energy, and

C) the working medium waste stream of at least a portion of the machine of self-expanding in the future absorbs than in low pressure absorbent liquid stream in absorber.