Abstract:
system and method is disclosed to increase the efficient of internal combustion engines using to generate electric power, where the system and method converts a portion of thermal energy produced in the combustion process to a usable form of energy.

Description:
BACKGROUND OF THE INVENTION 
       [0001]    1. Field of the Invention 
         [0002]    The present invention relates to the utilization of waste heat from diesel or other types of internal combustion engines used in power generation. 
         [0003]    More particularly, the present invention relates to utilizing waste heat from diesel or similar types internal combustion engines used for power generation, where the engines are relatively small and produce an exhaust gas effluent stream having an initial temperature not more than 900° F., and where the system produces a spent exhaust effluent stream having a final temperature as low as 250° F. 
         [0004]    2. Description of the Related Art 
         [0005]    A specific characteristic of small diesel engines or other similar internal combustion engines used for power generation is that they produce relatively low temperature exhaust gas effluent stream. 
         [0006]    Although the utilization of heat from exhaust gas can be done in many different ways using conventional type of bottoming cycles, these bottoming cycles generally require large capital investments and are not geared for use with small diesel engines used in power generation. 
         [0007]    Thus, not only is there an need in the art for more efficient and effective means for extracting usable work from waste heat generated by small internal combustion engines. 
       SUMMARY OF THE INVENTION 
       [0008]    The present invention provides a simple bottoming cycle for use with small internal combustion engines used for power generation. In its simplest embodiment, the cycle includes a turbine for extracting energy from a fully vaporized multi-component working fluid, a condenser, two heat exchangers and a separator designed to convert the spent working fluid into a liquid working fluid and into a partially vaporized working fluid stream and a recuperative heat recovery vapor generator designed to extract energy from an exhaust stream having a temperature not greater than about 900° F. to convert the partially vaporized working fluid stream into a fully vaporized and in certain embodiment superheated working fluid stream for energy extraction in the turbine. The cycle is a closed cycle for the working fluid. 
         [0009]    The present invention also provides a simple bottoming cycle for use with small internal combustion engines used for power generation. In another embodiment, the cycle includes a turbine for extracting energy from a fully vaporized multi-component working fluid, a condenser, three heat exchangers and a separator designed to convert the spent working fluid into a liquid working fluid and into a partially vaporized working fluid stream and a recuperative heat recovery vapor generator designed to extract energy from an exhaust stream having a temperature not greater than about 900° F. to convert the partially vaporized working fluid stream into a fully vaporized and in certain embodiment superheated working fluid stream for energy extraction in the turbine. The cycle is a closed cycle for the working fluid. 
         [0010]    The present invention also provides a simple bottoming cycle for use with small internal combustion engines used for power generation. The cycle comprises four multi-component fluid working solutions: a lean working solution having a highest concentration of the higher boiling component, a very rich working solution having a highest concentration of the lower boiling component, a rich working solution having a second highest concentration of the lower boiling component and an intermediate working solution having an intermediate concentration of the low boiling component. Stated differently, the stream have the following order of lower boiling component: [low boiling component] very rich &gt;[low boiling component] rich &gt;[low boiling component] intermediate &gt;[low boiling component] lean  and conversely [high boiling component] lean &gt;[low boiling component] intermediate &gt;[low boiling component] rich &gt;[low boiling component] very rich . Energy is extracted from the intermediate working solution stream, which can be fully vaporized and generally superheated directly or can be formed from a rich fully vaporized and superheated working solution stream and a lean fully vaporized and superheated working solution stream. Excess thermal energy in the spent intermediate working solution stream is used to heat and help vaporizing the stream that become the fully vaporized and generally superheated intermediate working solution stream. The lean and very rich streams are formed by separating a partially condensed spent intermediate working solution stream. The very rich stream is combined with a portion of the lean stream to from the rich working solution stream which is then fully condensed after transferring heat to a fully condensed higher pressure rich working solution stream. The cooled rich working fluid stream is then fully condensed by an external coolant stream and pressurized to form the higher pressure, rich working solution stream. The lean stream is pressurized and either combined with a partially vaporized rich working solution stream and the combined stream forwarded to the RHRVG or sent directly into the RHRVG along side the rich working solution stream and combined after the two stream are fully vaporized and generally superheated. Where the RHRVG derives its thermal energy from a gas exhaust stream from an internal combustion power generator. 
         [0011]    The present invention provides a method for extracting an additional amount of power from a small internal combustion power generator including the step of passing an exhaust gas stream not exceed about 900° F. into a recuperative heat recovery vapor generator to produce a cooled exhaust stream and a fully vaporized, and in certain embodiments a superheated, multi-component stream. The fully vaporized and optionally superheated multi-component stream is then passed through a turbine or other similar energy conversion unit in which a portion of thermal energy in the stream is converted to a more useable form of energy such as electrical energy. The spent multi-component stream is then forwarded to a heat exchange, condensation and pressurization subsystem that converts the multi-component stream into a fully condensed multi-component stream which is then partially vaporized and passed into the recuperative heat recovery vapor generator. 
     
     
       BRIEF DESCRIPTION OF THE DRAWINGS 
         [0012]    The invention can be better understood with reference to the following detailed description together with the appended illustrative drawings in which like elements are numbered the same: 
           [0013]      FIG. 1  an embodiment of an apparatus or system of this invention including a condenser HE 1 , three recuperative heat exchangers HE 2 , HE 3  and HE 4 , a recuperative heat recovery vapor generator RHRVG, turbine T 1 , a separator S 1  and three pumps P 1 , P 2  and P 4 ; 
           [0014]      FIG. 2  an embodiment of an apparatus or system of this invention including a condenser HE 1 , two recuperative heat exchangers HE 2  and HE 3 , a recuperative heat recovery vapor generator RHRVG, turbine T 1 , a separator S 1  and three pumps P 1 , P 2  and P 4 . 
           [0015]      FIG. 3  an embodiment of an apparatus or system of this invention including a condenser HE 1 , three recuperative heat exchangers HE 2 , HE 3  and HE 4 , a vaporizing heat exchange system including two heat exchanger HE 5  and HE 6 , turbine T 1 , a separator S 1  and three pumps P 1 , P 2  and P 4 . 
       
    
    
     DETAILED DESCRIPTION OF THE INVENTION 
       [0016]    The inventors have found an apparatus, system and method can be devised for power generation from intermediated temperature waste heat as a heat source, such as the exhaust stream from small diesel power units. The apparatus includes a condenser HE 1 , two or three recuperative heat exchangers HE 2 , HE 3  and HE 4 , and a recuperative heat recovery vapor generator RHRVG, turbine T 1 , a separator S 1  and three pumps P 1 , P 2  and P 4 . The system is relatively simple and permits ready installation and effectively conversion of waste heat or thermal energy into a more useable form of energy such as electrical or mechanical. The bottoming cycle significantly improves the overall power generation capability of such small diesel or other internal combustion power generation units. 
         [0017]    The systems of this invention are designed for power generation using intermediate temperature waste heat as a heat source such as waste heat from smaller diesel power generation engines. The systems are designed to utilize heat sources with an initial temperature not more than or not to exceed about 900° F. producing an exhaust stream having a final temperature as low as 250° F. The systems are ideally designed for application to relatively small power units (up to 10 MW). A typical application of such a system is as a bottoming cycle to a diesel engine, using the exhaust stream of the diesel engine as the heat source. 
         [0018]    The systems of this invention are designed to use a mixture of at least two components as a working fluid, (hereafter referred to as the “low boiling” and “high boiling” components). In certain embodiments, the working fluid for the systems of this invention are a mixture of water and ammonia, but the system can operate using other components with the same efficacy. 
         [0019]    The working fluids suitable for use in the condensation apparatuses of this inventions is a multi-component fluid that comprises a lower boiling point material—the low boiling component—and a higher boiling point material—the high boiling component. The working fluid, a multi-component mixture of at least two components with different normal boiling temperatures. In the certain embodiments of the system, the mixture consists of water and ammonia, but other working fluids, such as a mixture of hydrocarbons, freons or other substances can be used as well. In other embodiments, the working fluids include, without limitation, an ammonia-water mixture, a mixture of two or more hydrocarbons, a mixture of two or more freons, a mixture of hydrocarbons and freons, or the like. In other embodiments, the working fluid comprises a mixture of water and ammonia. However, the fluid can comprise mixtures of any number of compounds with favorable thermodynamic characteristics and solubilities. 
         [0020]    The dividing valves used in this invention are well known in the art and are used to split streams into two or more substream, where the flow going into each stream being controlled by the exact construction of the dividing valve or by a control on the valve setting so that the flow rate is changeable to maintain the system. 
       DETAILED DESCRIPTION OF THE DRAWINGS 
       [0021]    Referring now to  FIG. 1 , a conceptual flow diagram of an embodiment of a system of this invention, generally  100 , is shown. The system  100  includes a condenser HE 1 , three recuperative heat exchangers HE 2 , HE 3  and HE 4 , a separator S 1 , three pump P 1 , P 2 , and P 4 , a recuperative heat recovery vapor generator RHRVG and a turbine T 1 . 
         [0022]    The system  100  operates as follows: 
         [0023]    A fully condensed basic, rich working solution stream S 10  (i.e., a working fluid with a high concentration of the low-boiling component) having parameters as at a point  1 , is pumped by a first pump P 1  to a desired higher pressure forming a higher pressure, rich working solution stream S 12  having parameters as at a point  2 . Thereafter, the stream S 12  having the parameters as at the point  2  passes through a second heat exchanger HE 2 , where it is heated in counterflow by a returning rich working solution stream S 14  having parameters as at a point  26  in a heat exchange process  2 - 3  or  26 - 27  as described below. As a result of the heat exchange process  26 - 27  or  2 - 3 , a heated, higher pressure, rich working solution stream S 16  having parameters as at a point  3 , corresponding to a state of saturated liquid is formed as well as a partially condensed rich working solution stream S 18  having parameters as at a point  27 . 
         [0024]    Thereafter, the stream S 16  having the parameters as at the point  3  enters into a third heat exchanger HE 3 , where it is partially vaporized in heat exchange process  3 - 5 - 8  or  20 - 15 - 14  by a first returning intermediate working solution stream S 20  having parameters as at a point  20  as described below forming a partially vaporized, higher pressure, rich working solution stream S 22  having parameters as at a point  8  and a partially condensed spent intermediate working solution stream S 24  having parameter as at a point  14 . The partially vaporized, higher pressure, rich working solution stream S 22  having the parameters as at the point  8  corresponds to a state of vapor-liquid mixture. 
         [0025]    Thereafter, the partially vaporized, higher pressure, rich working solution S 22  having the parameters as at the point  8  enters into a recuperative heat recovery vapor generator RHRVG, where it is fully vaporized and superheated in a heat exchange process  8 - 4 - 11 - 16  forming a higher pressure, superheated vapor, rich working solution stream S 26  having parameters as at a point  16 . The stream S 26  is a rich working solution stream having parameters consistent with a state of higher pressure, superheated vapor. 
         [0026]    Thereafter, the stream S 26  having the parameters as at the point  16  is mixed with a lean working solution stream S 28  having parameters as at a point  29 , as described below. As a result of this mixing an intermediate working solution stream S 30  having parameters as at a point  17  is formed. The stream S 30  having the parameters as at the point  17  then enters into a turbine T 1 , where it is expanded, producing power, and forming a spent intermediate working solution stream S 32  having parameters as at a point  18 . The stream S 32  having the parameters as at the point  18  is in a state of superheated vapor. 
         [0027]    Thereafter, the stream S 32  having the parameters as at the point  18  is sent back into the RHRVG, where it is cooled, transferring a portion of its heat or excess thermal energy to other streams in the RHRVG including a diesel exhaust gas stream E 10  having initial parameters as at a point  600  in a heat exchange process  601 - 602  as described below. After passing through the RHRVG, the stream S 32  having the parameters as at the point  18  is converted into a cooled spent intermediate working solution stream S 34  having parameters as at a point  19 . 
         [0028]    Thereafter, the stream S 34  having the parameters as at the point  19  is split into the returning intermediate working solution stream S 20  having the parameters as at the point  20  and a second returning intermediate working solution stream S 36  having parameters as at a point  12 . 
         [0029]    A major portion or the bulk of the stream S 34  having the parameters as at the point  19  is sent into the stream S 20  having the parameters as at the point  20 . The stream S 20  having the parameters as at the point  20  then passes through the third heat exchanger, HE 3  as described above, where it is de-superheated a heat exchange process  20 - 15  and then partially condensed in a heat exchange process  15 - 14 , providing heat for the heat exchange process  3 - 5 - 8  as described above. Thereafter, the stream S 20  having the parameters as at the point  20  exits HE 3  as the stream S 24  having the parameters as at the point  14  as described above. 
         [0030]    The other and smaller portion of the stream S 34  having the parameters as at the point  19  is sent into the stream S 36  having the parameters as at the point  12 . The stream S 36  having the parameters as at the point  12  is then forwarded through a fourth heat exchanger HE 4 . The stream S 36  having the parameters as at the point  12  is de-superheated in a heat exchange process  12 - 6  and then partially condensed in a heat exchange process  6 - 13  providing heat for a heat exchange process  9 - 7 - 10  as described below forming a partially condensed stream S 38  having parameters as at a point  13  and a partially vaporized, lean working solution stream S 40  having parameters as at a point  10 . 
         [0031]    Thereafter, the streams S 24  and S 38  having the parameters as at the points  14  and  13 , respectively, are combined, forming a combined intermediate working solution stream S 42  having parameters as at a point  21 , which is in a state of a vapor-liquid mixture. The stream S 40  having the parameters as at the point  21  then enters into a gravity separator S 1 , where it is separated into a very rich saturated vapor stream S 44  having parameters as at a point  22  and a lean liquid stream S 46  having parameters as at a point  23 . 
         [0032]    The lean liquid stream S 46  having the parameters as at the point  23 , is then divided into two substreams S 48  and S 50  with parameters as at points  24  and  25 , respectively. Thereafter, the stream S 50  having the parameters as at the point  25  is combined with the very rich vapor stream S 44  having the parameters as at the point  22  as described above, forming the rich working solution stream S 14  having the parameters as at the point  26 . 
         [0033]    The stream S 14  having the parameters as at the point  26  then passes through the second heat exchanger HE 2 , where it is partially condensed, forming the stream S 18  having the parameters as at the point  27 , and providing heat for the heat exchange process  2 - 3  as described above. The stream S 18  having the parameters as at the point  27  is then sent into a first heat exchanger or condenser HE 1 , where it fully condensed, in counterflow with a coolant stream C 12  having parameters as at a point  51  comprising water or air in a heat exchange process  51 - 52  or  27 - 1  as described below. After heat exchange, the rich working solution stream S 18  is converted into the fully condensed, rich working solution stream S 10  having the parameters as at the point  1  as described above and a spent coolant stream C 14  having parameters as at a point  52 . 
         [0034]    The coolant stream C 12  having parameters as at the point  51  is formed from a coolant stream Cd 0  having initial parameters as at a point  50  by passed the coolant stream C 10  through a pump P 4  to increased its pressure and forming the coolant stream C 12  having the parameters as at the point  51 . When the coolant stream C 12  is air, then the pump P 4  is replace by a fan. 
         [0035]    Meanwhile, the stream S 48  having the parameters as at the point  24  as described above enters into a second or recirculating pump P 2 , where it is pumped to a required higher pressure, to from a higher pressure lean working solution stream S 52  having parameters as at point  9 . Thereafter, the stream S 52  having the parameters as at the point  9  is sent into the fourth heat exchanger HE 4 , where it is heated in the heat exchange process  9 - 7 - 10 , utilizing heat from the heat exchange process  12 - 6 - 13  as described above, forming the stream S 40  having the parameters as at the point  10 , where the parameters correspond to a state of subcooled liquid. 
         [0036]    The stream S 40  having the parameters as at the point  10  is then sent into the RHRVG, where it is heated, fully vaporized and superheated in a heat exchange process  10 - 30 - 31 - 29 , exiting the RHRVG as the stream S 28  having the parameters as at the point  29 . The stream S 28  having the parameters as at the point  29  is then mixed with stream S 26  having the parameters as at the point  16 , forming the stream S 30  having the parameter as at the point  17  as described above. 
         [0037]    Meanwhile, the stream E 10  of hot exhaust gas with initial parameters as at point  600  is sent into the RHRVG, in counterflow to streams S 40  having the parameter as at the point  10  and the stream S 22  having the parameter as at the point  8 , where it is cooled, in a heat exchange process  600 - 605 - 601 - 602 , proving heat for the heat exchanges processes  10 - 30 - 31 - 29  and  8 - 4 - 11 - 16 , to form a spent exhaust stream E 12  having parameters as at a point  602 , which is sent into a stack or other venting apparatus. 
         [0038]    The process is closed with respect to the working solution stream. 
         [0039]    In the embodiment of  FIG. 1 , the returning streams S 32  and S 34  having the parameters as at the points  18  and  19  move in counterflow with the streams S 22  and S 40  having the parameters as at the points  8  and  10 , and in parallel flow with the exhaust gas stream E 10  at the points  601  and  602 . While the exhaust gas stream E 10  in the heat exchange process  601 - 602  is cooled by the streams S 22  and S 40  having the parameters as at the points  8  and  10 , it is at the same time heated by stream S 32  having the parameters as at the point  18 . This recuperative heating has an effect that is the equivalent of increasing a flow rate of gas in stream E 10  at the points  601  and  602 . 
         [0040]    Referring now to  FIG. 2 , a flow diagram of a simplified version of the system of  FIG. 1  is presented. In the simplified version, the recuperative heat exchanger HE 4  is eliminated. Thus, the stream S 52  having the parameters as at the point  9  is not preheated. Instead, the stream S 52  having the parameters as at the point  9  is mixed with the stream S 22  having the parameters as at the point  8 , forming the intermediate solution stream S 40  with the parameters as at the point  10  before entering into the RHRVG. 
         [0041]    This simplified version of the proposed system has a reduced power output by approximately 4%. 
         [0042]    Referring now to  FIG. 3 , a flow diagram of another simplified version of the system of  FIG. 2 , where the RHRVG, if not desirable, (e.g., the heat source stream is a liquid), then the RHRVG can be replaced by three separate heat exchangers (HE 4 , HE 5 , and HE 6 ). In this case, the stream S 40  is split into the stream S 36  having the parameters as at the point  12  and a new stream S 54  having parameters as at a point  11  which is sent through the fourth heat exchanger HE 4  to form the stream S 38  having parameters as at the point  13 . 
         [0043]    The systems of this invention, utilizing intermediate temperature heat sources, provide a power output which is approximately 15% higher, for a given heat source, than the output of a conventional Rankine cycle used for the same purposes and with the same constraints. 
         [0044]    It has been calculated that if used with the exhaust from a 3 MW (megawatt) diesel engine as a heat source, the systems of this invention would produce a net output of 840 kW, or 810 kW for the simplified version. This corresponds to a 28% increase in power output from the diesel engine when combined with the systems of this invention. 
         [0045]    The typical parameters of the state points of the proposed system (as shown in  FIG. 1 ) are presented in Table 1. 
         [0000]    
       
         
               
             
               
               
               
               
               
               
               
               
               
               
               
             
               
             
               
               
               
               
               
               
               
               
               
               
               
             
               
             
               
               
               
               
               
               
               
               
               
               
               
             
           
               
                 TABLE 1 
               
               
                   
               
               
                 System Point Summary 
               
               
                   
               
             
             
               
                 Working Fluid 
               
             
          
           
               
                   
                 X 
                 T 
                 P 
                 H 
                 S 
                 Ex 
                 Grel 
                 Gabs 
                   
                 Wetness/T 
               
               
                 Pt. 
                 kg/kg 
                 ° C. 
                 bar 
                 kJ/kg 
                 kJ/kg-K 
                 kJ/kg 
                 G/G = 1 
                 kg/s 
                 Ph. 
                 (kg/kg)/° C. 
               
               
                   
               
               
                  1 
                 0.9300 
                 20.99 
                 8.228 
                 42.84 
                 0.3214 
                 141.39 
                 1.00000 
                 1.799 
                 Mix 
                 1 
               
               
                  2 
                 0.9300 
                 22.13 
                 49.016 
                 50.55 
                 0.3259 
                 147.81 
                 1.00000 
                 1.799 
                 Liq 
                 −70.46° C. 
               
               
                  3 
                 0.9300 
                 91.87 
                 48.327 
                 404.38 
                 1.3987 
                 196.89 
                 1.00000 
                 1.799 
                 Mix 
                 1 
               
               
                  4 
                 0.9300 
                 166.54 
                 47.983 
                 1,629.70 
                 4.6038 
                 511.66 
                 1.00000 
                 1.799 
                 Vap 
                 17.9° C. 
               
               
                  5 
                 0.9300 
                 123.92 
                 48.217 
                 1,317.90 
                 3.8479 
                 414.59 
                 1.00000 
                 1.799 
                 Mix 
                 0.1182 
               
               
                  6 
                 0.7433 
                 126.70 
                 8.614 
                 1,838.16 
                 5.7508 
                 392.31 
                 0.09023 
                 0.162 
                 Mix 
                 0 
               
               
                  7 
                 0.3009 
                 123.92 
                 48.217 
                 354.09 
                 1.5222 
                 104.95 
                 0.42209 
                 0.759 
                 Liq 
                 −60.85° C. 
               
               
                  8 
                 0.9300 
                 132.72 
                 48.189 
                 1,402.50 
                 4.0588 
                 439.27 
                 1.00000 
                 1.799 
                 Mix 
                 0.0776 
               
               
                  9 
                 0.3009 
                 95.59 
                 48.327 
                 220.57 
                 1.1733 
                 70.54 
                 0.42209 
                 0.759 
                 Liq- 
                 89.34° C. 
               
               
                 10 
                 0.3009 
                 126.75 
                 48.189 
                 367.66 
                 1.5562 
                 108.85 
                 0.42209 
                 0.759 
                 Liq 
                 −57.98° C. 
               
               
                 11 
                 0.9300 
                 184.61 
                 47.959 
                 1,686.16 
                 4.7298 
                 532.30 
                 1.00000 
                 1.799 
                 Vap 
                 36° C. 
               
               
                 12 
                 0.7433 
                 152.72 
                 8.642 
                 1,901.68 
                 5.9032 
                 412.52 
                 0.09023 
                 0.162 
                 Vap 
                 25.9° C. 
               
               
                 13 
                 0.7433 
                 98.86 
                 8.504 
                 1,213.62 
                 4.1449 
                 223.98 
                 0.09023 
                 0.162 
                 Mix 
                 0.2727 
               
               
                 14 
                 0.7433 
                 94.65 
                 8.504 
                 1,152.27 
                 3.9791 
                 209.74 
                 1.33186 
                 2.396 
                 Mix 
                 0.2985 
               
               
                 15 
                 0.7433 
                 126.70 
                 8.614 
                 1,838.16 
                 5.7508 
                 392.31 
                 1.33186 
                 2.396 
                 Mix 
                 0 
               
               
                 16 
                 0.9300 
                 349.64 
                 47.500 
                 2,161.41 
                 5.6218 
                 754.15 
                 1.00000 
                 1.799 
                 Vap 
                 201.4 C. 
               
               
                 17 
                 0.7433 
                 350.00 
                 47.500 
                 2,344.37 
                 5.9689 
                 836.55 
                 1.42209 
                 2.559 
                 Vap 
                 158.9° C. 
               
               
                 18 
                 0.7433 
                 187.86 
                 8.849 
                 1,986.06 
                 6.0826 
                 445.95 
                 1.42209 
                 2.559 
                 Vap 
                 60.3° C. 
               
               
                 19 
                 0.7433 
                 152.72 
                 8.642 
                 1,901.68 
                 5.9032 
                 412.52 
                 1.42209 
                 2.559 
                 Vap 
                 25.9° C. 
               
               
                 20 
                 0.7433 
                 152.72 
                 8.642 
                 1,901.68 
                 5.9032 
                 412.52 
                 1.33186 
                 2.396 
                 Vap 
                 25.9° C. 
               
               
                 21 
                 0.7433 
                 94.92 
                 8.504 
                 1,156.16 
                 3.9897 
                 210.63 
                 1.42209 
                 2.559 
                 Mix 
                 0.2968 
               
               
                 22 
                 0.9300 
                 94.92 
                 8.504 
                 1,553.56 
                 5.1797 
                 271.89 
                 0.99997 
                 1.799 
                 Mix 
                 0 
               
               
                 23 
                 0.3009 
                 94.92 
                 8.504 
                 214.75 
                 1.1705 
                 65.52 
                 0.42212 
                 0.759 
                 Mix 
                 1 
               
               
                 24 
                 0.3009 
                 94.92 
                 8.504 
                 214.75 
                 1.1705 
                 65.52 
                 0.42209 
                 0.759 
                 Mix 
                 1 
               
               
                 25 
                 0.3009 
                 94.92 
                 8.504 
                 214.75 
                 1.1705 
                 65.52 
                 0.00003 
                 0.000 
                 Mix 
                 1 
               
               
                 26 
                 0.9300 
                 94.92 
                 8.504 
                 1,553.46 
                 5.1794 
                 271.87 
                 1.00000 
                 1.799 
                 Mix 
                 0.0001 
               
               
                 27 
                 0.9300 
                 54.39 
                 8.366 
                 1,199.62 
                 4.1750 
                 203.39 
                 1.00000 
                 1.799 
                 Mix 
                 0.1321 
               
               
                 29 
                 0.3009 
                 350.00 
                 47.500 
                 2,777.83 
                 6.4568 
                 1,126.79 
                 0.42209 
                 0.759 
                 Vap 
                 111.4° C. 
               
               
                 30 
                 0.3009 
                 166.54 
                 48.133 
                 564.29 
                 2.0248 
                 172.37 
                 0.42209 
                 0.759 
                 Liq 
                 −18.12° C. 
               
               
                 31 
                 0.3009 
                 184.61 
                 48.106 
                 658.39 
                 2.2345 
                 206.89 
                 0.42209 
                 0.759 
                 Mix 
                 1 
               
               
                   
               
             
          
           
               
                 Heat Source 
               
             
          
           
               
                   
                 X 
                 T 
                 P 
                 H 
                 S 
                 Ex 
                 Grel 
                 Gabs 
                   
                 Wetness/T 
               
               
                 Pt. 
                 kg/kg 
                 C. 
                 bar 
                 kJ/kg 
                 kJ/kg-K 
                 kJ/kg 
                 G/G = 1 
                 kg/s 
                 Ph. 
                 (kg/kg)/° C. 
               
               
                   
               
               
                 600  
                 GAS 
                 440.00 
                 1.082 
                 671.96 
                 1.8029 
                 205.12 
                 4.96643 
                 8.936 
                 Vap 
                 389.8° C. 
               
               
                 601  
                 GAS 
                 177.86 
                 1.076 
                 376.77 
                 1.2899 
                 55.69 
                 4.96643 
                 8.936 
                 Vap 
                 127.8° C. 
               
               
                 602  
                 GAS 
                 142.72 
                 1.075 
                 338.47 
                 1.2017 
                 42.44 
                 4.96643 
                 8.936 
                 Vap 
                 92.7° C. 
               
               
                 605  
                 GAS 
                 195.54 
                 1.076 
                 396.13 
                 1.3319 
                 63.12 
                 4.96643 
                 8.936 
                 Vap 
                 145.4° C. 
               
               
                 614  
                 GAS 
                 142.72 
                 1.075 
                 338.47 
                 1.2017 
                 42.44 
                 8.09982 
                 14.573 
                 Vap 
                 92.7° C. 
               
               
                 615  
                 GAS 
                 142.72 
                 1.075 
                 338.47 
                 1.2017 
                 42.44 
                 3.13340 
                 5.638 
                 Vap 
                 92.7° C. 
               
               
                 616  
                 GAS 
                 177.86 
                 1.076 
                 376.77 
                 1.2899 
                 55.69 
                 3.13340 
                 5.638 
                 Vap 
                 127.8° C. 
               
               
                 617  
                 GAS 
                 177.86 
                 1.076 
                 376.77 
                 1.2899 
                 55.69 
                 8.09982 
                 14.573 
                 Vap 
                 127.8° C. 
               
               
                 620  
                 GAS 
                 440.00 
                 1.082 
                 671.96 
                 1.8029 
                 205.12 
                 1.72304 
                 3.100 
                 Vap 
                 389.8° C. 
               
               
                 621  
                 GAS 
                 195.54 
                 1.076 
                 396.13 
                 1.3319 
                 63.12 
                 1.72304 
                 3.100 
                 Vap 
                 145.4° C. 
               
               
                 622  
                 GAS 
                 440.00 
                 1.082 
                 671.96 
                 1.8029 
                 205.12 
                 3.24339 
                 5.836 
                 Vap 
                 389.8° C. 
               
               
                 623  
                 GAS 
                 195.54 
                 1.076 
                 396.13 
                 1.3319 
                 63.12 
                 3.24339 
                 5.836 
                 Vap 
                 145.4° C. 
               
               
                 624  
                 GAS 
                 195.54 
                 1.076 
                 396.13 
                 1.3319 
                 63.12 
                 2.05102 
                 3.690 
                 Vap 
                 145.4° C. 
               
               
                 625  
                 GAS 
                 177.86 
                 1.076 
                 376.77 
                 1.2899 
                 55.69 
                 2.05102 
                 3.690 
                 Vap 
                 127.8° C. 
               
               
                 626  
                 GAS 
                 177.86 
                 1.076 
                 376.77 
                 1.2899 
                 55.69 
                 2.16714 
                 3.899 
                 Vap 
                 127.8° C. 
               
               
                 627  
                 GAS 
                 142.72 
                 1.075 
                 338.47 
                 1.2017 
                 42.44 
                 2.16714 
                 3.899 
                 Vap 
                 92.7° C. 
               
               
                 628  
                 GAS 
                 177.86 
                 1.076 
                 376.77 
                 1.2899 
                 55.69 
                 5.93269 
                 10.674 
                 Vap 
                 127.8° C. 
               
               
                 629  
                 GAS 
                 142.72 
                 1.075 
                 338.47 
                 1.2017 
                 42.44 
                 5.93269 
                 10.674 
                 Vap 
                 92.7° C. 
               
               
                 630  
                 GAS 
                 195.54 
                 1.076 
                 396.13 
                 1.3319 
                 63.12 
                 2.91541 
                 5.245 
                 Vap 
                 145.4° C. 
               
               
                 631  
                 GAS 
                 177.86 
                 1.076 
                 376.77 
                 1.2899 
                 55.69 
                 2.91541 
                 5.245 
                 Vap 
                 127.8° C. 
               
               
                   
               
             
          
           
               
                 Coolant 
               
             
          
           
               
                   
                 X 
                 T 
                 P 
                 H 
                 S 
                 Ex 
                 Grel 
                 Gabs 
                   
                 Wetness/T 
               
               
                 Pt. 
                 kg/kg 
                 ° C. 
                 bar 
                 kJ/kg 
                 kJ/kg-K 
                 kJ/kg 
                 G/G = 1 
                 kg/s 
                 Ph. 
                 (kg/kg)/° C. 
               
               
                   
               
               
                 50 
                 Water 
                 10.94 
                 1.013 
                 46.08 
                 0.1650 
                 0.10 
                 18.9053 
                 34.015 
                 Liq 
                 −89.03° C. 
               
               
                 51 
                 Water 
                 10.99 
                 1.703 
                 46.35 
                 0.1658 
                 0.17 
                 18.9053 
                 34.015 
                 Liq 
                 −104.21° C. 
               
               
                 52 
                 Water 
                 25.63 
                 1.013 
                 107.54 
                 0.3760 
                 1.63 
                 18.9053 
                 34.015 
                 Liq 
                 −74.35° C. 
               
               
                   
               
             
          
         
       
     
         [0046]    The state point in table which are not shown in  FIG. 1  are “virtual points” used in the computational process. 
         [0047]    A summary is performance and power output for the system shown in  FIG. 1  is presented in Table 2. 
         [0000]    
       
         
               
             
               
               
               
               
               
             
               
               
               
             
               
             
           
               
                 TABLE 2 
               
               
                   
               
               
                 Plant Performance Summary 
               
               
                   
               
             
             
               
                   
               
             
          
           
               
                 Heat in 
                 2,979.88 
                 kW 
                 1,656.22 
                 kJ/kg 
               
               
                 Heat rejected 
                 2,081.29 
                 kW 
                 1,156.78 
                 kJ/kg 
               
               
                 Turbine enthalpy Drops 
                 916.78 
                 kW 
                 509.55 
                 kJ/kg 
               
               
                 Gross Generator Power 
                 874.19 
                 kW 
                 485.88 
                 kJ/kg 
               
               
                 Process Pumps (−10.16) 
                 −19.66 
                 kW 
                 −10.93 
                 kJ/kg 
               
               
                 Cycle Output 
                 854.53 
                 kW 
                 474.95 
                 kJ/kg 
               
               
                 Other Pumps and Fans (−5.21) 
                 −10.07 
                 kW 
                 −5.60 
                 kJ/kg 
               
               
                 Net Output 
                 844.46 
                 kW 
                 469.35 
                 kJ/kg 
               
               
                 Gross Generator Power 
                 874.19 
                 kW 
                 485.88 
                 kJ/kg 
               
               
                 Cycle Output 
                 854.53 
                 kW 
                 474.95 
                 kJ/kg 
               
               
                 Net Output 
                 844.46 
                 kW 
                 469.35 
                 kJ/kg 
               
             
          
           
               
                 Net thermal efficiency 
                 28.34%% 
                   
               
               
                 Second Law Limit 
                 48.78%% 
               
               
                 Second Law Efficiency 
                 58.09%% 
               
             
          
           
               
                 Overall Heat Balance kJ/kg 
               
               
                 Heat In: Source + pumps = 1,656.22 + 10.16 = 1,666.39 
               
               
                 Heat Out: Turbines + condenser = 509.55 + 1,156.78 = 1,666.33 
               
               
                   
               
             
          
         
       
     
         [0048]    All references cited herein are incorporated by reference. Although the invention has been disclosed with reference to its preferred embodiments, from reading this description those of skill in the art may appreciate changes and modification that may be made which do not depart from the scope and spirit of the invention as described above and claimed hereafter.