Abstract:
A first aspect of the present invention is a self-contained electrolysis process. The process includes utilizing a cryogenic cogeneration process to extract a liquid from an atmospheric medium, passing a current through the liquid, and separating at least one chemical element from the liquid. A second aspect of the present invention is a self-contained electrolysis apparatus. The apparatus includes cryogenic cogeneration means for extracting a liquid from an atmospheric medium, electrical means for passing a current through the liquid and separating means for separating at least one chemical compound from the liquid. A third aspect of the present invention is a method and system of removing at least one element from a chemical compound. The method and system include utilizing a cryogenic cogeneration process to remove the at least one element from the chemical compound.

Description:
CROSS REFERENCE TO RELATED APPLICATION(S) 
       [0001]    This application is related to and claims priority from U.S. Provisional Patent Application Ser. No. 60/904,130, filed Feb. 27, 2007. 
     
    
     BACKGROUND 
     Hydrogen Production 
       [0002]    Hydrogen has been touted as an environmentally friendly wonder fuel that can be used in vehicles and burns to produce only water as a by product. Hydrogen production is a large and growing industry. Globally, some 50 million metric tons of hydrogen, equal to about 170 million tons of oil equivalent, were produced in 2004. The growth rate is around 10% per year. Within the United States, 2004 production was about 11 million metric tons (MMT), an average power flow of 48 gigawatts. As of 2005, the economic value of all hydrogen produced worldwide is about $135 billion per year. 
         [0003]    There are two primary uses for hydrogen today. About half is used to produce ammonia (NH 3 ) via the Haber process, which is then used directly or indirectly as fertilizer. The other half of current hydrogen production is used to convert heavy petroleum sources into lighter fractions suitable for use as fuels. This latter process is known as hydrocracking. Hydrocracking represents an even larger growth area, since rising oil prices encourage oil companies to extract poorer source material, such as tar sands and oil shale. The scale economies inherent in large-scale oil refining and fertilizer manufacture make possible on-site production and “captive” use. Smaller quantities of “merchant” hydrogen are manufactured and delivered to end users as well. 
         [0004]    Additionally, it is possible that fuel cells, using hydrogen as a fuel, will be able to replace most internal combustion engines and at the same time will solve most grid load balancing needs. It will do this by allowing “storage” of electrical energy in a grid of plug-in automobiles, which will be available to store excess energy as hydrogen, and offering it to the electrical grid as needed, after conversion in fuel cells. Hydrogen in this sense would act like a chemical battery and would essentially replace battery technology in electrical hybrid cars. 
         [0005]    Although hydrogen fuel cells do not emit harmful gases into our atmosphere but other hazardous conditions exist due to the extremely explosive properties of hydrogen. Also, it is not economically efficient to completely modify our infrastructure to make our society dependent on hydrogen, since present technology requires costly energy consumption to liquify the hydrogen. 
       Carbon Capture 
       [0006]    About 85% of the world&#39;s commercial energy needs are currently supplied by fossil fuels. Carbon capture and storage is an approach to mitigate global warming by capturing carbon dioxide from large point sources such as fossil fuel power plants and storing it instead of releasing it into the atmosphere. Although CO 2  has been injected into geological formations for various purposes, the long term storage of CO 2  is a relatively untried concept and as yet no large scale power plant operates with a full carbon capture and storage system. 
         [0007]    CCS applied to a modern conventional power plant could reduce CO 2  emissions to the atmosphere by approximately 80-90% compared to a plant without CCS. Capturing and compressing CO 2  requires much energy and would increase the fuel needs of a plant with CCS by about 11-40%. These and other system costs are estimated to increase the cost of energy from a new power plant with CCS by 21-91%. These estimates apply to purpose-built plants near a storage location: applying the technology to preexisting plants or plants far from a storage location could be more expensive. 
         [0008]    Consequently, the technology of CCS would enable the world to continue to use fossil fuels but with much reduced emissions of CO 2 , while other low-CO 2  energy sources are being developed and introduced on a large scale. In view of the many uncertainties about the course of climate change, further development and demonstration of CCS technologies is a prudent precautionary action. 
       SUMMARY 
       [0009]    Varying embodiments of the present invention include a self-contained electrolysis process and an apparatus associated therewith. In an embodiment, a cryogenic cogeneration process is employed in conjunction with an atmospheric medium to separate desired chemical compounds via electrolysis for storage and/or future use. Consequently, through the use of the present inventive concepts, desired chemical compounds (e.g. hydrogen, CO 2 ,) can be capture in an effective and cost efficient manner. 
         [0010]    A first aspect of the present invention is a self-contained electrolysis process. The process includes utilizing a cryogenic cogeneration process to extract a liquid from an atmospheric medium, passing a current through the liquid, and separating at least one chemical element from the liquid. 
         [0011]    A second aspect of the present invention is a self-contained electrolysis apparatus. The apparatus includes cryogenic cogeneration means for extracting a liquid from an atmospheric medium, electrical means for passing a current through the liquid and separating means for separating at least one chemical compound from the liquid. 
         [0012]    A third aspect of the present invention is a method and system of removing at least one element from a chemical compound. The method and system include utilizing a cryogenic cogeneration process to remove the at least one element from the chemical compound. 
         [0013]    Other aspects and advantages of the present invention will become apparent from the following detailed description, taken in conjunction with the accompanying drawings, illustrating by way of example the principles of the invention. 
     
    
     
       BRIEF DESCRIPTION OF DRAWINGS 
         [0014]    The accompanying drawings, which are incorporated in and constitute a part of the specification, illustrate varying embodiments of the inventive concepts and, together with a general description given above and the detailed description of the varying embodiments given below, serve to explain the principles of the invention. 
           [0015]      FIG. 1  shows a cryogenic cogeneration system in accordance with an embodiment of the present invention. 
           [0016]      FIGS. 2-1  and  2 - 2  shows the system in conjunction with varying embodiments of the present invention. 
           [0017]      FIG. 3  show an overview of the integrated electrochemical and thermochemical renewable energy production, storage, distribution and recycling system in conjunction with an automated computer control network. 
       
    
    
     DETAILED DESCRIPTION 
       [0018]    The following description is presented to enable one of ordinary skill in the art to make and use the invention and is provided in the context of a patent application and its requirements. Various modifications to the embodiments and the generic principles and features described herein will be readily apparent to those skilled in the art. Thus, the present invention is not intended to be limited to the embodiment shown but is to be accorded the widest scope consistent with the principles and features described herein. 
         [0019]    Varying embodiments of the present invention include a self-contained electrolysis process and an apparatus associated therewith. In an embodiment, a cryogenic cogeneration process/system is employed in conjunction with an atmospheric medium to separate desired chemical compounds via electrolysis for storage and/or future use. Consequently, through the use of the present inventive concepts, desired chemical compounds (e.g. hydrogen, CO 2 ,) can be capture in an effective and cost efficient manner. 
       Hydrogen Production 
       [0020]      FIG. 1  shows a cryogenic cogeneration system  1  in conjunction with an embodiment. The system  1  includes a liquid receiver  8 , a liquid subcooler  14 , a super heater compressor  22 , a condenser  35  and an expansion engine  150 . In an embodiment, the system  1  converts energy from an external heat source medium  1000  into mechanical and/or electrical energy. For a further description of this exemplary system, reference may be had to U.S. patent application Ser. No. 11/100,197, filed Apr. 5, 2005, entitled “Cryogenic Cogeneration System”, which is incorporated herein by reference. 
         [0021]    Please refer now to  FIGS. 2-1  and  2 - 2 . Accordingly, the electrolysis process preferably begins by chilling heat source medium  1000 , via the superheater compressor  22 . Once chilled, the medium  1000  is piped through distribution valve  1059  via supply piping route  1003  and piping and apparatuses  1025 , into optional atmospheric vapor extraction coil  1002 . Vapor extraction coil  1002  preferably absorbs desired electrolyte from vapor  1001  via thermally conductive contact with vapor  1001 . The condensed/frozen vapor  1001  is then stored as ice and/or as liquid (e.g. water) via gravity flow into liquid electrolyte supply tank  1007 . 
         [0022]    A liquid electrolyte pressure pump  1026  draws the ice and/or liquid  1001  to central electrolyte supply distributor  1004 . Here a conductive solvent injection system  1013  and a vaporized electrolyte steam Supply tank  1005  collaborate to distribute negatively charged anions to ion supply  1012  in anode tank  1018  and positively charged cations to ion supply  1006  in cathode tank  1020 . Here, the desired element gas (e.g. hydrogen) can be separated from the liquid molecule/compound (e.g. water). 
         [0023]    Accordingly, the hydrogen gas exits cathode tank  1020  via discharge exit  1008  and distribution valve  1051  to a gas turbine  1066  via valve  1067  and/or to a storage tank  1022  via supply line  1009 . Hydrogen gas is subsequently discharged from storage tank  1022  via discharge exit  1010  to a heat rejection coil  1011  to condense/freeze/sublime the hydrogen and fill storage tank  1014  at supply tank entrance  1016 . The hydrogen can then be removed from storage tank  1014  via discharge exit  1015 . 
         [0024]    In an embodiment, expansion engine  150  provides power to turn drive shaft  1030  that is coupled to an electrical generator  1032  and rectifier  1071 . The electrical generator  1032  can be a direct current (DC) generator or an alternating current (AC) generator. The negatively charged (electron excessive) pole  1034  of generator  1032  (or Optional Rectifier  1071 ) feeds the line side of electrolysis cell  1072  to polarize electrolytic cathode electrode  1040 . The positively charged (electron deficient) pole  1036  of generator  1032  (or Optional Rectifier  1071 ) feeds the line side of electrolysis cell  1072  to polarize electrolytic anode electrode  1038  to facilitate the correlated above-described electrolysis process. 
       Voltaic Process 
       [0025]    In an alternate embodiment, a self-contained voltaic process is implemented. Here, the hydrogen from storage tank  1009  and/or cathode tank  1020  are routed by the distribution valve  1051  to anode fill tank  1047  via anode electrode  1046  of voltaic fuel cell  1045 . The voltaic fuel cell  1045  also includes a cathode fill tank  1049  for storing cathodes routed to the cathode electrode  1048  via storage tank  1018 . The pertinent re-dox reaction with the voltaic fuel cell electrolyte  1050  takes place and desired ions/reactant(s)/element (e.g. oxygen) from the cathode fill tank  1049  re-bond and form gas and/or liquid (e.g. steam/water) that can exit via piping  1025  through valves  1055  and  1056  to be distributed per demand conditions. 
         [0026]    Alternatively, the steam/water can be recycled back into original reduced forms via re-entering the electrolysis system as a gas through a steam supply tank  1005  and/or the steam reforming tank  1037  as distributed by steam feeder valve  1056  and/or as a liquid via the bottom exit of  1050  and re-entering supply tank  1007  through piping  1025 . Steam can optionally travel via supply distribution valve  1066  and perform work output via steam expansion engine turbine  1065 . 
       Liquefaction 
       [0027]    Liquefaction of gases includes a number of processes used to convert a gas into a liquid state. The processes are used for scientific, industrial and commercial purposes. Many gases can be put into a liquid state at normal atmospheric pressure by simple cooling; a few, such as carbon dioxide, require pressurization as well. Liquefaction is used for analyzing the fundamental properties of gas molecules (intermolecular forces), for storage of gases and in refrigeration and air conditioning. 
         [0028]    Accordingly, in an alternate embodiment, a liquefaction process can be implemented. The process begins whereby the desired element e.g. Hydrogen, exits hydrogen production tank  1029  through distribution valve  1054  via hydrogen outlet  1035 . The hydrogen then proceeds through to gas turbine  1066  via valve for  1067  and/or storage tank  1009 . Next, the hydrogen exits storage tank  1009  via discharge exit  1010  to become in thermally conductive contact with heat rejection coil  1011 . Once in thermally conductive contact with the heat rejection coil  1011 , the hydrogen liquefies to fill storage tank for  1014  through supply entrance  1016 . 
         [0029]    Although the above-described embodiments are described in the context of hydrogen production, one of ordinary skill in the art will readily recognize that a variety of different chemical elements can be produced with this system while remaining spirit and scope of the present inventive concepts. 
         [0000]    Self Contained Electricity Generation, Distribution and/or Storage Process 
         [0030]    In an alternate embodiment, a self-contained electricity generation, distribution and storage process is implemented. The process begins whereby expansion engine  150  from cryogenic cogeneration system  1  provides power to turn drive shaft  1030  that is coupled to electrical generator  1032  with or without the option of utilizing rectifier  1071 . The negatively charged (electron excessive) pole  1034  and the positively charged (electron deficient) pole  1036  of rectifier  1071  feed the line sides of electrical switching to battery storage  1073  through switch  1042  to facilitate the charging of storage battery(s)  1041 . 
         [0031]    In an alternate process, expansion engine  150  from cryogenic cogeneration system  1  provides power to turn drive shaft  1030  that is coupled to electrical generator  1032  with rectifier  1071 . The negatively charged (electron excessive) pole  1034  and the positively charged (electron deficient) pole  1036  of rectifier  1071  feed the line sides of switch  1073  through switches  1076  and  1077  to facilitate the alternating and/or direct current power load to/from Supplemental Refrigeration/Thermalelectric System  1078 ( a,b  . . . ) within a parallel array of Supplemental Refrigeration/Current Generation System(s)  1079 . This array can include but is not be limited to Dilution Cryocooler(s), Adiabatic Demagnetization Refrigerators, Pulse Tubes, Brayton Cycles, Claude Cycles, Thermal Electric Refrigerators, Vortex Tubes, Dry Ice Refrigerators, and Stirling Engines which could include the utilization of Optional Sequenced Inverter  1093 ( a,b  . . . ). 
         [0032]    Direct Current 
         [0033]    In another embodiment, expansion engine  150  from cryogenic cogeneration system  1  provides power to turn drive shaft  1030  that is coupled to electrical generator  1032  with rectifier  1071 . The negatively charged (electron excessive) pole  1034  and the positively charged (electron deficient) pole  1036  of rectifier  1071  feed the line sides of switch  1073  through power distribution switch  1074  to supply direct current to electrical power demand load  1075  (e.g. electric motor, transformer, etc). 
         [0034]    Alternating Current 
         [0035]    In another embodiment, expansion engine  150  from cryogenic cogeneration system  1  provides power to turn drive shaft  1030  that is coupled to electrical generator  1032  with rectifier  1071 . The negatively charged (electron excessive) pole  1034  and the positively charged (electron deficient) pole  1036  of rectifier  1071  feed alternating current to the line sides of switch  1073  through power distribution switch  1074  to supply alternating current to electrical power demand load  1075  (e.g. electric motor, transformer, etc). 
         [0036]    Voltaic Fuel Cell 
         [0037]    In another embodiment, Voltaic (Fuel) Cell anode electrode  1046  and Voltaic (Fuel) Cell cathode electrode  1048  feed direct current power via switch  1044  through switch  1074  for supply of direct current demand load  1075  or via inverter  1070  for supply of alternating current to demand load  1075 . Additionally, Voltaic (Fuel) Cell anode electrode  1046  and Voltaic (Fuel) Cell cathode electrode  1048  feed direct current power via switch  1044  to facilitate the charging of Storage Battery(s)  1041 . 
         [0038]    Furthermore, the distribution of electrical power demand load  1075  can be cryogenically cooled to reduce/eliminate resistance attributed to counter electromotive force via thermal contact with Superconducter Cryogenic Cooling Medium/Heat Exchanger  1064  contained within Superconducter Cryogenic Cooling Loop for Electrical Power Distribution Line Feeders  1063 . After Medium  1064  absorbs heat from load  1075 , the medium returns as a heat source medium  1000  via valve  1062 . The medium then rejects heat and becomes re-chilled via superheater compressor  22  to be re-supplied via valves  1061  and  1090  back to complete Loop  1063 . 
         [0000]    Integration of the Cryogenic Cogeneration System with a Parallel Array of Supplemental Refrigeration and/or Thermal Electrical Current Generation System(s) 
         [0039]    This integration process begins by chilling heat source medium  1000 , via superheater compressor  22 , from cryogenic cogeneration system  1 . The medium  1000  is discharged though distribution valve  1059 , where the chilled medium  1000  is routed to piping route  1003  via distribution valves  1090  and  1061 . Chilled medium  1000  then proceeds through distribution valve  1088  to the calculated pertinent thermal energy exchanger  1084 ( a,b  . . . ) which will absorb thermal energy from the thermal energy exchanger for supplemental refrigeration system  1081 ( a,b  . . . ). Medium  1000  then returns back to superheater compressor  22  via distribution valves  1087 ,  1062  and  1052  to complete the integration loop. 
         [0040]    Additionally, temperature and/or thermal differentials between  1081 ( a,b  . . . ) and  1080 ( a,b  . . . ) at least partially attributed to the aforementioned integration process may generate a current that can travel via switching  1076 ,  1077 , and  1042  to supplement the charging of battery storage systems  1041  and/or other appropriate electrical power load demands. 
         [0000]    Cryogenic Cogeneration System Interaction with Supplemental Refrigeration/Current Generation System 
         [0041]    Condenser to Subcooler 
         [0042]    In an embodiment, the cryogenic cogeneration system  1  can interact with the Supplemental Refrigeration/Current Generation System(s)  1080  ( a,b  . . . ) to create a temperature difference in order to supplement the efficient operation thereof. Here, the condenser  35  rejects heat to heat sink medium  1094  which will exit condenser  35  through distribution valve  1089  via distribution valve  1085  to enter the calculated pertinent thermal energy exchanger  1080 ( a,b  . . . ) which will absorb heat from medium  1094  as it circulates through the calculated pertinent thermal energy rejecter coil  1083 ( a,b  . . . ). It then exits as a chilled/sub-cooled medium via distribution valve  1086  and then proceeds through distribution valve  1091  to feed liquid sub-cooler  14  and/or liquid receiver  8 . 
         [0043]    Receiver to Subcooler 
         [0044]    In an alternate embodiment, liquid receiver  8  rejects heat to heat sink medium  1094  which exits receiver  8  through distribution valve  1089  via distribution valve  1085  to enter the calculated pertinent thermal energy exchanger  1080 ( a,b  . . . ) which will absorb heat from medium  1094  as it circulates through the calculated pertinent thermal energy exchanger rejecter coil  1083 ( a,b  . . . ) to exit as a chilled/subcooled medium via distribution valve  1086  then through distribution Valve  1091  to feed liquid sub-cooler  14  and/or liquid receiver  8 . 
       Carbon Capture 
       [0045]    In another embodiment, the cryogenic cogeneration system  1  can be employed to remove carbon from fossil fuel. This can be accomplished pre-combustion or post-combustion. 
       Pre-Combustion 
       [0046]    In the pre-combustion embodiment, the process begins whereby fossil fuel  1031  and/or discharge for desired gas element (e.g. Oxygen)  1021  flows via valve  1108  and/or distribution valve  1110  to gas emission capture tank  1027  where waste gas separator coil  1028  is employed to remove undesired elements through thermally conductive contact with carbon emission extraction coil  1024 . Fuels  1031  and  1021  can then re-circulate back via valve  1106  to supply burners  1095  for cleaner combustion. This process can be applied to all types of combustion systems. 
       Post-Combustion 
       [0047]    In the post-combustion embodiment, make up steam from boiler  1033  enters and supply steam reforming tank via  1037  as distributed by feeder valve  1056  to mix with fossil fuel  1031  via steam reforming tank entrance  1039  within steam reforming (Hydrogen Production) tank  1029 . 
         [0048]    Harmful emissions (e.g. carbon) can be captured from Steam Reforming Tank  1029  and/or Optional Steam Boiler  1033  and/or Burners  1095  preferably with extraction hood  1057  to be exhausted via distribution piping  1058  to injector  1028  and extraction coil  1024 . The extraction coil  1024  then transfers absorbed heat into external heat source medium  1000 , via thermally conductive contact. The medium  1000  then returns via circulation through distribution valve  1052  back to the superheater compressor  22 . 
         [0049]    Here, the medium  1000  is re-chilled and re-circulated via distribution valve  1059  to be routed back through loop  1060  and again through capture tank  1027 . Processed product (e.g. liquid CO 2  and Dry Ice) can then be removed from capture tank exit  1069  and/or Dry Ice Dispenser door  1092 . 
         [0050]    It should be noted that an automated computer control network may be implemented to control part and/or all of the aforementioned processes via the use of an indefinite number of electronic and/or electromechanical and/or pneumatic and/or hydraulic actuators, relays, and all other pertient parts and accessories of a complete control system.  FIG. 3  show an overview of the integrated electrochemical and thermochemical renewable energy production, storage, distribution and recycling system  1096  in conjunction with an automated computer control network  1097 . 
         [0051]    Without further analysis, the foregoing so fully reveals the gist of the present inventive concepts that others can, by applying current knowledge, readily adapt it for various applications without omitting features that, from the standpoint of prior art, fairly constitute the characteristics of the generic or specific aspects of this invention. Therefore, such applications should and are intended to be comprehended within the meaning and range of equivalents of the following claims. Although this invention has been described in terms of certain embodiments, other embodiments that are apparent to those of ordinary skill in the art are also within the scope of this invention, as defined in the claims that follow.