MX2008009087A - High efficiency absorption heat pump and methods of use - Google Patents

Abstract

An energy conversion system including a high efficiency absorption heat pump cycle is disclosed using a high pressure stage, a supercritical cooling stage, and a mechanical energy extraction stage to provide a non-toxic combined heat, cooling, and energy system. Using the preferred carbon dioxide gas with partially miscible absorber fluids, including the preferred ionic liquids as the working fluid in the system, the present invention desorbs the CO.sub.2 from an absorbent and cools the gas in the supercritical state to deliver heat. The cooled CO.sub.2 gas is then expanded, preferably through an expansion device transforming the expansion energy into mechanical energy thereby providing cooling, heating temperature lift and electrical energy, and is returned to an absorber for further cycling. Strategic use of heat exchangers, preferably microchannel heat exchangers comprised of nanoscale powders and thermal-hydraulic compressor / pump can further increase the efficiency and performance of the system.

Description

HEAT PUMP OF HIGH EFFICIENCY ABSORPTION AND METHODS OF USE FIELD OF THE INVENTION The invention is generally directed to heat pumps, and more specifically to a high pressure absorption heat pump using carbon dioxide and a low vapor pressure absorber as the circulating fluid. BACKGROUND OF THE INVENTION Heat pumps are well known in the art. A heat pump is simply a device for supplying heat or cooling to a system, while a cooler is a device for removing heat from a system. Thus, a refrigerator can be considered a type of heat pump. Throughout the application, the invention will be referred to as a heat pump with the understanding that the designation of refrigerator, air conditioner, water heater, cogeneration system (also referred to as CHP system or combined heat and power system) , which is the use of a heat engine or a power station to simultaneously generate electricity and useful heat), and trigeneration system (a cogeneration system that additionally produces cooling) could be replaced without changing the operation of the device. The inherent characteristic of a heat pump is to transport / move thermal energy from a heat source to a heat sink. The use of the term heat pump, therefore, is widely applied as the transport of thermal energy from one enthalpy / entropy state to another. Thus, the use of heat pumps is not restricted to the generation of heating or cooling, but also to the intrinsic movement of thermal energy in virtually any thermodynamic cycle that includes means to convert such thermal energy into power generation (e.g., electric power). or mechanical). In absorption heat pumps, an absorber such as water absorbs the refrigerant, typically ammonia, thus generating heat. When the combined solution, also referred to as a binary solution, is pressurized and further heated, the refrigerant is expelled. When the refrigerant is pre-cooled and expanded at a low pressure, it provides cooling. The low pressure refrigerant is then combined with the low pressure depleted solution to complete the cycle. Many current absorption heat pumps / refrigerators make use of either a water-ammonia couple, or a lithium-water bromide couple. These two absorption partners suffer from certain disadvantages. The water-ammonia pair increases the safety problems in view of the toxicity and flammability of the ammonia, and that the LiBr is corrosive and very prone to failures due to the operation at low pressure, that is, small leaks create contamination. In addition, the tendency to crystallize can be a problem of obstruction. Operating at very low pressures is often impossible due to water freezing. Other absorption processes have been proposed, but generally involve working fluids that are toxic, flammable, deplete ozone, or have high atmospheric greenhouse effect. US Patent No. 6,374,630 for "Carbon dioxide absorption heat pump" for Jones describes a traditional absorption cycle utilizing supercritical carbon dioxide. The '630 patent does not anticipate an absorber having either a very low vapor pressure, a boiling point of less than 50 ° C, or any means to achieve a coefficient of performance better than 0.70. The '630 patent also does not anticipate any non-thermal means to reduce the desorption temperature, nor the extraction of the expansion energy. It is understood that the term carbon dioxide and the abbreviations for carbon dioxide used are interchangeable including C02 and C02. Also, the term water and the abbreviations for water used are interchangeable that include H20 and H20.

U.S. Patent Application No. US 2003/0182946 for "Method and apparatus for using magnetic fields for enhancing heat pump and refrigeration equipment performance" for Sami et al., it uses a magnetic field that is operable to destabilize the intermolecular forces and weakens the intermolecular attraction to improve the expansion of the working fluid to the vapor phase. It has been found that the energy of the magnetic field alters the polarity of the refrigerant molecules and destabilizes the dispersive forces of intermolecular Van der aals between the refrigerant molecules, although Sami et al. it does not anticipate the use of a magnetic field to reduce the desorption energy. U.S. Patent No. 6,434,955 for "Electro-adsorption chiller: a miniaturized cooling cycle with applications from microelectronics to conventional air-conditioning" for Ng et al., Presents the combination of absorption and thermoelectric cooling devices. The governing physical processes are primarily the surface rather than the mass effects, or they involve the electron instead of the fluid flow. The '955 patent does not anticipate a continuous absorption process, but rather the thermal energy transfer of a batch desorption process in the sequentially processed batch for subsequent desorption.

U.S. Patent Application No. US 2003/0221438 for "Energy efficient sorption processes and systems" for Rane, et al. idea of adsorption modules with heat transfer passages in thermal contact with the wall of the adsorption module and the switchable heat pipes. The adsorption module of this invention leads to lower cycle times as low as 5 minutes that produce a multi-stage efficient regeneration process for regenerating the liquid desiccant using rotating contact disks. The '438 patent does not anticipate either a continuous process or an absorption process. U.S. Patent Application No. US 2002/0078696 for "Hybrid heat pump" and U.S. Patent No. 6,539,728 for "Hybrid heat pump", both for Korin, describe a hybrid heat pump system that includes (i) a membrane permeator having a permselective membrane capable of selectively removing vapor from a gas containing steam to produce a dry gas, and (ii) a heat pump having (a) an internal side for exchanging thermal energy with a process fluid, (b) an external side for exchanging thermal energy with an external environment, and (c) a thermodynamic mechanism for pumping thermal energy between the inner side and the outer side in any direction. Korin uses membranes to pre-condition the air in conjunction with a cooling air conditioning system, and does not perform or anticipate any phase separation within the refrigerant itself. In addition, although the membranes have been used in various separation applications, their use for heat pump systems has been limited. U.S. Patent Nos. 4,152,901 and 5,873,260 propose improving an absorption heat pump by using a semipermeable membrane and a pervaporation membrane, respectively. US Patent No. 4,467,621 proposes to improve vacuum cooling using the porous sintered metal membrane, and US Patent No. 5,946,931 discloses an evaporative cooling apparatus using a microporous PTFE membrane. These patents do not anticipate the use of membranes for phase separation within an absorption system, but rather within the adsorption systems. US Patent No. 4,152,901 to Munters discloses a method and apparatus for transferring energy in an absorption heating and cooling system where the absorbent is separated from the working medium by diffusing the mixture under pressure through a semipermeable membrane defining an area of relatively high pressure and a relatively low pressure zone, greater than the ambient pressure. The '901 patent does not anticipate the supercritical operation, since it explicitly states that the "dilute solution of the working medium is passed to the evaporator upon being depressurized, while the concentrated solution of the absorbent, when reduced to the ambient pressure, is passed to the sorbeión station ". U.S. Patent No. 5,873,260 for "Refrigeration apparatus and method" for Linhardt, et al. it uses the increased pressure of the absorbent / coolant solution which is then supplied to a pervaporation membrane separator to provide as one output stream a vapor rich refrigerant, and as another output stream a concentrated liquid absorbent. The '260 patent does not anticipate supercritical fluids since it explicitly stated that "the pressure of the refrigerant inlet substantially vaporized to the absorber is less than 3.515 kg / cm2 (50 psia)" and "the pressure of the incoming absorbent / coolant solution. The membrane separator is within the range of approximately 17,575 to 28.12 kg / cm2 (250 to 400 psia). " The '260 patent further notes that "the osmotic membrane absorption reflectance cycles are also capable of reaching low temperatures and may have a higher COP than conventional ammonia / water heat separation systems., but they require very high pressures, in the order of 140.6 kg / cm2 (2,000 psia) or more to force the coolant through the pores of the osmotic membrane. "It should be noted that a pervaporation membrane operates in a completely different manner from the Membrane separation processes of the prior art used in refrigeration and heat pump systems Such prior art membrane systems rely on osmotic pressure to force the refrigerant through the membrane, thus separating the refrigerant from other components. The ammonia-water pair, this conventionally requires pressures of the order of magnitude of 140.6 to 281.2 kg / cm2 (2,000 to 4,000 PSI) and higher.The osmotic membranes are porous which allows the ammonia to pass through the membrane. pervaporation are not porous, but pass components through the membrane by dissolving the selected material in the membrane.This allows a very strong driving force. or less, significantly less than 28.12 kg / cm2 (400 PSI), act as the driver. In the case of an ammonia-water mixture, the pervaporation membrane selectively passes the water vapor and ammonia and rejects the liquid water. US Patent No. 6,739,142 for "Membrane desiccation heat pump" for Korin describes a system that includes a membrane permeator for removing steam from a process gas and for providing a steam-depleted process. This patent does not disclose the use of any supercritical fluid. US Patent No. 6,918,254 for "Superheater capillary two-phase thermodynamic power conversion cycle system" for Baker describes a two-phase thermodynamic power system that includes a capillary device, steam accumulator, superheater, in-line turbine, condenser, a liquid pump and a liquid preheater to generate output power as a generator through the generation of a stepped or pulsed release of steam flow. The capillary device, such as a heat circuit tube or a capillary pumped circuit, is coupled to a steam accumulator, superheater, the in-line turbine to generate power output for power generation, liquid pump and liquid preheater . The capillary device receives input heat that is used to change the phase of the liquid received from the liquid preheater, liquid pump and condenser to steam for extra heating in the superheater used to then drive the turbine. A superheater in combination with a liquid pump and preheater are implemented for use with the evaporator for improved thermal efficiency by operating at maximum cycle temperatures well below other available power conversion cycles. The '254 patent requires a capillary device that includes heat circuit tubes and pumped circuitry to increase the single pressure of the operating fluid (ie, to achieve the pressure differential that results from the gain in thermal energy) instead of the traditional use of a compressor to increase the pressure within a thermodynamic power conversion cycle. In addition, the '254 patent uses the superheater stage to eliminate any liquid droplets to avoid the collision of the liquid inside the turbine blades. The '254 patent is also a low pressure device that has low pressure differentials between the high pressure stage and the low pressure stage as specifically noted by its reference to hair wicks with approximately one pore size (commercially available). ) that can withstand a pressure differential of approximately ten psi. In conclusion, the '254 patent does not allow the use of working fluids including fluids characterized as binary composition, supercritical and / or non-toxic fluids. The '254 patent is dependent on the use of a capillary device as a means to achieve a pressure differential. U.S. Patent No. 5, 899,067 for "Hydraulic engine powered by introduction and removal of heat from a working fluid" for Hageman describes a thermal source as a means to increase the pressure of a working fluid which in turn drives a piston for pumping, or alternatively refers to the piston being connected to a generator to result in electricity. The '067 patent is dependent in its operation on the sequential heating and cooling of a fluid to enable the pressure in the piston to be increased by heating and subsequently to decrease by cooling to enable the recovery of fully expanded potions to fully compressed The '067 patent is a low pressure device, uses a single operating fluid, and is comprised of a piston in motion, has relatively little surface, the entire area resulting in slow power conversion rates and large physical size. "Poly (ionic liquid) s as New Materials for C02 Absorption" by Youqing Shen et al. Department of Chemical and Petroleum Engineering, University of Wyoming, Laramie, yoming 82071, USA, received for publication on February 9, 2005, identifies that simply converting ionic liquids to polymeric forms significantly increases the sorption capacity of C02 compared to liquids ionic Shen et al. Further notes that especially ionic liquid polymers based on tetraalkylammonium have C02 sorption capacities 6.0-7.6 times those of ionic liquids at room temperature. The sorption and desorption of C02 of the polymer solids are very fast, and the desorption is completely reversible. Shen et al. , then specifically note the use of such polymers as being "very potential as membrane materials and sorbent for the separation of C02". Exemplary poly-ionic liquid (s), as noted by Shen et al., Are comprised of PF6 anions of ionic liquids that have the highest sorption capacity of C02. More specifically, poly-ionic liquids include 1- [2- (Methylacryloyloxy) ethyl] -3-butyl-imidazolium tetrafluoroborate ([MABI] [BF4]) and l- (p-vinylbenzyl) -3-butyl tetrafluoroborate. imidazolium ([VBBI] [BF4], poly [1- (4-vinylbenzyl) -3-butylimidazolium] tetrafluoroborate] (PVBIT), poly [(1- (4-vinylbenzyl) -3-butylimidazolium] hexafluorophosphate] (PVBIH), and poly [2- (l-butylimidazolium-3-yl) ethyl methacrylate tetrafluoroborate] (PBIMT) The specific results that prove the particle size gave the conclusion that the absorption capacity of C02 is mainly dependent on the chemical structure of the particles. poly-ionic liquids, while the rate of absorption of C02 is dependent on the particle size, Shen et al., clearly by the polymer being stationary as either a sorbent or membrane materials, does not anticipate the use of polyester liquids. ionic as being the heat transfer fluid or the fluid of work within a thermodynamic cycle. The prior art lacks high efficiency, a system with an operating coefficient greater than 0.7, an efficient and environmentally friendly absorption cycle that uses a non-toxic, non-corrosive working fluid with a positive working pressure. BRIEF DESCRIPTION OF THE INVENTION A process of generating cooling, heating and absorbent, safe, environmentally friendly energy is provided. The process uses a carbon dioxide absorption cycle that uses a liquid, non-toxic absorbent such as ionic liquids, from which the carbon dioxide gas is absorbed. Only the carbon dioxide refrigerant is circulated to the heat exchangers of the condenser and evaporator, the components directly in contact with breathing air, thus avoiding a series of disadvantages associated with the absorber. The additional incorporation of a thermodynamic hydraulic pump increases the energy efficiency, especially in the combustion power generation cycles, since it eliminates a substantial portion of energy used for compression before combustion. An aspect of the invention is to integrate an absorption heat pump with integral power extraction capabilities to a standard steam compression heat pump as a means to increase the total power conversion and the cooling performance coefficient. The figures depicted within the specification of the invention provide exemplary configurations of the most important components of the energy conversion system. A detailed description of the figures is provided in the following paragraphs. BRIEF DESCRIPTION OF THE DRAWINGS Figure 1 is a flow chart view of the absorption heat pump depicted with an expansion turbine configuration as the mechanical energy extraction device. Figure 2 is a flow chart view of the absorption heat pump depicted with an expansion turbine configuration as the mechanical energy extraction device that drives a vapor compression pump (i.e., a compressor). Figure 3 is a flow chart view of the absorption heat pump shown with a magnetic cooling heat pump configuration as the non-thermal means for increasing the temperature of the concentrated solution. Figure 4 is a flow chart view of the absorption heat pump depicted with a sealed containment of an expansion turbine configuration. Figure 5 is a flow chart view of the absorption heat pump depicted with a concentrated solution of pre-heating of the condenser of the multi-stage thermal pump system. Figure 6 is a three-dimensional view of the heat pof absorption represented with a preheating of the concentrated solution through the containment of the combustion chamber and the recuperator. Figure 7 is a cross-sectional view of the absorption heat prepresented with the thermal energy of the desorption of the concentrated solution obtained by an integral heat exchanger of microchannels inside the solar collector. Figure 8 is a flowchart view of an absorption heat prepresented in a Goswami cycle. Figure 9A and Figure 9B are views of the flow diagram of a thermodynamic hydraulic p Figure 10 is a flowchart view of the non-thermal nanofiltration membrane to desorb the refrigerant from the concentrated solution. Figures 11A, 11B, 11C, and 11D are views of the flow diagram of multiple configurations of two-stage absorption heat pump systems. Figure 12 is a flow chart view of the multi-use refrigerant desorbed from an absorption heat pump system. Figure 13 is a flow chart view of the refrigerant and / or weak multi-use solution for cleaning the combustion by-products. Figure 14 is a flow chart view of an absorption heat pump system as an integral component of a biomass to biofuel conversion process. Figure 15 is a flow chart view of an integrated liquid desiccant and combustion system. Figure 16 is a flow chart view of a membrane filtration system with pressure equilibrium across the membrane. Figure 17 is a flow chart view of an integrated combustion system having independent control of a compressor and energy extraction device. Figure 18 is a flow chart view of an improved cavitation absorption heat pump and improved biomass to biofuel conversion process.

Figure 19 is a flowchart view of an absorption / heat pump that uses waste heat from the lower cycle to energize the compressor. Figure 20 is a flow diagram view of a thermal bus switching circuit. Figure 21 is a flow chart view of a thermal bus and a range of thermal sources. Figure 22 is a flow chart view of a thermal bus and a range of heat sinks. DETAILED DESCRIPTION OF THE PREFERRED MODALITIES The inventive high efficiency absorption heat pump device, hereinafter also referred to as "ScHPX", is now established as a device mainly comprised of a supercritical absorption heat pump, low pressure absorbers of steam and a series of integral components to achieve desorption using non-thermal means. The term "thermodynamic cycle" is defined as a process in which a working fluid undergoes a series of state changes and finally returns to its initial state.

The term "solar energy" is defined as the energy derived from the sun, which most often refers to the direct conversion of photons radiated into electrons or phonons through a variety of ways. Solar energy is also indirectly converted into additional forms of energy such as warming water from the earth (also known as geothermal water). The term "geothermal" is defined as being related to the internal heat of the earth, which is affected by the solar energy absorbed. The term "ionic liquids" "ILs" is defined as liquids that are non-coordinating, highly solvent media in which a variety of organic and inorganic solutes are capable of dissolving. They are effective solvents for a variety of compounds, and their lack of measurable vapor pressure makes them a desirable substitute for Volatile Organic Compounds (VOCs). Ionic liquids are attractive solvents since they are non-volatile, non-flammable, have a high thermal stability, and are relatively inexpensive to manufacture. The key point about ionic liquids is that they are liquid salts, which means that they consist of a salt that exists in the liquid phase and that has to be manufactured; they are not simply salts dissolved in liquid. Usually one or both of the ions are particularly large and the cation has a low degree of symmetry. These factors result in ionic liquids that have reduced reticule energy and therefore lower melting points. The term "electride" is defined as being similar to alkalines except that it is assumed that the anion is simply an electron that is localized to a region of the crystal between the complexing cations. The term "alkaline" is defined as a class of ionic compounds where the anions are from the (alkaline) elements of the Type I Na, K, Rb, Cs group (no lithium is known). The cation is an alkaline cation that is complexed by a large organic complexing agent. The resulting chemical form is A + [Complex former] B-, where the complex former is either a Cryptand, Crown Ether or Aza-Crown. The term "nanofluid" is defined as a fluid containing nanoscale powders, which are powders having a diameter of less than about 1 miter and preferably less than about 100 nanometers. The term "supercritical" is defined as the point at which fluids have been exploited above their critical pressures and temperatures. The term heat pump is defined as the transport of thermal energy extracted from a heat source to a heat sink by means including absorption, adsorption and vapor compression. The term "cyclic compound" is a compound in which a series of carbon atoms are connected together to form a loop or ring. Benzene is a well-known example. The term "polycyclic" is used when more than one ring are combined in a single molecule, and the term "macrocycle" is used for a ring that contains more than a dozen atoms. The term "electron acceptor" is a compound that receives or accepts an electron during cellular respiration. The process begins with the transfer of an electron from an electron donor. During this process (electron transport chain) the electron acceptor is reduced and the electron donor is oxidized. Examples of acceptors include oxygen, nitrate, iron (III), manganese (IV), sulfate, carbon dioxide, or in some cases chlorinated solvents such as tetrachloroethene (PCE), trichloroethene (TCE), dichloroethene (DCE), and vinyl chloride (VC). The term "absorption" is widely accepted in the application of heat pumps for cooling. Absorption, in chemistry, is a physical or chemical phenomenon or a process in which atoms, molecules, or ions enter some material in volume of solid, liquid or gaseous phase. This is a different process of adsorption, because the molecules are occupied by the volume, not by the surface. A more general term is the sorption that covers adsorption, absorption, and ion exchange. The term "stoichiometric combustion" is the ideal combustion process during which a fuel is completely burned. A complete combustion is a process that burns all the carbon (C) to (C02), all the hydrogen (H) to (H20) and all the sulfur (S) to (S02). If there are unburned components in the exhaust gas such as C, H2, CO, the combustion process is incomplete. The term "excess gas" is defined as the amount of gas in excess of the stoichiometric amount. The term "process intensification reactor" is defined as the miniaturization of the chambers in which the chemical reactions take place. The use of micromixing, particularly with supercritical fluids, achieves a high mass transfer and fast reaction times. Supercritical fluids include gases such as carbon dioxide, methane, methanol, ammonia, ethanol, butanol, and hydrogen. Supercritical fluids can be pred in emulsions, which are preferably nanoemulsions as a means to significantly increase the surface area. The devices include hydrodynamic cavitation devices, microchannel reactors, rotating disk reactor, tube rotary tube, oscillating flow reactors, and reactive distillation reactors. The ScHPX, an extension of the Champagne Heat Pump as developed by Jones, establishes new methods to lower the desorption temperature and total energy requirements to achieve desorption. The refrigerant, which is the circulating working fluid, is comprised of any environmentally friendly fluid (also known as greenhouse friendly) whereby the fluid expands into a gas within the evaporator. A large variety of refrigerants, specifically those known in the art for absorption heat pumps are compatible with the ScHPX. The preferred refrigerant is selected from the group of ammonia and carbon dioxide. The most preferred refrigerant is carbon dioxide, which has reduced toxicity and recognized safety. The specifically preferred coolant operates within the supercritical or transcritical range, as determined by the specific refrigerant. The inventive heat pump also achieves superior desorption through a modified rotary disk reactor "SDR". SDRs have extremely high mass and heat transfer coefficients. The concentrated solution is pumped simultaneously to the center of the disk and forms a thin film while the liquid moves outward. The centrifugal force creates waves of intense interference, which generate high heat transfer between the concentrated solution and the rotating disk. SDR can also be used through intense local mixing to accelerate the absorption of supercritical C02 in the weak solution. The ScHPX is additionally comprised of an absorber in which the refrigerant is absorbed as a method to either increase the temperature rise (ie, transforming a relatively low temperature fluid at a higher temperature (also known as superior quality) from a thermal source, or providing cooling. The energy requirements of an absorption system are traditionally limited to a thermal source for desorption, and mechanical or electrical energy for pumping / pressurizing the concentrated solution. The term "energy efficiency" is the energy output divided by the energy input required to produce the desired output. A high efficiency absorption system, which is characterized in terms of the "COP" operating coefficient, requires methods to reduce mainly the desorption energy requirements. Desorption is effectively the process in which the refrigerant is separated from the absorber. The inventive ScHPX utilizes a range of absorbers that includes at least one absorber selected from the group consisting of ionic liquids, ionic solids, electride solutions, and alkaline solutions. Ionic solids and liquids are recognized in the art of environmentally friendly solvents. The solutions of electrons and alkalis are recognized in the art of chemical reduction methods and oxidation methods respectively. The ScHPX exceptionally presents "IL" ionic liquids, which have very low if not negligible vapor pressure, preferably ionic liquids compatible with the supercritical carbon dioxide "scC02". The inventive combination of scC02 and ILs have excellent carbon dioxide solubility and simple phase separation due to their classification as combinations of partially miscible fluids. The partially miscible fluids are both; miscible and immiscible as a direct function of both; pressure and temperature. A partially miscible fluid in its immiscible state can be simply decanted for phase separation, which is inherently a low energy separation method. The behavior of the C02 phase with the ionic liquids and how the solubility of the gas in the liquid is influenced by the choice and structure of the cation and the anion. The preferred embodiment of the working fluid is an "emulsion" of polyionic liquid and ionic liquid having the combined benefits of the fluid flow of the ionic liquid monomers and the improved absorption / desorption properties of the poly-ionic liquid polymers. , also referred to as ionic polymers. The standard categorization of ionic liquid "emulsions" is characterization as one phase of the emulsion as an "ionic liquid monomer" or abbreviated as "ILM" phase and the other phase being an "ionic liquid polymer" or abbreviated as "ILP" phase. The ILM and ILP phases are also described as a slurry of ionic liquid, hereinafter referred to as "ILS". A preferred ILS is comprised of at least one ionic liquid monomer and at least one ionic liquid polymer. The preferred ILS is comprised of an ILP having a particle size approximately between about 0.1 nanometers and about 500 microns. Particularly preferred ILS is comprised of an ILP having a particle size of between about 10 nanometers and about 5 microns. And the specifically preferred ILS is comprised of an ILP having a particle size approximately between about 0.1 nanometers and about 500 nanometers. The prior art that uses nanoscale powders has identified 100 nanometers, without being limited by theory, as a threshold of significant size that has a quantum effect on heat transfer. Dimensioning nanoscale dust is a highly nonlinear process in which 50 nanometer particles have superior results compared to 100 nanometers. And likewise, 30, 20, and 10 nanometers are each superior to the respective larger size. Another significant threshold is 10 nanometers, again without being limited by theory, as a size threshold where dust sizes of less than 10 nanometers have heat transfer performance benefits that are not realized by the powder sizes by over 10 nanometers. The average free path of phonons is accepted as being less than 10 nanometers. Most noted is the inclusion of binary working fluids having at least one fluid selected from at least one group of ionic liquid, ionic liquid polymer, electride, alkali, and nanofluid solutions. Particularly preferred working fluids have at least one fluid selected from the group consisting of ionic liquids, combination of ionic poly-liquid polymers and ionic liquids. The specifically preferred working fluid is comprised of a heat transfer fluid comprised of at least one ionic liquid and at least one polymer of polyionic liquid). The further inclusion of nanoscale powders that include conductive powders, semiconductor powders, or combinations thereof increases the thermal conductivity of the working fluid. The use of a polymer of polyionic liquid and at least one additional working fluid selected from the group consisting of ionic liquids, solid non-polymeric adsorbents, and combinations thereof, maintains the ability of the working fluid to be pumped and circulated through heat exchangers for increased heat transfer while demonstrating superior absorption and desorption rates of refrigerant. A specifically preferred ionic liquid or ionic polymer is itself magnetic having distinct advantages including higher rates of absorption and desorption when subjected to / removes from magnetic fields, and the ability to isolate said coolant materials more easily by non-thermal means. The additional additive of at least one nonionic compound selected from the group consisting of cyclic, polycyclic, and macrocycle compounds, and combinations thereof including antioxidants, polyphenols, lignans, and vitamins, provides the working fluid with operative life and stability. improved thermal, and without being limited by the theory of electron transfer and improved heat transfer. Mediators of electron transfer include polycationic protein, complexes with tialoto bridges, thiolated complexes, metalloproteins, protein complexes that have an iron-sulfur grouping, trehalose complexes, iron-sulfur grouping, sodium-ammonia, sulfur-ammonia, a chitosan complex including chitosan lactate, chitosan alpha lipoic acid, or thiolated chitosan, or combinations thereof. Additional additives that impact electron transfer include iron salts, iron salt derivatives, potassium salts, lactic acid salts, potassium salt derivatives, lactic acid salt derivatives, phytic acid, gallic acid, and combinations thereof. Absorption heat pumps including energy conversion are particularly preferred when they are further comprised of at least one additive selected from the group consisting of electron transfer mediator, electron donor, electron acceptor, ultraviolet light absorber, infrared absorber , quantum dot, nanoscale dust, and combinations thereof. The use of nanoscale powders improves heat transfer and electrical conductivity by quantum means, without being limited by theory. The addition of additives, preferably in the nanoscale range, has an impact on the conversion of photons for phonons, photons to electrons, electrons to phonons, phonons to electrons, etc. The particularly preferred application of the heat transfer fluid is operable within thermal energy conversion devices that include devices selected from the group consisting of flat solar panels, thermal, solar thermal concentrator receivers, thermionic emission cells, thermovoltaic cells, generator electricity, compressor, and heat pump. And the specifically preferred application is by means of which the fluid and at least one absorbed gas (preferably C02) operable with the transcritical or supercritical region in the solution by means of which the subsequently desorbed gas is used within a thermodynamic cycle which includes selected cycles of the group consisting of Goswami, Uehara, Kalina, Rankine, Carnot, Joule-Brayton, Ericsson, and Stirling. Additional combinations of refrigerants and absorbers are recognized in the art as having partial miscibility. A further aspect of the inventions is the achievement of phase separation as a function of at least one function selected from the group consisting of temperature, pressure, and pH. The preferred solution further includes the use of small amounts of pH to vary the solubility of the refrigerant within the absorber. The most preferred solution varies the temperature and pressure, in combination with pH control using methods that include electrodialysis. An additional method to enable phase separation is the application of electrostatic fields, since electrostatic fields increase the solubility of ionic fluids. The inventive ScHPX also influences the solutions of electrons and alkalis. The preferred electrolyte solution is comprised of ammonia. The main benefit of electrons is centered on the transfer of free electrons (ie, energy state) between the cathode and the anode. An additional benefit, which is important for the subsequent incorporation of powders at the nanoscale, is the strongly reducing characteristic of electride. This is important since nanoscale powders, specifically metals, are easily oxidized due in part to the large surface area of the powder. Still another embodiment of the invention is the additional inclusion of at least one nanoscale powder selected from the group consisting of conductive, semiconductor, ferroelectric, and ferromagnetic powders. Nanoscale powders, as recognized in the art, maintain colloidal dispersions while improving or varying a range of properties including magnetism, thermophysical properties (eg, thermal conductivity), electrical conductivity, and absorption characteristics. The most preferred nanoscale powders are additionally comprised of nanoscale powders having nanoscale surface modifications, including surface modifications selected from the monolayer group, and nanoscale multilayers (i.e., surface coatings of less than 100 nanometers). Specifically preferred nanoscale powders improve more than a parameter selected from the group consisting of thermophysical properties, electrical conductivity, and absorption of the sunlight spectrum. A further feature of the inventive ScHPX is the integration of mechanical energy extraction devices. Mechanical energy extraction devices improve efficiency (i.e., COP) by extracting energy during the expansion step of the refrigerant following the desorption step. Referring to Figure 1, the mechanical energy can be transformed using the desorbed refrigerant desorbed from the desorber 50 through a valve or flow regulator 20 in a variety of useful forms of energy as known in the art, including a turbine 65 of expansion. The ScHPX, depending on the operating conditions, has additional cooling capacity through a heat exchanger 25 before the refrigerant is absorbed in the absorber 30. These forms include transforming the mechanical energy to electrical energy (e.g. of direct or alternating current electricity), or drive pumps, compressors, or motors. These include energy extraction devices selected from the group consisting of gerotor, quasiturbine, piston, spherical motor, expansion turbine, expansion pump, Stirling cycle engine, Ericsson cycle engine, and jet-turbine turbine. The preferred mechanical extraction device influences the supercritical state of the refrigerants, which has relatively high "density" mass flow and operations within the supersonic range. Referring to Figure 2, the most preferred mechanical extraction device is an integral supersonic device selected from the group consisting of the compressor 15 and the turbine 65. The specifically preferred device operates on either the ramjet or pulse jet principle. The result is a relatively compact high efficiency turbine or compressor for introducing mechanical energy respectively by pressurizing the concentrated solution or extracting mechanical energy by reducing the pressure during the expansion of the refrigerant.

Referring to Figure 2, the ScHPX has the ability to be in fluid communication with a traditional vapor compression system, such as the compressor 15. The refrigerant desorbed from the desorber 50 is further compressed with the vapor compressor 15 which elevates both; temperature and pressure as a method to increase the operating coefficient when cooling is desired, since the compressor energy is required only to increasingly increase the pressure gain beyond the pressure of the desorber 50, which is significantly less electrically / mechanically intensive energy. The refrigerant is in fluid communication with a heat exchanger 25 which effectively acts as a condenser, whose thermal energy can be transferred for many purposes including a desorber of the absorption heat pump of the second stage, preheating combustion air, preheating fuel of combustion, heating a secondary heat transfer fluid, or coations thereof. As noted earlier, the most critical aspect for efficiency in a heat pump absorption is the desorption energy. The ScHPX achieves desorption by the inventive coation of both; non-thermal methods and traditional thermal methods. Traditional thermal methods, as is known in the art, are achieved by the simple transfer of heat through heat exchangers air to liquid or liquid to liquid by means of which a relatively hotter fluid transfers thermal energy to the concentrated solution relatively colder. Preferred non-thermal methods are selected from the group consisting of magnetic refrigeration, vapor compression heat pump, spectrum light absorption, direct, activated, solar, electrostatic field, electrodialysis, membrane separation, electrodesorption, pervaporation, centrifugation gas, C02 liquid absorber from a vortex tube, and decanting. The membranes used for the removal of C02 do not operate as filters, where small molecules are separated from the larger ones through a medium with pores. Instead, they operate on the principle of solution-diffusion through a non-porous membrane. The first C02 dissolves in the membrane and then diffuses through it. Because the membrane has no pores, it does not separate on the basis of molecular size. Rather, it separates based on how well the different compounds dissolve in the membrane and then diffuse through it. An array of polyvinyl acetate vinyl chloride membranes, for example, allows a faster permeation of C02. Very small molecules and highly soluble molecules, small molecules (for example, C02) permeate faster than large molecules.

Referring to Figure 10, an additional non-thermal desorption medium includes radiofrequency and / or microwave energy. The preferred working fluid containing ionic liquids and ionic polymers is unique in its ability to absorb microwave energy. A preferred embodiment is the use of a nanofiltration device 400 that is devoid of materials that absorb microwave energy, absorb radiofrequency energy, destabilize the electrostatic field, destabilize the magnetic field, or coations thereof. The localized exposure of the concentrated solution to the aforementioned fields produces a rapid and energy efficient desorption. Membrane separation includes nanofiltration and traditional ultrafiltration as a method for separating components by means including molecular weight and particle size separation. Referring to Figure 3, the most preferred non-thermal method uses the coation of ferroelectric / ferromagnetic nanoscale powders in coation with magnetic refrigeration 105 which uses the magnetocaloric effect to elevate the concentrated solution 100 to more than the desorption temperature, and the subsequent removal of the working fluid from the magnetic field enables the refrigerant 120 to be desorbed, producing the weak solution 115 which transforms the concentrated solution into the weak solution by either using less heat energy from a heat exchanger or even without using thermal energy (that is, without any heat exchanger). The specifically preferred implementation continuously and sequentially pulses the concentrated solution into at least two desorption zones. Sequentially pressing the concentrated solution to the desorption zone enables a reduction of the pumping energy required to pressurize the concentrated solution in the desorption zone. Yet another aspect of the invention is the absence of a compressor in the standard absorption design. The only moving part is limited to a very small pump where small is in terms of energy consumed compared to the total energy of the system. The use of a piston-free pump offers the opportunity for an oil-free, low-cost, quiet, high-efficiency vapor compression system. The absence of oil is important in achieving benefits that include avoiding the solubilization of oil in the preferred supercritical carbon dioxide, which presents significant complexities, and eliminating the boundary layer of oil created on the heat transfer surfaces, which presents a deterioration of heat transfer. A ScHPX with ultra high COP incorporates a vapor compression stage as a method to achieve comparable COPs and beyond heat pumps with high vapor compression. Preferred compressors are also oil-free, which is achieved by incorporating many techniques as known in the art to reduce friction, including diamond coatings, diamond-like coatings, ultra-fine diamond coatings, air supports, levitation Magnetic and solid lubricants. Another aspect of the invention further avoids the complexities associated with compressors or pumps that are leak-free. Referring to Figure 4, the ScHPX, therefore, further includes a sealed container 35, whereby the sealed container captures the refrigerant filtered by the pumping system which is periodically evacuated in the weak solution. The sealed container captures the concentrated low pressure solution that filters into the sealed container. A controller monitors the pressure inside the sealed container to determine when a control valve is switched, whereby the pump 460 between the absorber 30 and desorber 50, which normally pressurizes the concentrated solution to the desorber, now pressurizes the losses in the sealed container in the absorber. The physical size and absorption speed are additional important components of any absorption system. The inventive ScHPX also includes a cavitation device, whereby the cavitation device improves the absorption rate by creating micro-bubbles with significantly greater surface area. The most preferred cavitation device is selected from the category of devices that create hydrodynamic cavitation. The physical size of the ScHPX is further reduced by the use of microchannel heat exchangers, whereby the supercritical fluids have reduced surface tension which counteracts the fluid friction associated with the large surface area heat exchangers. Configuration of the ScHPX System The inventive ScHPX is unique not only because of the specific components but also in terms of the operational configuration. A multi-stage heat pump system, also known as a cascade system, by means of which a different A coolant is used in at least one other stage and at least one other different B coolant is used in at least one other stage. Each stage is in effect a different thermodynamic cycle, although each stage is coupled to the other because the exit of one is the entrance of the other. The preferred ScHPX influences the differences in the desorption temperature of a refrigerant A and the absorption temperature of the refrigerant B. Refer to Figure 5, in other words, the thermal source of condensation (ie the condenser 259) of a single stage is the thermal source of desorption of the other stage (ie, capacitor 258). Still another configuration is the ScHPX that has direct infusion of a parallel power generation system or combustion chamber such that its exhaust is infused into the absorber. A key advantage is the capture of the latent energy of the exhaust stream. A more preferred implementation uses techniques as is known in the art to selectively enable the refrigerant to enter the absorber, thus, the exhaust air is treated to remove the by-products, whereby the by-products include NOx and sulfur. This implementation achieves the concurrent sequestration of carbon dioxide. The available cooling of the ScHPX is then used to pre-cool the combustion air to increase turbine capacity and energy efficiency. Referring to Figure 6, an additional gain in efficiency is obtained by capturing the thermal energy directly recovered from the losses of the thermal conduction of a combustion chamber 230 and of the combustion recuperator 220. Reclaimers are often used to capture waste heat, although thermal conduction through the external walls of the recuperator limits the total energy recovered, especially by narrow space deployments such as mobile vehicle applications. The thermal energy of the inventive ScHPX exceptionally uses low quality thermal sources. One such source is a non-concentrated solar collector. The most preferred solution has an integral heat exchanger inside the solar collector. Referring to Figure 7, a most preferred implementation is a solar collector 300 that achieves at least one benefit selected from the group consisting of concentrating the solar energy 310 as a means to reduce thermal losses and cool the photovoltaic cells 320. A specifically preferred implementation is an integral microchannel heat exchanger 340 to further reduce thermal losses and the size of the heat exchanger. And the particularly preferred implementation has a translucent film 330 that separates the solar collector and the heat exchanger, whereby the photons of the solar spectrum enable the desorption stimulated by the photon, thus reducing the desorption temperature. The stimulated desorption is also achieved by external electromagnetic and electric fields. The additional inclusion of nanoscale powders, including quantum dots and ultraviolet light absorbers, improves efficiency whereby the colloidal dispersion of the powders within the absorber improves the direct conversion of photons to electrons, and the subsequent transmission of the electron between the cathode and the electrode. The optimum solution has at least one solar collector stage followed by at least one solar concentrator stage where each stage creates an independent pressure zone (i.e., a superheated steam state). The use of the inventive ScHPX as noted earlier produces a higher power generation efficiency when the working fluid is further elevated to higher vapor states. The rise of the working fluid to a first vapor state through the use of a relatively lower temperature heat source, such as waste heat or non-concentrated solar energy, subsequently rises to a state of steam higher than through means that include the traditional steam compressor, concentrated solar energy, a combustion source, a relatively higher temperature heat source, or combinations thereof. This elevation of a lower vapor state to the subsequent higher vapor states can be repeated. Optimal energy efficiency replaces the use of the traditional steam compressor with staggered increments in the vapor states as a means to elevate the vapor state through a series of thermodynamic stages via a compressor / thermal-hydraulic pump. The use of a large surface area heat exchanger as an integral component of the area that increases the thermal-hydraulic pressure enables rapid increases in pressure. The ability to rapidly increase the pressure within each zone enables the expansion device to receive a working fluid with a constant pressure. There are numerous methods and devices to isolate one area from another. Such means is a valveless hydraulic pump comprised of a rotating cylinder having microchannels in the outer portion of the rotating cylinder. The internal part of the rotating cylinder is exposed to the thermal source. The rotating cylinder is inside an outer cylinder that seals each micro-channel thus isolating each zone within the micro-channel of the other zones. During the rotation period, the working fluid within the microchannel increases in both; in temperature and therefore in pressure. The fluid enters an individual micro-channel, preferably from an inlet duct that is perpendicular to the micro-channel along the entire length of the micro-channel. Likewise, the outlet duct has the same orientation with respect to the microchannel, but displaced rotationally along the cylinder. Alternatively, the thermal-hydraulic pump / compressor incorporates a slurry / "solid" of large surface area heated to a specified temperature, which is subsequently placed in a "sealed container". The working fluid is then infused into the sealed container leading to a rapid increase in pressure. The further incorporation of a spring piston to create a counterforce, preferably such that the spring creates a constant force at least equivalent to the desired inlet pressure of the expansion device. The spring also enables all the superheated steam to be ejected from the pressure zone and to maintain a constant pressure. The additional use of an air chamber or springs improves the constant pressure output from one pressure zone to the next or to the expansion device. An additional advantage is that each pressure zone is emptied essentially for full occupancy by the anterior pressure zone. Referring to Figure 9B, the independent pressure zones are alternatively produced by the use of the input diode 200, also referred to as input flow control devices. One such device used to regulate the output is an output diode 240, also referred to as a pressure relief valve. The use of a series of pressure relief valves, such that the thermofracting pressure is increasingly set to increase from the first pressure relief valve to the last with increasing increments for each pressure relief valve, is a effective way to prevent counterflow and to inherently provide controllable means to increase the steam state of the working fluid. The addition of the series of pressure relief valves within a heat exchanger, heater 250, or heater 220 of the displacement pump is hereinafter referred to as a "pressure train" heat exchanger. Thus, the pressure relief valve effectively creates independent zones within the pressure train. There are numerous methods known in the art for achieving precise and / or relative pressure control. It is anticipated that the optimal scenario is such that the last independent zone enables the output flow to occur at a precise pressure, either the pressure is controlled by an electronic pressure control in conjunction with a pressure detector or by a relief valve of mechanical pressure. Such a relief valve can also be activated at a differential pressure between the previous exit zone and the subsequent entry zone. Multiple heat exchangers of the pressure train, parallel, enable a constant pressure output for the power extraction device, such that an increase in either or both; the number of pressure relief valves within the pressure train and / or the number of multiple parallel pressure trains, leads to a more constant pressure output. Referring to Figure 9B, additional devices that create zones of independent pressure include a quasiturbine, quasiturbine used as a positive displacement pump, the positive displacement pump comprised of an inlet duct 210, an internal heater 220, and a duct 230 of output, and the hydraulic pump. Regarding Figure 8, the final characteristic of the implementation of the ScHPX achieves a higher efficiency operating with the cycle Goswami, Kalina, Baker, or Uehara. Under the Goswami cycle, the ScHPX can be optimized to provide maximum heating levels, cooling or energy, in addition to the total, optimal energy efficiency. An absorption heat pump system is represented having at least two pressure stages wherein each sequential stage has increasing pressure, with the first stage Pl less than the second stage P2. The use of at least one "compression" stage comprised of absorption uses significantly less electrical / mechanical energy compared to traditional steam compression compressors. An absorption heat pump exceptionally transforms the thermal energy, which is often the waste heat or readily available from the support processes, under pressure due to lower energy requirements to compress an "incompressible" liquid against a compressible vapor. The benefits are achieved under numerous configurations including, referring to Figure 11A where the working / absorbing fluid 450, such as ILs, is mixed with the concentrated solution of the absorber 430, such as the solid (Al) adsorbent, in an absorber 431 of the second stage. The mixed concentrated solution (A2) is subsequently pumped 460 from a lower pressure (Pl) to an increased pressure (P2) which is in fluid commation with the desorber 50. The desorbed refrigerant can optionally be compressed via a traditional steam compressor 15 for numerous purposes that include increasing the temperature of the condenser and raising the pressure for a subsequent extraction process. Referring to Figure 11B, the refrigerant was desorbed from a desorber 50 of the heat pump of absorption of the first stage and subsequently regulated with the flow valve 20 in an absorber 30 of the heat pump of absorption of the second stage to be raised to an increased pressure by pumping 460 of the concentrated solution, which is incompressible. Referring to Figure 11C, the refrigerant was desorbed from a desorber 50 of the heat pump of absorption of the first stage and subsequently regulated with a flow valve 20 in a vapor compression compressor 15 of the second stage to be raised to a increased pressure. Referring to Figure 11D, it alternatively represents the vapor compression compressor 15 as the first stage, such as the cases when the initial pressure PO is not sufficient for the refrigerant to be absorbed into the weak solution of the absorber 30 of the heat pump of absorption of the second stage, which, subsequently, is subsequently raised to an even higher pressure with high mechanical / electrical energy efficiency by the high pressure pump 460. All of these aforementioned configurations use less mechanical / electrical energy compared to a single-stage or even multi-stage steam compression compressor. Example 1 The absorption heat pump system wherein the operating mode for increasing the pressure from the initial pressure PO to the pressure P2 of the second stage is selected from the group consisting of (1) having a first adsorption or absorption stage that has the pressure Plx including solid or liquid adsorbents and a second stage of adsorption or absorption having the pressure P2i wherein the adsorbent Ali of the first stage is combined with a non-compressible liquid adsorbent A2i of the second stage and where Pli is less that P2i, or (2) have a compression stage without absorption of the first stage including compressors or turbochargers wherein the first stage increases the pressure of the initial pressure P02 to the operating pressure Pl2 and a second stage comprised of a stage of absorption that includes solid or liquid adsorbents where Pl2 is less than P22. Example 2 Example 1 is further comprised of a third step to further increase the pressure where the pressure-increasing means includes a compression step without absorption (i.e., traditional compressors, turbochargers, etc.) or an absorption pumping stage. Referring to Figure 12, the desorbed refrigerant, from the desorber 50, wherein the refrigerant is subsequently processed in at least one post-desorption process step selected from the group consisting of reaction chemistry (includes enzymatic chemistry, fermentation chemistry), extraction of the component, supercritical combustion, and combinations thereof, wherein the combined mechanical and electrical energy (?) required to increase the pressure of the working fluid to the operating pressure (PI) is at least ten percent less than the combined mechanical and electrical energy (E2) required to increase the working fluid pressure to the operating pressure (Pl) by compressing the compressible portion of the working fluid. This configuration is an enabling approach to increase the utilization of the benefits recognized in the art of supercritical extraction, supercritical combustion, and process intensification reactors "PIR". A wide variety of specific devices as known in the art are recognized for PIRs including hydrodynamic cavitation reactors, microchannels, rotating disk, tube rotary tube, oscillating flow, and reactive distillation reactors. The additional incorporation of nanoscale catalysts into the PIR, and more specifically with the use of supercritical working fluids, increases the reaction rates dramatically due to the high mass transfer rates and lower viscosity. A post-desorption process step, most notably within the applications of biomass to biofuel conversion, is an enzymatic reaction that is additionally comprised of immobilized enzymes. The conversion of biomass to biofuel, most notably cellulose to ethanol, is widely known in the art to utilize enzymes. However, the failure to solubilize cellulose demands the use of "free" enzymes in comparison to the immobilized enzymes to obtain acceptable enzymatic conversion rates. The inventive use of ionic liquids, and preferably poly-ionic liquid polymers of which a great variety is known in the art to have the ability to solubilize cellulose, exceptionally enable the immobilized enzymes to be used in combination. The additional use of refrigerants, particularly supercritical fluids including carbon dioxide significantly decreases the viscosity of the solubilized cellulose within the ILs. Poly-ionic liquid polymer "PILP" is superior to ILs due to the relative ease in recovering immobilized enzymes, which are incorporated into PILP by means known in the art of immobilizing enzymes in polymers, especially when using membrane filtration as a means to isolate the enzyme converted biomass of ILs and PILP. The combination of ILs and PILP provides the benefit of both immobilized enzymes, having relatively easy circulation of ILs compared to PILPs thus achieving effective biomass transport for immobilized enzymes. A preferred embodiment of the inventive application has the unique ability for the immobilized enzymes to be reused to produce a dramatic conversion rate and economical, with the additional advantage of having the subsequent ability to remove the spent enzymes from the PILP and IL slurry. which then are subsequently replenished with active enzymes, and again subsequently immobilized further within the PILP. Immobilized enzymes, which are specialty proteins that catalyze chemical reactions are removed from ILs by the additional addition of different enzymes that effectively transform the immobilized enzymes into byproducts that include amino acids, protein hydrolysates, or combinations thereof. The short chain amino acids and the protein hydrolysates have increased water solubility, therefore they can be washed from the PILP and IL slurry easily. Thus, the removal of the immobilized enzymes takes advantage of the byproducts that are insoluble or partially immiscible in the IL or PILP phase. The determination of when either / both of the IP and the PILP, and the immobilized enzymes are "spent" with the requirement of being removed / regenerated / replaced is by the placement of detectors to monitor at least one condition selected from the group consisting of the ionic liquid absorption rate, ionic liquid desorption rate, catalytic conversion rate, enzymatic conversion rate, and combinations thereof. Referring to Figure 12, a series of detectors 70 are placed to monitor the concentrated solution, the weak solution, and the refrigerant within the absorption heat pump, and both; before and after the subsequent process 470 which uses means to accelerate the conversion rate from biomass to biofuel including catalysts and enzymes. An alternative subsequent process for the absorption heat pump system is supercritical combustion. The previously noted benefits of achieving supercritical pressures by utilizing waste heat, including from said supercritical combustion process, enables the parasitic loss reduction of the energy process generated from the combustion process (i.e., energy coupled with the extraction device). of energy such as turbine) to be used to generate additional mechanical / electrical energy, while the low quality thermal energy is recovered to drive the compression of the inlet air.

Referring to Figure 13, an even further advantage of the present embodiment of the absorption heat pump, particularly the low energy availability of the supercritical fluids, enables at least one component of the by-products of combustion waste to be removed from within of the working fluid (for example, C02). The weak solution desorbed from the desorber 50, which contains ILs and / or PILP, and / or the refrigerant desorbed in the combustion process 480. It is widely recognized that supercritical carbon dioxide and ionic liquids, both individually and in combination, are superior solvents, therefore, operating the supercritical combustion process in a batch mode enables the non-combustion portion of the discontinuous operation to clean the by-products of combustion. The additional use of a fuel that contains excess gas greater than the gas required for stoichiometric combustion, enables the continuous removal of by-products, specifically when the excess gas is supercritical C02. rdless of whether the weak solution and / or the coolant is used to clean the combustion chamber of the combustion process 480, the "cleaning" fluid must have combustion waste byproducts removed in a manner known in the art for separation, which they include nanofiltration 400, before being used again within the cycle of the absorption heat pump. Referring to Figure 14, it is another preferred embodiment wherein the absorption / adsorption / ion exchange of the byproducts of the biomass to biofuel conversion process, which include carbon dioxide, methane, methanol, or combinations thereof, are used for produce additional biofuels. The traditional conversion of corn-based starch to ethanol is widely recognized for producing significant amounts of C02, and additionally uses a significant amount of thermal energy by producing waste heat of low quality. This waste heat recovered from the biomass process 490 through the heat exchanger 25 is in fluid communication with the desorber 50 through the heat exchanger 25. Another benefit of using supercritical combustion is the ability to add at least one 510 fuel additive that includes chitosan, glycerin, cellulose, and lignan. The preferred embodiment is such that chitosan, cellulose, and lignan are precipitated from the IL and PILP slurry by injection of water, and specifically preferred within a microchannel as a means to create a particle size less than about 10 microns and more. preferably less than about 1 miera and sizes particularly preferred less than about 100 nanometers. The large surface area enables a more complete combustion 520, which reduces the production of coal slag, ash and tar. An excellent carrier for biomass precipitates includes at least one fuel additive selected from the group consisting of biodiesel, natural gas, butanol, ethanol, gasoline, carbon dioxide, ammonia, hydrogen, and water. Still further additives include water, wet biomass, glycerin, glycerol, glycol including a glycol, dimethylene glycol, trimethylene glycol, or combinations thereof. A fuel containing colloidal suspensions of biomass precipitates is ideally suited for supercritical combustion within a porous combustion chamber, as recognized in the art to effectively produce zero emissions. Alternatively, the desorbed refrigerant which is in supercritical pressures enables more effective process intensification reactions 530. The reactions include at least one additional conversion process selected from the group consisting of catalytic reactions, combustion reactions, enzymatic reactions, and combinations thereof. A particularly preferred embodiment is the conversion of biomass by-products into additional biofuels that are converted electrochemically into a liquid or gaseous biofuel. The specifically preferred configuration transforms the waste heat to produce electricity that, at least in part, energizes the electrochemical conversion process. This configuration significantly increases the income yield of the biomass to biofuel conversion plant, since the revenues per unit of energy produced are much higher than the wholesale price of electricity. The ability to stay out of the grid and produce methanol (for example, from C02 + H20 in a reverse fuel cell) or other electrochemical reaction products has numerous benefits that include more carbon dioxide neutrality, increased income, higher fuel velocities reaction due in part to supercritical pressures, higher electrical conductivity due in part to IL, PILP, electron transfer mediators, etc. and to the 530 process intensification devices. Referring to Figure 15, another embodiment is an absorption heat pump system in fluid communication with a liquid desiccant system. A preferred embodiment includes the conversion of combustion processes to be supercritical combustion 520 where the exhaust waste heat is recovered. The combination exceptionally enables the waste heat used from the liquid desiccant system 540 to be recovered via the heat exchanger 25 to desorb the concentrated solution, which can be subsequently recovered to preheat the subsequent combustion cycle 550 including at least one selected of the group consisting of air intake of the combustion cycle, fuel of the combustion cycle, and combinations thereof. Continuing the waste heat recovery process allows the combustion exhaust to be recovered to produce power, increased cooling, or combinations thereof by means including desorbing the working fluid, regenerating the spent / wet desiccant system, or combinations thereof. Another configuration is an energy conversion system wherein the spent liquid desiccant of the liquid desiccant system 540, either as a dry desiccant / wet desiccant and with / without refrigerant desorbed from the desorber 50 of the absorption system, is additionally used as the fuel or a fuel component for combustion cycle 550. The preferred liquid desiccant is comprised of glycerin, glycerol, or glycol including a glycol selected from the group consisting of dimethylene glycol and trimethylene glycol, or combinations thereof. This distinct capacity produces fundamental advantages for integrating a variety of biofuel production into a plant, specifically the integration of a biodiesel plant that has significant thermal energy and glycerin as byproducts, both being valuable inputs for the production of ethanol. A still preferred embodiment recovers the latent energy of said exhaust from the combustion cycle 550 which becomes spent liquid absorbent and wherein said spent liquid absorbent is then used as the fuel or a fuel component for the combustion cycle. The spent liquid desiccant may additionally be comprised of at least one fuel selected from the group consisting of biodiesel, natural gas, butanol, ethanol, gasoline, carbon dioxide, ammonia, and hydrogen. Referring to Figure 16 is an enabling feature for the use of membrane filtration, which includes micro- and nanofiltration, under conditions of supercritical pressures. A series of detectors / controllers is required to maintain the pressure through nanofiltration 400 per membrane of the desorption chamber where the differential pressure across the membrane is less than the maximum operating pressure of the membrane. A minimum of two detectors / sensors 70 is required to monitor the pressure on each side of the membrane. Flow valves are required to vary the flow of the solution Concentrated on the inlet side of the membrane when using and controlling the flow of refrigerant to achieve precise control of the pressure. This occurs by simultaneously controlling the flow through the refrigerant flow valves 20 on the outlet side of the membrane to maintain the pressure differential at acceptable operating levels according to the membrane specifications. The insulated refrigerant can optionally be stored in a high pressure storage tank 560, and can be further pressurized using a traditional vapor compression compressor 15 to maintain adequate pressure particularly during start conditions. Each flow valve 20 of the working fluids is individually controlled for both sides of the membrane of the chamber.

Referring to Figure 17 is another feature implemented implementing a preferred embodiment of the absorption heat pump system, which is an energy conversion system comprised of an individually controlled compressor and an energy extraction device, and a fuel combustion chamber. whthe compression energy is switched or controlled dynamically to maximize power generation. The compression energy is provided from at least one source selected from the group consisting of (a) the thermal storage system 590, (b) the high pressure storage tank 560 which includes air, working fluid, or hydraulic oil, (c) the external preheater 580 including the thermal energy of said fuel combustion chamber, geothermal and solar sources, and (d) the heat pump of absorption using the waste heat for the desorber 50 of at least one selected source of the group consisting of said fuel combustion chamber, process of conversion of biomass to biofuel, geothermal and solar sources whthe expansion energy extracted from the turbine 65 drives a compressor 15 for the air inlet 570 of the compressor. Referring to Figure 18 is still another feature whthe desorbed refrigerant of the desorber 50 is comprised of C02. Supercritical C02 has difft advantages in the pre-processing of biomass 600 whthe working fluid passes through a separation process that includes nanofiltration 400 as a means to isolate carbon dioxide from other components within said fluid of work that include water, minerals, mineral salts, non-combustible, by-products of combustion, or combinations thf. Further separation of the cyclic, polycyclic, and macrocycle compounds including polyphenols, aromatics-containing compounds from the biomass before the 610 process of converting biomass to biofuel has benefits that include increasing the rate of conversion to biofuels and extracting additional components. of high value to increase the income stream. The isolation of C02 is an effective way to sequester C02, particularly since the C02 is already under supercritical pressure thus avoiding the significant energy penalty associated with the traditional C02 sequestration. Yet another preferred embodiment is the additional inclusion of cavitation devices that improve at least one speed selected from the group consisting of absorption 710, desorption 720, or combinations thf. The relatively high viscosity of the ILs and PILPs, especially with biomass gains with high solids content significantly from the use of cavitation devices that provides intimate mixing operating in the absorption mode, and separation operating in the desorption mode. Referring to Figure 19, another embodiment is an absorption heat pump system in fluid communication with a combustion process. A preferred embodiment includes recovering the waste heat from the exhaust air 581 through the recuperator 863 of the combustion process 480 such that the low quality energy of the lower cycle is transformed into useful energy by the high pressure of the heat pump system of absorption, desorbing of the refrigerant from the desorber 50 through a pressure exchanger 861, such as gerotor or a combination of compressor and expander (e.g., the turbine) with a common shaft, to "compress" the inlet air 570 into a higher pressure (preferably supercritical pressure). Another preferred embodiment preheats the inlet air 570 through a condenser 860 which recovers the absorption heat of the absorber 30 (which has gained thermal energy via the evaporator 862 within a refrigeration / air conditioning cycle). Another more preferred mode uses the air 581 in fluid communication downstream of the recuperator 863 to at least in part provide thermal energy to desorb the refrigerant and subsequently to provide thermal energy through a heat exchanger 25 for a variety of purposes including domestic hot water and preheating of the process water. The thermal energy resulting from the aforementioned combustion process 480 can be used for a wide variety of thermal energy conversion processes including the steam cycle, process heat, process heat, kettle and supercritical kettle. Referring to Figure 20, another embodiment is a dynamic thermal bus for switching a series of thermal sources, represented herein as a general heat exchanger 25 and the heat pump 850 (i.e., in this scenario the reverse thermal diode 93 to be in fluid communication with the capacitor). The preferred embodiment has a switching arrangement 94 comprised of at least one input switching circuit 95 and output switches 92 (including normally open as shown with preferably a normally closed 91 as shown), as is known in the art, which has the ability to switch any thermal source from a series of thermal sources to any thermal bus circuit of a series of thermal bus or thermal bus circuits. A representative example of the variation of the thermal bus circuits is a series of circuits having an objective temperature that deviates from the average temperature of the thermal bus 834. This example uses three circuits that have a target temperature differential of ten degrees Celsius below the mean respectively 833, 832, and 831, in addition to three circuits that have a target temperature differential of ten degrees Celsius above the mean respectively 835, 836, and 837. Each circuit of the thermal bus has at least one detector 70 that includes the temperature sensor to detect the actual temperature of the circuit. The detector / additional measurements include the mass flow rate, thermal energy flow rate, and pressure.

Measuring the pressure is critical, especially when the pressures are in the supercritical range to keep the pressure below the burst pressure, to minimize pressure losses. A preferred embodiment of the dynamic thermal bus is to integrate a series of detectors 70 to detect / monitor critical parameters, particularly parameters (hereinafter referred to as "non-linear parameters") to identify the nonlinear algorithm for the energy efficiency of the source thermal, energy efficiency of the heat sink, coefficient of performance of the final product of the thermal source, and coefficient of performance of the final product of the heat sink (eg cooling, electric power produced, etc. divided by the total energy input) as a function of at least one parameter selected from the group consisting of inlet temperature of the heat exchanger of the thermal bus, heat exchanger outlet temperature of the thermal bus, mass flow rate of the thermal bus, inlet temperature of the thermal source, thermal source outlet temperature, and flow rate of mass of the thermal source. Numerous methods known in the art are anticipated to control fluid flow including valves, clean materials whose properties change as a function preferably, but not limited to temperature, variable speed pumps, flow switches and thermal diodes. Referring to Figure 21, an alternative embodiment is shown showing a series of heat sources where a thermal source has insufficient thermal energy that is transported away to the thermal collector from the thermal source leading to the path of the thermal power switching circuit from the thermal source in contact / thermal communication directly to a heat sink including the pump 850 heat to raise the temperature. Yet another embodiment is where a lower temperature circuit, such as supporting a refrigerator evaporator 920 is then directed in fluid communication to a thermal source including the heat pump 851 for undercooling. The thermal bus of the multiple circuit is represented by an example of three circuits 810, 820, and 830 that are in fluid communication switchable by methods known in the art for switching flows and / or thermal transport as represented by the switched circuit 840. Still another embodiment is a configuration where the thermal sources within any one circuit are in series of thermal sources by sequentially increasing the inlet temperature of the thermal source as a method to maximize the heat transfer of each thermal source. Alternatively where the heat sinks within any circuit are in series of heat sinks by the heat sink input temperature that decreases sequentially as a method to maximize the heat transfer of each heat sink. A wide variety of heatsinks or thermal sources are anticipated within residential / commercial / industrial environments including refrigerator condenser 910, refrigerator evaporator 920, dishwasher waste heat reclaimer 930 (also optionally with water recovery), cooler 940 furnace, 950 water tap sink, 960 shower, 970 electronic components cooler, 980 lighting cooler (including LEDs, particularly a series of LEDs), a 990 heat pump condenser, 991 heat pump evaporator, one or more 992 heat exchangers of external heat, and / or a window heat exchanger 993. The aforementioned window heat exchanger transforms non-visible light (ie the infrared and / or ultraviolet spectrum) into thermal energy that is in thermal contact with a thermal bus circuit. The optimal implementation of the window heat exchanger is a compound transparent to visible light, preferably comprised of a nanocomposite of high thermal conductivity to transport the thermal energy in the thermal bus. The most preferred embodiment includes a nanocomposite film transparent to visible light having high thermal conductivity, contained within the multi-facet cavity, in thermal communication with the window heat exchanger (preferably a supercritical pressure fluid heat exchanger). , and particularly preferred is a fluid having nanoscale additives with low visible light absorption and high infrared absorption and / or high ultraviolet light absorption). The particularly preferred embodiment of the window heat exchanger is additionally comprised of a nanocomposite film having an outer film that reflects the inside of the infrared and / or ultraviolet spectrum waves. The heat exchanger is additionally comprised of a nanocomposite film on an inner face that reflects the infrared and / or ultraviolet spectrum waves from the outer surface back to the thermally conductive film and reflects the waves of the infrared and / or ultraviolet spectrum from interior of the building (in which the window exchanger is built) back to the occupied space of the building to minimize thermal losses. The window heat exchanger and / or the thermally conductive film are preferably additionally comprised of aerogels as one such method to minimize thermal losses. The thermally conductive film and the window heat exchanger are additionally thermally insulated from the window structure as is known in the art. Referring to Figure 22, the fluid flow velocity of the thermal bus or thermal bus is controlled within the preferred embodiment by a variable speed pump control 460 using a series of detectors 70 that detect / monitor a range of parameters for determine energy efficiency including inlet and outlet temperature, flow fluid velocity, kilowatt-hour "kwh" energy consumption, kWh power generation, BTUs meter (ie, thermal energy). Due to the non-linearity of thermodynamics, achieving optimal, total system energy efficiency is not simply dependent on maximizing the thermal recovery of waste heat from thermal sources but rather to precise flow control as the preferred method for impact the temperature change (ie, delta T) through the thermal sources. The thermal bus or thermal bus is controlled to maximize the temperature gain of the largest thermal bus circuit within the constraints of the maximum thermal energy demand of the thermal energy dissipators that include the maximum flow rate and the maximum temperature (ie, the system will not increase the flow rate beyond the maximum usable level by adding energy dissipators or beyond the maximum usable temperature of any power dissipator by concurrently sacrificing the energy efficiency of other power dissipators) . The determination to maximize the temperature of a thermal circuit has many sanction conditions in terms of the energy efficiency of the individual component that include (a) reducing the total amount of waste heat recovered, (b) reducing sub-cooling / pre-heating the condenser inside a vapor compression system that can lead to lower energy efficiency to achieve air conditioning / cooling, (c) biomass pre-processes 600 and / or biomass fermentation processes have clear maximum process temperatures at which enzymatic reactions will deteriorate and enzymes could even be deactivated, (d) increasing the temperature for the removal of absorption energy within the absorber 30 leads to a lower absorption cooling, (e) increasing the temperature beyond the critical desorption temperature simply increases the amount of energy that needs to be removed in the subcooling portion of the absorption cooling cycle, (f) increasing the temperature beyond the limits The design of components such as turbine blades 65 can gain energy efficiency but at the cost of system life time where the increasing revenue gain from power generation can not exceed the increasing increase in maintenance expense, and (g) numerous heat sinks are not operated either in steady state / equilibrium conditions including the liquid desiccant cooling system 540 which in fact is regenerated discontinuously. Another feature of the preferred embodiment uses the aforementioned switch circuit 840 to determine the output of a particular thermal bus circuit, selected (eg, the highest temperature circuit 837) which is routed in fluid communication to a particular heat sink, selected including devices such as the cooling condenser 910, or the inlet air 570 for a subsequent combustion process. The direction / path of the fluid flow of the thermal bus or thermal bus is controlled by a series of algorithms based on non-linear parameters that represent the thermal sources and the heat sinks in fluid communication (ie, connected) to the thermal bus.

The thermal source (s) and the heat sink (s) are connected to at least one circuit of the thermal bus through a thermal interface that includes the thermal diode and / or the thermal switch (including the diode / thermal switch of the following types as known in the art: liquid metal switches, phase change materials, clean materials, movable thermal contact comprised switches that include high thermal conductivity nanocomposites such as a compound of fixation of carbon nanotubes). The particular heat sink / source, preferred, is connected via an arrangement of the switching circuit which has the means to vary the thermal communication with at least two circuits of the thermal bus. The switching circuit of the specifically preferred dynamic thermal bus is controlled according to a thermal bus control system comprised of at least one series of non-linear parameters and at least one diode / thermal switch. The dynamic thermal bus is additionally comprised of thermal storage devices preferably additionally comprised of detectors to provide real-time feedback of the level of storage capacity and temperature. The modes of operation of the control system include: (a) method for maximizing the total thermal energy for the mechanical / electrical energy conversion, (b) method for maximizing the mass flow rate at the highest achievable temperature, (c) ) method to maximize mass flow velocity at minimum achievable temperature, (d) method to minimize energy consumption from fuel sources that have greenhouse gas emissions, (e) method to minimize the cost of consumption of total energy from all sources where cost includes any sanctions for greenhouse gas emissions, (f) the aforementioned "e" mode additionally comprised of the operating restrictions of the parameters that ensure that each thermal source and heat sink (a) from now on also referred to as "equipment") meets the minimum operating conditions, and (g) the previously mentioned "f" mode additionally e of quantitative costs due to failure to meet the minimum operating conditions. The control system is additionally comprised of data that include schedules, equipment operation programs, predictive equipment operation programs, predictive meteorology and occupancy programs of buildings, and is additionally comprised of non-linear algorithms that include algorithms of energy consumption of the equipment and power generation algorithms of the equipment.

Claims (98)

1. CLAIMS 1. An energy conversion system, characterized in that it comprises an absorption heat pump system and at least one operating fluid selected from the group consisting of ionic liquids, ionic solids, electride solutions, and alkaline solutions.
2. 2. An energy conversion system, characterized in that it comprises an absorption heat pump system, at least one supercritical working fluid, and at least one device selected from the group consisting of (a) a rotating disk reactor, ( b) a hydraulic thermal compressor including a pressure train heat exchanger, (c) a series of independent pressure stages having stepped or pulsed flow, (d) a hydraulic pump having an integral heat sink or a gerotor, and (e) a mechanical energy extraction device including a gerotor, an expansion turbine, an expansion pump, a Stirling cycle engine, an Ericsson cycle engine, or a pulse jet turbine.
3. 3. An energy conversion system, characterized in that it comprises an absorption heat pump system and a working fluid desorbed by at least one thermal method and at least one non-thermal method including non-thermal methods selected from the group consisting of magnetic refrigeration, absorption of spectrum light, direct, activated, solar, electrodialysis, apply electrostatic fields, separation by membrane, electrodesorción, pervaporación, apply gas centrifuge, apply the liquid absorber of C02 of tube with vortex, and decantation.
4. 4. The energy conversion system according to claim 2, characterized in that the at least one supercritical fluid is staggered or pulsed sequentially in series in at least two zones of superheated or desorption steam.
5. The energy conversion system according to claim 4, characterized in that it further comprises a sealed container capable of capturing the refrigerant filtered by the absorption heat pump system and wherein the sealed container is periodically evacuated in the weak solution .
6. 6. The energy conversion system according to claim 4, characterized in that it further comprises a cavitation device capable of improving the absorption speed that includes cavitation devices capable of creating hydrodynamic cavitation.
7. The energy conversion system according to claim 4, characterized in that the at least one supercritical fluid is staggered or pulsed sequentially by means devoid of pistons, capillary devices, or heat pipes.
8. 8. An energy conversion system, characterized in that it comprises a multiple phase absorption heat pump, capable of operating in a first stage and in a second stage, and having at least one first refrigerant used in the first stage and minus a second refrigerant used in the second stage.
9. 9. The energy conversion system according to claim 2, characterized in that it further comprises a combustion process wherein the combustion process is capable of creating exhaust and where the exhaust is infused into the heat pump of absorption as a medium for the sequestration of carbon dioxide.
10. The energy conversion system according to claim 9, characterized in that the exhaust from the combustion process is further processed to reduce the exhaust byproducts including N0X and sulfur.
11. The energy conversion system according to claim 2, characterized in that it also comprises a combustion process and a combustion recuperator capable of recovering the waste heat that includes thermal conduction losses, wherein the waste heat recovered is used to desorb the supercritical working fluids of the absorption heat pump system.
12. 12. The energy conversion system according to claim 2, characterized in that it further comprises at least one integral solar collector and at least one integral solar concentrator in series creating at least two independent pressure zones.
13. 13. The energy conversion system according to claim 12, characterized in that it further comprises at least one absorber selected from the group consisting of ionic liquids, ionic solids, electride solutions, and alkaline solutions.
14. 14. An energy conversion system, characterized in that it comprises an absorption heat pump system with at least one integral supersonic device selected from the group consisting of a compressor and a turbine, wherein the compressor and the turbine are capable of operating either on a ramjet principle or a pulse reactor principle.
15. 15. The energy conversion system according to claim 2, characterized in that the energy conversion system is operable on a thermodynamic cycle selected from the group consisting of a Goswami cycle, a Kalina cycle, a Baker cycle, a cycle Uehara, and derivatives thereof.
16. 16. The energy conversion system according to claim 1, characterized in that it further comprises at least one nanoscale powder selected from the group consisting of conductive, semiconductor, ferroelectric, and ferromagnetic powders.
17. 17. The energy conversion system according to claim 3, characterized in that it further comprises at least one nanoscale powder selected from the group consisting of conductive, semiconductor, ferroelectric, ferromagnetic powders including powders with nanoscale surface modifications, including surface modified powders having monolayer, or multilayer, nanoscale coatings.
18. 18. The energy conversion system according to claim 1, characterized in that the at least one working fluid has partial miscibility including and wherein the phase separation is by means of the variation of at least one fluid parameter of work selected from the group consisting of temperature, pressure, and pH.
19. 19. The energy conversion system according to claim 2, characterized in that the at least one working fluid has a partial miscibility and wherein the phase separation is by means of varying at least one parameter of the selected working fluid. of the group consisting of temperature, pressure, and pH.
20. 20. The energy conversion system according to claim 1, characterized in that the working fluid is an electride or alkali solution operable in addition with additional thermodynamic cycles as a means to maximize the thermal energy in power generation.
21. 21. The energy conversion system according to claim 3, characterized in that the at least one working fluid has a partial miscibility and wherein the phase separation is by means of varying at least one parameter of the selected working fluid. of the group consisting of temperature, pressure, and pH.
22. 22. An energy conversion system, characterized in that it comprises an absorption heat pump operable as a hydraulic thermal pump, wherein the hydraulic thermal pump is comprised in addition to a supercritical working fluid, wherein the supercritical working fluid is stepped or pulsed sequentially through an integral heat exchanger, and where the supercritical working fluid is desorbed by the absorption heat pump.
23. 23. The energy conversion system according to claim 22, characterized in that the supercritical working fluid is further comprised of at least one absorber selected from the group consisting of ionic liquids, ionic solids, electride solutions, and solutions of alkaline
24. 24. The energy conversion system according to claim 1, characterized in that the working fluid is further comprised of at least one ionic liquid monomer and at least one ionic liquid polymer.
25. 25. The energy conversion system according to claim 24, characterized in that the ionic liquid polymer is of a particle size approximately between about 0.1 nanometers and about 500 microns.
26. 26. The energy conversion system according to claim 24, characterized in that the ionic liquid polymer is of a particle size of between about 10 nanometers and about 5 microns.
27. 27. The energy conversion system according to claim 24, characterized in that the ionic liquid polymer is of a particle size of approximately 0.1 nanometers to 500 nanometers.
28. 28. A working fluid of the energy conversion system, characterized in that it comprises an absorption heat pump system and a working fluid, wherein the working fluid is additionally comprised of a polymer of polyionic liquid and at least an additional additive selected from the group consisting of ionic liquids, solid non-polymeric adsorbents, and combinations thereof.
29. 29. The energy conversion system according to claim 28, characterized in that the working fluid is additionally comprised of at least one non-ionic compound selected from the group consisting of cyclic, polycyclic, and macrocycle compounds including antioxidants, polyphenols , lignans, and vitamins, and for which the working fluid has improved thermal stability and operational life.
30. 30. The energy conversion system according to claim 28, characterized in that the working fluid is additionally comprised of at least one additive selected from the group consisting of electron transfer mediator, electron donor, electron acceptor, ultraviolight absorber, infrared absorber, quantum dot, and nanoscale dust.
31. 31. The energy conversion system according to claim 28, characterized in that the absorption heat pump uses microwaves for the desorption energy.
32. 32. The energy conversion system according to claim 28, characterized in that the absorption heat pump is additionally comprised of a nanofiltration device devoid of materials that absorb the energy of at least one energy source or field selected from the group which consists of microwave energy, radiofrequency energy, electrostatic field, and magnetic field.
33. 33. The energy conversion system according to claim 28, characterized in that the working fluid is selected from the group consisting of magnetic ionic liquids, poly-ionic liquid polymers, and combinations thereof.
34. 34. The energy conversion system according to claim 30, characterized in that the electron transfer mediator includes polycationic protein, complexes with tialoto bridges, thiolated complexes, metalloproteins, protein complexes having an iron-sulfur group, complexes trehalose, iron-sulfur grouping, sodium-ammonia, sulfur-ammonia, a complex of chitosan including chitosan lactate, lipoic acid chitosan alpha, and thiolated chitosan, or combinations thereof
35. 35. The energy conversion system according to claim 28, characterized in that the working fluid is additionally comprised of an additive capable of improving the transfer of the electron including iron salts, iron salt derivatives, potassium salts, salts of lactic acid, derivatives of potassium salts, salt derivatives of lactic acid, phytic acid, gallic acid and combinations thereof.
36. 36. An energy conversion system, characterized in that it comprises an absorption heat pump system with multiple pressure stages, wherein a first pressure stage has a first pressure, Pl, and a second pressure stage has a second pressure. , P2, and where the first pressure Pl is less than the second pressure P2.
37. 37. The energy conversion system according to claim 36, characterized in that the multiple pressure stages are comprised of at least one absorption pressure stage and at least one vapor compression pressure stage.
38. 38. The energy conversion system according to claim 36, characterized in that the multiple pressure stages are capable of operating in a first pressure stage and a second pressure stage, and have at least a first absorbent Al used in the first pressure stage and at least one second absorbent A2 used in the second pressure stage, and whereby the absorbers include solid adsorbents, ionic liquids, poly-ionic liquid polymers, and combinations thereof.
39. 39. The energy conversion system according to claim 38, characterized in that the absorbent Al is mixed in the absorbent A2, and wherein the energy required to achieve an increase in the pressure P2 is less than the energy required to raise the pressure from Pl to P2 for the absorbent Al.
40. 40. The energy conversion system according to claim 39, characterized in that the absorbent Al is selected from the group consisting of a solid adsorbent, polyionic liquid polymer, and combinations thereof, and wherein the absorbent A2 is selected from the group consisting of ionic liquids, glycerin, water, and combinations thereof.
41. 41. The energy conversion system, characterized in that it comprises a system of absorption heat pump, a working fluid, and a desorption stage in which the working fluid is desorbed in a working fluid of weak solution and a refrigerant , and wherein the refrigerant is subsequently processed in at least one process step selected from the group consisting of (a) a chemical reaction process that includes enzymatic chemistry, fermentation chemistry, (b) a component extraction process, ( c) a supercritical combustion process, and combinations thereof, wherein the combined mechanical and electrical energy Ei required to increase the pressure of the working fluid to the operating pressure Pl is at least ten percent less than the mechanical E2 energy and combined electric required to increase the working fluid pressure to the operating pressure Pl by compressing the compressible portion of the l work fluid.
42. 42. The energy conversion system according to claim 41, characterized in that the at least one process step uses a process intensification reactor that includes reactors selected from the group consisting of hydrodynamic cavitation reactors, microchannels, rotating disk , tube rotating tube, oscillating flow, and reactive distillation reactors.
43. 43. The energy conversion system according to claim 42, characterized in that the at least one process step is additionally comprised of nanoscale catalysts.
44. 44. The energy conversion system according to claim 42, characterized in that the at least one process step is additionally comprised of immobilized enzymes.
45. 45. The energy conversion system according to claim 44, characterized in that the immobilized enzymes are immobilized in at least one ionic liquid selected from the group consisting of polymer of polyionic liquid, and ionic liquid.
46. 46. The energy conversion system according to claim 45, characterized in that the immobilized enzymes are further processed by sequential process steps that include (a) removing the immobilized enzymes from the ionic liquid, and (b) replenishing then immobilizing the active enzymes within the ionic liquid.
47. 47. The energy conversion system according to claim 46, characterized in that the immobilized enzymes are further processed by sequential process steps that include (a) removing the immobilized enzymes from the ionic liquid by the additional enzyme addition to convert the enzymes. Enzymes immobilized in byproducts that include amino acids, protein hydrolysates, and combinations thereof.
48. 48. The energy conversion system according to claim 47, characterized in that the working fluid is comprised of at least a first phase and a second phase, and wherein the first phase contains the ionic liquid and the second phase is insoluble or partially immiscible with the ionic liquid, and wherein the by-products are insoluble or partially immiscible in the first phase.
49. 49. The energy conversion system according to claim 41, characterized in that the absorption heat pump system is additionally comprised of a detector for monitoring at least one parameter selected from the group consisting of an ionic liquid absorption rate, ionic fluid desorption rate, catalytic conversion rate, and enzymatic conversion rate.
50. 50. The energy conversion system according to claim 41, characterized in that the supercritical combustion process step is additionally comprised of at least one fuel additive that includes chitosan, glycerin, cellulose, and lignan.
51. 51. The energy conversion system according to claim 50, characterized in that the supercritical combustion process step is additionally comprised of fuel, and wherein the fuel is additionally comprised of at least one fuel additive selected from the group consisting of of biodiesel, natural gas, butanol, ethanol, gasoline, carbon dioxide, ammonia, hydrogen, and water.
52. 52. The energy conversion system according to claim 41, characterized in that the supercritical combustion process step is comprised of a combustion process within a porous combustion chamber.
53. 53. The energy conversion system according to claim 41, characterized in that the supercritical combustion process step is capable of producing a by-product waste and wherein the waste by-product is removed by at least one component within the fluid of work.
54. 54. The energy conversion system according to claim 53, characterized in that the stage of combustion process is capable of operating discontinuously having a combustion cycle and a non-combustion cycle, and wherein the waste by-product it is removed during the non-combustion cycle.
55. 55. The energy conversion system according to claim 41, characterized in that the supercritical combustion process step is additionally comprised of a fuel that contains an amount of excess gas greater than the amount of gas required for the stoichiometric combustion. , and where the amount of excess gas cleans the combustion chamber of waste by-products.
56. 56. An energy conversion system, characterized in that it comprises a system of absorption heat pump and a working fluid, wherein the working fluid absorbs at least one by-product of a biomass to biofuel conversion process that includes a by-product comprised of at least one gas selected from the group consisting of carbon dioxide, methane, and methanol, and wherein the working fluid absorbs the at least one by-product at a pressure P0 of operation.
57. 57. The energy conversion system according to claim 56, characterized in that the process of converting biomass to biofuel is capable of producing waste heat, and where the waste heat is used to desorb the at least one by-product in a Pl pressure of operation, and where Pl is greater than PO.
58. 58. The energy conversion system according to claim 56, characterized in that the process of converting biomass to biofuel has at least one stage of conversion process selected from the group consisting of catalytic reactions, combustion reactions, and reactions enzymatic
59. 59. The energy conversion system according to claim 56, characterized in that the process of converting biomass to biofuel is additionally comprised of a process step capable of electrochemically converting the at least one by-product into a liquid fuel or gaseous.
60. 60. The energy conversion system according to claim 58, characterized in that the process step that is capable of electrochemically converting the at least one by-product is energized by the electricity produced at least in part of the pump system. calorific absorption.
61. 61. The energy conversion system according to claim 41, characterized in that the absorption heat pump is additionally comprised of a pressure exchanger selected from the group consisting of gerotor, piston, and turbine.
62. 62. The energy conversion system according to claim 41, characterized in that the working fluid is comprised of a refrigerant, and wherein the refrigerant is made in a mixture additionally comprised of at least one selective additive of the group consisting of of water, wet biomass, glycerin, glycerol, glycol including a glycol, dimethylene glycol, trimethylene glycol, biodiesel, natural gas, butanol, ethanol, gasoline, carbon dioxide, ammonia, and hydrogen.
63. 63. The energy conversion system according to claim 62, characterized in that the mixture is capable of being used within a supercritical combustion process.
64. 64. The energy conversion system according to claim 63, characterized in that the mixture is capable of being used within a process intensification reactor.
65. 65. An energy conversion system, characterized in that it comprises an absorption heat pump system in fluid communication with a liquid desiccant system.
66. 66. The energy conversion system according to claim 65, characterized in that it further comprises a combustion cycle capable of producing waste heat, and wherein the waste heat is used to produce power, additional cooling, or combinations of the same.
67. 67. The energy conversion system according to claim 66, characterized in that the waste heat is used to desorb the working fluid, regenerate the liquid desiccant system, or combinations thereof.
68. 68. The energy conversion system according to claim 65, characterized in that the waste heat is used to desorb the working fluid, regenerate the liquid desiccant system, or combinations thereof.
69. 69. An energy conversion system, characterized in that it comprises an absorption heat pump system and a combustion system, wherein the combustion system is capable of producing a by-product of combustion, and wherein the working fluid of the combustion Absorption heat pump is used to clean the combustion system of combustion byproducts.
70. 70. The energy conversion system according to claim 69, characterized in that the absorption heat pump system is comprised of a refrigerant absorption stage, wherein the combustion by-product is comprised of impurities, and wherein the Working fluid is further processed to isolate the impurities from the working fluid before the absorption stage of the refrigerant.
71. 71. An energy conversion system, characterized in that it comprises a liquid desiccant system and a combustion cycle, wherein the liquid desiccant system is capable of producing waste heat from the process to regenerate the spent liquid desiccant, and wherein the waste heat is additionally used to preheating a combustion inlet that includes at least one selected from the group consisting of air intake of the combustion cycle, fuel of the combustion cycle, and combinations thereof, in a subsequent combustion cycle process.
72. 72. The energy conversion system according to claim 71, characterized in that the subsequent combustion cycle is capable of producing additional waste heat, and wherein the additional waste heat is additionally used to regenerate the spent liquid desiccant.
73. 73. The energy conversion system according to claim 71, characterized in that the combustion cycle is capable of burning a fuel, and wherein the fuel is additionally comprised of the spent liquid desiccant.
74. 74. The energy conversion system according to claim 71, characterized in that the spent liquid desiccant is additionally comprised of a supercritical gas.
75. 75. The energy conversion system according to claim 71, characterized in that the liquid desiccant system comprises at least one liquid desiccant selected from the group consisting of (a) glycerin, (b) glycerol, and (c) glycol including a glycol selected from the group consisting of dimethylene glycol and trimethylene glycol.
76. 76. The energy conversion system according to claim 71, characterized in that the spent liquid desiccant further comprises at least one fuel selected from the group consisting of biodiesel, natural gas, butanol, ethanol, gasoline, carbon dioxide, ammonia , and hydrogen.
77. 77. The energy conversion system according to claim 76, characterized in that the fuel is at a pressure greater than the supercritical pressure.
78. 78. An energy conversion system, characterized in that it comprises a combustion process and a liquid absorber, wherein the combustion process burns a fuel, wherein the combustion process is capable of producing exhaust, wherein the liquid absorbent is capable of recovering the latent energy of the exhaust that becomes a spent liquid absorbent, and wherein the spent liquid absorbent is capable of being used as at least one component of the fuel.
79. 79. An energy conversion system, characterized in that it comprises a detector / controller for maintaining the pressure through a membrane of the desorption chamber, wherein the pressure through the membrane of the desorption chamber is a differential of pressure, and where the pressure differential is less than the maximum operating pressure of the membrane of the desorption chamber.
80. 80. The energy conversion system according to claim 79, characterized in that the membrane of the desorption chamber is comprised of an inlet side and an outlet side, wherein the energy conversion system is additionally comprised of a working fluid, and wherein the detector / controller is capable of varying the flow of the working fluid individually on both sides; of entrance and exit, of the membrane of the desorption chamber.
81. 81. An energy conversion system, characterized in that it comprises a fuel combustion chamber, a compressor capable of being controlled individually and dynamically, and an energy extraction device capable of being individually controlled to maximize the generation of power.
82. 82. The energy conversion system according to claim 81, characterized in that the compressor consumes compression energy, and wherein the compression energy is provided from at least one source selected from the group consisting of (a) thermal storage system , (b) high pressure storage tank that includes air, working fluid, or hydraulic oil, (c) external preheater that includes thermal energy from the fuel combustion chamber, a solar source, and geothermal source, and (d) ) the absorption heat pump using the waste heat from at least one source selected from the group consisting of the fuel combustion chamber, a biomass to biofuel conversion process, a solar source, and a geothermal source.
83. 83. The energy conversion system according to claim 36, characterized in that the pressure before the first pressure stage is an initial pressure PO, and wherein the energy conversion system is additionally comprised in an operating mode for increasing the pressure from PO to P2 selected from the group consisting of (a) having a first adsorption or absorption stage, wherein the first stage of adsorption or absorption has a Pli pressure, wherein the first stage of adsorption or absorption has a absorbent Alj. which includes solid or liquid absorbent, wherein the second stage of adsorption or absorption has a pressure P2i and an absorbent A2X, where Ali is combined with A2lr where A2i is a non-compressible liquid adsorbent, and where Pli is less than? 2 ?, and (b) ) having a compression stage without absorption of the first stage including compressors or turbochargers wherein the first stage of adsorption or absorption has a pressure Pl2, wherein the pressure of the first stage of adsorption or absorption increases from the initial pressure PO to the operating pressure Pl2, wherein the second adsorption or absorption stage has a pressure P22, wherein the second adsorption or absorption stage has an adsorbent A22 that includes solid or liquid adsorbents, and wherein Pl2 is less than P22.
84. 84. The energy conversion system according to claim 83, characterized in that it further comprises a third stage of adsorption or absorption capable of increasing the pressure above the pressure of the second adsorption stage or absorption stage, and where to increase the pressure is by means that include a compression process without absorption or a pumping process with absorption.
85. 85. The energy conversion system according to claim 83, characterized in that the energy conversion system further comprises a working fluid containing carbon dioxide and at least one additional fluid component, wherein the working fluid passes. through at least one separation process step as a means to isolate carbon dioxide from the at least one additional fluid component in the working fluid.
86. 86. The energy conversion system according to claim 83, characterized in that the energy conversion system is capable of sequestering carbon dioxide.
87. 87. The energy conversion system according to claim 83, characterized in that the absorption heat pump is additionally comprised of a cavitation device capable of improving at least one speed selected from the group consisting of absorption and desorption speed.
88. 88. The energy conversion system according to claim 83, characterized in that the energy conversion system further comprises a working fluid containing at least one nanoscale powder including a nanoscale powder selected from the group consisting of nanoscale conductive, semiconductor, ferroelectric, and ferromagnetic, and combinations thereof.
89. 89. The energy conversion system according to claim 83, characterized in that it further comprises at least one working fluid, wherein the working fluid has partial miscibility and is capable of phase separation by means including varying at least a parameter selected from the group consisting of temperature, pressure, and pH.
90. 90. The energy conversion system according to claim 36, characterized in that it further comprises a working fluid containing cyclic, polycyclic, and macrocycle compounds including polyphenols, compounds containing aromatic rings of biomass before the conversion process of biomass to biofuel, and wherein the energy conversion system is additionally comprised of a separation method to isolate the cyclic, polycyclic, and macrocycle compounds from the working fluid.
91. 91. An energy conversion system, characterized in that it comprises a dynamic bus or thermal bus and a thermal bus or switchable thermal bus that has multiple thermal bus circuits, multiple devices selected from the group consisting of a source device thermal and a heat sink device, and a switching circuit, wherein the switching circuit is capable of routing dynamically the thermal transport between the thermal bus circuit and the device.
92. 92. The energy conversion system according to claim 91, characterized in that it further comprises a control system with non-linear algorithms capable of determining at least one parameter selected from the group consisting of energy efficiency of the thermal source, efficiency of heat sink energy, coefficient of performance of the final product of the thermal source, and coefficient of performance of the final product of the heat sink.
93. 93. The energy conversion system according to claim 92, characterized in that the control system is capable of operating as a function of at least one parameter selected from the group consisting of inlet temperature of the heat exchanger of the thermal bus or thermal bus bar, thermal bus heat exchanger outlet temperature, thermal bus mass flow rate, thermal source input temperature, thermal source output temperature, and mass flow rate of the source thermal
94. 94. The energy conversion system according to claim 92, characterized in that the control system is able to dynamically route the fluid flow between the thermal sources, the heat sinks, and the thermal bus or thermal bus circuits , wherein the thermal sources are able to be ordered sequentially by increasing the inlet temperature of the thermal source, and where the heat sinks are ordered sequentially by decreasing the heat sink inlet temperature.
95. 95. The energy conversion system according to claim 91, characterized in that it further comprises a window heat exchanger in thermal contact with a thermal bus circuit, wherein the window heat exchanger is exposed to light, and wherein the window heat exchanger is capable of transforming the ultraviolet and / or infrared spectrum into thermal energy.
96. 96. The energy conversion system according to claim 92, characterized in that the control system is capable of routing dynamically the flow of fluid between the thermal sources, the heat sinks, and the thermal bus or thermal bus circuits, and where the thermal bus is controlled to maximize the temperature gain of a thermal bus circuit within the operating constraints of the thermal sink parameter including the maximum demand of thermal energy, maximum flow speed and maximum temperature.
97. 97. The energy conversion system according to claim 92, characterized in that the control system operates in selected modes of the group consisting of (a) maximizing the total thermal energy for the mechanical / electrical energy conversion, (b) ) maximize the mass flow rate at the highest achievable temperature, (c) maximize the mass flow rate at the minimum achievable temperature, (d) minimize the energy consumption of fuel sources that have effect gas emissions greenhouse, (e) minimize the cost of total energy consumption from all sources where cost includes any sanctions for greenhouse gas emissions, (f) mode "e" additionally comprised of operating restrictions of the parameters that ensure that each thermal source and heat sink meets the minimum operating conditions, and (g) the "f" mode additionally comprised of quantitative costs per failure to meet the s minimum operating conditions.
98. 98. The energy conversion system according to claim 92, characterized in that it also comprises data including schedules, equipment operation programs, predictive equipment operation programs, predictive meteorology and building occupancy programs, and included in addition to non-linear algorithms that include heat sink energy consumption algorithms and heat sink energy generation algorithms.