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US 2012/0186219A1 Jul.26,2012 Theprocessofisolatingcarbondioxideisreversiblesuchthat liquidfuels.TypicalcatalyticreactionsWillalsoyieldmeth anincreaseoftemperaturebeyondacriticalpointchangesthe equilibriumpoint. [0021] Theterm“recuperator”isamethodofrecovering Waste heat downstream of an expander and transferring the thermal energy upstream of either a compressor, turbocom pressor or pump. [0022] Theterm“exhaustport”isanymethodcapableof discharging a Working ?uid that can include safety valve, pressureregulatedvalve,expansiondeviceventingtoatmo sphere,etc. [0023] Theterm“pressureincreasingdevice”isanydevice capableofincreasingthepressureofaWorking?uid,include a turbocompressor, turbopump, compressor, or pump. [0024] Theterm“high-side”isthehighpressuresideofa closed loop thermodynamic cycle such that the high-side is doWnstream of a pressure increasing device and upstream of an expander device. [0025] Theterm“loW-side”istheloWpressuresideofa closed loop thermodynamic cycle such that the loW-side is doWnstream ofan expander device and up stream ofa pressure increasingdevice. [0026] Here,asWellaselseWhereinthespeci?cationand claims, individual numerical values and/or individual range limits can be combined to form non-disclosed ranges. [0027] Exemplaryembodimentsofthepresentinvention WillnoW bediscussedWithreferencetotheattachedFigures. Such embodiments are merely exemplary in nature. Further more, it is understand as knoWn in the art that sensors to measure thermophysical properties including temperature and pressure are placed throughout the embodiments as knoWn in the art, most notably positioned to measure at least one thermophysical parameter for at least one thermody namic state point. The utiliZation of valves as standard mass ?oW regulatorsisassumed(i.e.,notdepicted)tobeasknoWn intheartandcanalsoincludevariable?oW devices,expan sionvalve,turboexpander,tWo Way orthreeWay valves.The utiliZation of methods to remove heat from the Working ?uid by a condensor (used interchangeably With condenser) is merely exemplary in nature as a thermal sink and can be substitutedbyanydevicehavingatemperatureloWerthanthe Working ?uid temperature including absorption heat pump desorber/generator, liquid desiccant dehumidi?er, process boilers, process superheater, and domestic hot Water. With regard to FIGS. 1 through 4, like reference numerals refer to likeparts. ane and hydrogen as byproducts. The reactor 10 ispreferably con?guredWithanintegralphaseseparator,suchthatatleast CO2 isremovedatacontrolledratetobothvarythebiomass solutionpH andtoincreaseinteractionbetWeenthecellulose and the desired reactant(s). The liquid fuel has a higher den sity than the ScCO2, as Well as other byproducts including methaneandhydrogen,thusthenon-condensablegases(i.e., insupercriticalstate)attheseconditionsWillbubbletothetop ofthereactor10.The particularlypreferredreactantWiththe cellulose material 20 is methanol 30, Which are either mixed Withthecellulosicmaterial20priortothereactor10orin-situ Within the reactor 10. Though not depicted in FIG. 1, the cellulosicmaterial20ispreferablypreheatedbyutiliZingthe ScCO2 as removed from the reactor 10. The utiliZation of biomass as depicted in FIG. 1 can be substituted by virtually anyCO2 source,suchasacalcinerutiliZedforthemanufac turingofcement.YetanotheralternativeistheCO2 produced bybiomassfermentation. [0031] TurningtoFIG.2,FIG.2isasequential?oWdia gram offurtherembodiments ofFIG. 1inaccordanceWiththe presentinvention.The ScCO2 isfurtherfractionatedfromthe othergases46(i.e.,includingmethaneCH4 andhydrogen H2). The other gases 46, Which can also be fractionated betWeentheCH4 andH2 asdesired),areutiliZedWithina poWer generator such as a gas turbine 60. The gas turbine 60 ispreferablyaramjet,asknoWn intheart,capableofaccept ingarelativelyloWcalori?cfuelofatleastoneofCH4 and H2. The Waste heat from the gas turbine 60 is transferred through the Waste heat exhaust heat exchanger 70 to the methanol 30 reactant in the preferred embodiment. The uti liZation of Waste heat, preferably above 400 degrees Celsius (andparticularlyabove600degreesCelsius,andspeci?cally above 800 degrees Celsius) enables the methanol to disasso ciate into syngas 35 (as knoWn in the art). The disassociation reaction is an endothermic reaction, thus enabling the pre ferred separation of the endothermic reaction from the sub sequent exothermic reaction of cellulose disassociation. RemainingunutiliZedWastenottransferredintothemethanol 30 is then transferred through a second Waste heat exhaust heat exchanger 76 into a second poWer generator cycle 100 (as knoWn in the art to include Organic Rankine Cycle “ORC”, Supercritical CO2 “ScCO2” Rankine or Brayton Cycles, or steam simple to combined cycle). Itisunderstood that the order of heat exchangers 70 and 76 can be altered in the event that the methanol disassociation is not desired prior to entry of the reactor 10 or ifthe disassociation temperature of methanol is substantially reduced through enhanced cata lytic performance. The enhanced catalytic performance [0028] Itisunderstoodthatvirtuallyeveryembodimentof thisinventioncanincludeCO2 sourcessuchascalciners,high temperaturefurnaces,andfuelcombustors. [0029] Everycon?gurationandembodimenthasacontrol Wouldenablehigherexergyef?ciencytobeachievedby system and method of control to operate the poWer generation cycle(s) and to obtain optimal control of a combined ScCO2 cycle and a secondary cycle that yields at least CO2 and preferablyalsoyieldsWasteheatasabyproduct. [0030] TurningtoFIG.1,FIG.1isasequential?oWdia gramofoneembodimentofasupercriticalCO2 sourcein accordance With the present invention. The ScCO2 as depicted here is from the reaction of biomass at conditions in excess of 100 degrees Celsius (preferably above 150 Celsius, andparticularlypreferableabove200Celsius)andpressures abovethesupercriticalpressureofCO2 (preferablyabove 1500psi,particularlypreferableabove2000psi,andspeci? axial,orimpulseturbines)toproducepoWer(e.g.,mechanical callypreferredabove2500psi).Thepreferredreactionyields energyorelectricity).ThenoWexpandedCO2 ispreferably CO2, suchasthecellulosicbreakdoWnusingcatalystsinto passed through the cellulosic material 20, more speci?cally expanding the Working ?uid (and producing poWer) of the poWer generator cycle 100 prior to transferring thermal energy to the methanol 30, such that the Waste heat from the poWergeneratorcycle100Wouldbesubsequentlytransferred tomethanol30inlieuofheatexchanger70.Oncethemetha nol 30 is disassociated by Waste heat transferred by the heat exchanger 70, the noW syngas is quenched by transferring thermalenergyintothesupercriticalCO2 45asamethodof superheatingthroughtheWasteheatexhaustheatexchanger 75. The noW superheated CO2 45 is expanded through an expander80(asknoWninthearttoincludecentrifugal,radial,PDF Image | HYBRID SUPERCRITICAL POWER CYCLE
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