US20070144195A1

US20070144195A1 - Method and apparatus for combining a heat pump cycle with a power cycle

Info

Publication number: US20070144195A1
Application number: US11/203,783
Authority: US
Inventors: George Mahl
Original assignee: Individual
Current assignee: Individual
Priority date: 2004-08-16
Filing date: 2005-08-15
Publication date: 2007-06-28
Also published as: US20160032785A1; US20140053556A1; US20110308250A1

Abstract

Method and Apparatus for Combining a Heat Pump Cycle With A Power Cycle. The working fluid for the heat pump cycle will be different than that for the power cycle.

Description

CROSS-REFERENCE TO RELATED APPLICATIONS

Priority is claimed to both U.S. Provisional Patent Application Ser. No. 60/602,270, filed Aug. 16, 2004 and U.S. Provisional Patent Application Ser. No. 60/604,663, filed Aug. 26, 2004, both of which are incorporated herein by reference.

STATEMENT REGARDING FEDERALLY SPONSORED RESEARCH OR DEVELOPMENT

Not applicable

REFERENCE TO A “MICROFICHE APPENDIX”

Not applicable

BACKGROUND

1. Field
The present invention relates to cycles. More particularly, the present invention relates to a method and apparatus for combining a power cycle with a refrigeration cycle or heat pump.
2. General Background
A general vapor power cycle can include a boiler, turbine, condenser and a pump. FIG. 1 shows a general power cycle. From “a” to “b” subcooled fluid can be heated to the saturated fluid temperature in the boiler. From “b” to “c” saturated fluid can be vaporized in the boiler, producing saturated gas. From “c” to “d” a superheater option can be used to increase the fluid temperature while maintaining pressure. From “d” to “e” vapor expands through a turbine and does work as it decreases in temperature, pressure, and quality. From “e” to “f” vapor is liquified in the condenser. From f to a liquid is brought up to the boiler pressure. The expansion process between states d and e is essentially adiabatic. Ideal turbine expansion also is isentropic.
The Carnot cycle is an ideal power cycle which is stated to set the maximum attainable work output from a power cycle or heat engine. Various property diagrams for a Carnot cycle are provided in FIGS. 2A through 2C. FIG. 2A shows a pressure-volume diagram. FIG. 2B shows a temperature-entropy diagram. FIG. 2C shows an enthalpy-entropy diagram. From “a” to “b” occurs isothermal expansion of a saturated fluid to a saturated gas. From “b” to “c” occurs isentropic expansion. From “c” to “d” occurs isothermal condensation. From “d” to “a” occurs isentropic compression. The thermal efficiency of the entire cycle is calculated by the following formula: $n_{th} = \frac{T_{high} - T_{low}}{T_{high}}$
Refrigeration cycles are essentially power cycles in reverse. FIG. 3 is a schematic diagram of a refrigeration cycle. It is necessary to do work on the refrigerant in order to have it discharge energy, Q_H, to a high temperature sink. After discharging energy to the high temperature heat sink the refrigerant is expanded through an expansion valve to drop its temperature allowing it to absorb energy, Q_L, from a low temperature heat source. A heat pump also operates on a refrigeration cycle. One difference between a refrigerator and a heat pump is the purpose of each. The refrigerator's main purpose is to cool a low temperature area and to reject the absorbed heat to a high temperature area. The heat pump's main purpose is to reject the absorbed heat to a high temperature area, having picked up that heat from a low temperature area. Heat pumps use energy more efficiently than resistance heaters. For each kilowatt of energy used by the compressor of a heat pump, one kilowatt of compression heat is produced plus heat picked up through a refrigeration effect. The refrigeration effect of the heat pump can vary from ten to as high as five hundred percent or higher of the energy input into the compressor. This refrigeration effect is dependent on the temperatures involved and fluid used.
Up to this point it was believed that the Carnot cycle was the most efficient power cycle that could be used. However, this belief did not consider a refrigeration/heat pump cycle being combined with a power cycle. No one has used a refrigeration cycle or heat pump as a heat source in a power cycle.
While certain novel features of this invention shown and described below are pointed out in the annexed claims, the invention is not intended to be limited to the details specified, since a person of ordinary skill in the relevant art will understand that various omissions, modifications, substitutions and changes in the forms and details of the device illustrated and in its operation may be made without departing in any way from the spirit of the present invention. No feature of the invention is critical or essential unless it is expressly stated as being “critical” or “essential.”

BRIEF SUMMARY

The apparatus of the present invention solves the problems confronted in the art in a simple and straightforward manner. What is provided is an original process for the removal and use of energy from the ambient environment, including air, water, or earth. This energy is removed in the form of mechanical motion such as work, which may be used either directly or to drive electrical generators, or supply other energy needs.
In one embodiment the process can consist of a combined refrigeration/power cycle. A first media (Media No. 1) can be vaporized at ambient temperatures, compressed, and condensed at a higher temperature, T_H, in a first heat exchanger. This portion of the method and apparatus can be a cycle similar to conventional heat pumps.
The refrigeration/heat pump cycle can be combined with a second cycle in which a second media (Media No. 2) is vaporized at the higher temperature, T_H. Energy can then be extracted from Media No. 2 by flowing it through a mechanical drive turbine or other engine, then condensing Media No. 2 at ambient temperature in the condenser.
The heat pump cycle using Media No. 1 produces a quantity of available energy at T_Hequal to the energy of evaporation of Media No. 1 at ambient temperature plus the energy of compression of Media No. 1. Thus, the energy available at T_Hcompared to the input of mechanical energy is:
E@T _H =E Evap.+E Mech. Input
The ratio of E@T_Hto E Mechanical Input depends upon the thermodynamic properties of Media No. 1, the ambient temperature and condensation temperature, T_Hat which the cycle is operating.
The second portion of this process is the cycle of Media No. 2. Media No. 2 is evaporated in Heat Exchanger No. 1 at T_Hby the condensation of Media No. 1. Media No. 2 is then passed through a turbine or other engine where mechanical energy is removed, then condensed at ambient temperature in the condenser. The energy of Media No. 2 available for transformation into mechanical energy is the difference of the energy of:
1. Heating, evaporating and superheating of Media No. 2 in the Heat Exchanger No. 1, and:
2. The energy of condensation of Media No. 1 at ambient temperature in the condenser, or;
Available Energy=E(Heat Exchanger No. 1)−E(Condensation at condenser).
The theoretical output of the process is then determined by the product of: $\frac{E @ T_{H}}{E Mech . Input}$
of Cycle No. 1 and the per unit available energy of Cycle No. 2. If the media for Cycle No. 1 and Cycle No. 2 and operating temperatures are properly selected such that the ratio of $\frac{E @ T_{H}}{E Mech . Input}$
of Cycle No. 1 is maximized and the available energy of Cycle No. 2 is maximized, then the theoretical mechanical output to mechanical input ratio exceeds unity. Thus, there is a net flow of energy from the ambient environment, which is converted into mechanical energy.
The drawings constitute a part of this specification and include exemplary embodiments to the invention, which may be embodied in various forms.

BRIEF DESCRIPTION OF THE SEVERAL VIEWS OF THE DRAWINGS

For a further understanding of the nature, objects, and advantages of the present invention, reference should be had to the following detailed description, read in conjunction with the following drawings, wherein like reference numerals denote like elements and wherein:
FIG. 1 is a schematic diagram of a power cycle.
FIGS. 2A through 2C are schematic diagrams of various diagrams of the properties in a Carnot cycle.
FIG. 3 is a schematic diagram of a refrigeration cycle.
FIG. 4 is a schematic diagram of a preferred embodiment of the invention.
FIG. 5 is a pressure-enthalpy diagram for R11.
FIG. 6 is a pressure-enthalpy diagram for R600.

DETAILED DESCRIPTION

Detailed descriptions of one or more preferred embodiments are provided herein. It is to be understood, however, that the present invention may be embodied in various forms. Therefore, specific details disclosed herein are not to be interpreted as limiting, but rather as a basis for the claims and as a representative basis for teaching one skilled in the art to employ the present invention in any appropriate system, structure or manner.
FIG. 4 is a schematic diagram of a preferred embodiment 10. In this embodiment a heat pump cycle 20 is used as the heat source for a power cycle 30. Heat pump cycle 20 can comprise expansion valve 60, evaporator 70, compressor 40, and a condenser. The condenser can be heat exchanger 50. Power cycle 30 can comprise engine 80, condenser 90, pump 100, and a heat source or boiler. The heat source or boiler can also be heat exchanger 50.
In heat pump cycle 20, a first media (Media No. 1) can be vaporized at ambient temperatures, compressed, and condensed at a higher temperature, T_H, in heat exchanger 50.
Heat pump cycle 20 is combined with a second cycle 30 in which a second media (Media No. 2) is vaporized at the higher temperature, T_H. Energy can then be extracted from Media No. 2 by flowing it through a mechanical drive turbine or other engine 80, then condensing Media No. 2 at ambient temperature in condenser 90.
Heat pump cycle 20 using Media No. 1 produces a quantity of available energy at T_Hequal to the energy of evaporation of Media No. 1 at ambient temperature plus the energy of compression of Media No. 1. Thus, the energy available at T_Hcompared to the input of mechanical energy is:
E@T _H =E Evap.+E Mech. Input
The ratio of E@T_Hto E Mechanical Input depends upon the thermodynamic properties of Media No. 1, the ambient temperature and condensation temperature, T_Hat which the cycle is operating.
The second portion of this process is power cycle 30 using Media No.2. Media No.2 can be evaporated in heat exchanger 50 at T_Hby the condensation of Media No. 1 of cycle 20. Media No. 2 is then passed through turbine or other engine 80 where mechanical energy is removed, then condensed at ambient temperature in condenser 90. The energy of Media No. 2 available for transformation into mechanical energy is the difference of the energy of:
1. Heating, evaporating and superheating of Media No.2 in heat exchanger 50, and:
2. The energy of condensation of Media No. 1 at ambient temperature in condenser 90, or;
Available Energy=E(heat exchanger 50)−E(Condensation at condenser 90).
The theoretical output of overall process 10 is then determined by the product of: $\frac{E @ T_{H}}{E Mech . Input} of Cycle No . 1 (cycle 20) \times \begin{matrix} the per unit available \\ energy of Cycle \\ No . 2 (cycle 30) . \end{matrix}$
If the media for Cycle No. 1 and Cycle No. 2 and operating temperatures are properly selected such that the ratio of $\frac{E @ T_{H}}{E Mech . Input}$
of Cycle No. 1 (cycle 20) is maximized and the available energy of Cycle No. 2 (cycle 30) is maximized, then the theoretical mechanical output to mechanical input ratio exceeds unity for overall cycle 10. Thus, there is a net flow of energy from the ambient environment, which is converted into mechanical energy.
One example of a preferred embodiment 10 using specific fluids is shown in FIG. 4. This system uses refrigerant No. R11 as the media of Cycle No. 1 (cycle 20), evaporating at an ambient temperature of 70° F. and condensing in heat exchanger 50 at 190° F. Refrigerant R600 is used in Cycle No. 2 (cycle 30), evaporating in heat exchanger 50 and condensing at the ambient temperature of 70° F.
Cycle 20 shows refrigerant entering expansion valve 60 at 70° F., at a pressure of 90 pounds per square inch, and having a heat content of 22.4 BTUs per pound. After passing through expansion valve 60 the refrigerant is at a pressure of 13.39 pounds per square inch and maintain a heat content of 22.4 BTUs per pound. It should be noted that depending on the refrigerant used, an expansion turbine may be used in place of expansion valve 60 to enhance performance of the overall process. Next, the refrigerant enters evaporator 70. Fed into evaporator 70 can be water at 70° F. having a heat capacity of 78.3 BTUs per pound (or 166.2 BTUs per minute). The refrigerant leaves evaporator 70 at 70° F., at a pressure of 13.39 pounds per square inch, and having a heat content of 100.72 BTUs per pound. Next the refrigerant is compressed by compressor 40 which can require an input energy of 142 BTUs per pound (or 30.146 BTUs per minute). The refrigerant leaves compressor 40 at 200° F., at a pressure of 90 pounds per square inch, and having a heat content of 114.9 BTUs per pound. Finally, the refrigerant passing through heat exchanger 50 where it absorbs heat and leaves at 70° F., at a pressure of 90 pounds per square inch, and having a heat content of 22.4 BTUs per pound. The heat loss by the working fluid in heat exchanger 50 can be 92.5 BTUs per pound (or 196.37 BTUs per minute).
Cycle 30 shows a working fluid entering engine 80 (which can be a turbine) at 190° F., at a pressure of 173.25 pounds per square inch, and having a heat content of 256.374 BTUs per pound. Leaving engine 80 the working fluid can be at 70° F., at a pressure of 31.279 pounds per square inch, and having a heat content of 217.017 BTUs per pound. The mechanical output of engine 80 can be 39.357 BTUs per pound or 39.357 BTUs per minute. Next, the working fluid can enter condenser 90 and leave at 70° F., at a pressure of 31.279 pounds per square inch, and having a heat content of 59.867 BTUs per pound. To achieve such a change in properties of the working fluid water at 70° F. can be fed through condenser 90 and exiting at 157.15 BTUs per pound (or 157.15 BTUs per minute). Next, the working fluid is pumped by pump 100 and leaves at 70° F., at a pressure of 194.09 pounds per square inch, and having a heat content of 60.22 BTUs per pound. The mechanical input to pump 100 can be 0.3618 BTUs per pound or 0.3618 BTUs per minute. Next, the working fluid enters heat exchanger 50 and exits at 190° F., at a pressure of 173.25 pounds per square inch, and having a heat content of 256.374 BTUs per pound. The heat gain for the working fluid entering heat exchanger 50 can be 196.154 BTUs per pound (or 196.154 BTUs per minute).

The working fluid for cycle 20 can be R11. The working fluid for cycle 30 can be R600. The ratios of flow rates for R11 to R600 can be 2.123 to 1. For example, the flow rate of R11 can be 2.123 pounds per minute and the flow rate of R600 can be 1 pound per minute. FIG. 5 is a pressure-enthalpy diagram for R11. FIG. 6 is a pressure-enthalpy diagram for R600. In both FIGS. 5 and 6 pressure is on the y-axis and enthalpy is on the x-axis. Tables 1A and 1B list various thermophysical properties for R11. Tables 2A and 2B list various thermophysical properties for R600.

TABLE 1A


Refrigerant 11 (Trichlorofluoromethane) Properties of Saturated Liquid and Saturated Vapor

		Density,	Volume,	Enthalpy,	Entropy,	Specific Heat c_p,
Temp,*	Pressure,	lb/ft³	ft³/lb	Btu/lb	Btu/lb · ° F.	Btu/lb · ° F.

° F.	psia	Liquid	Vapor	Liquid	Vapor	Liquid	Vapor	Liquid	Vapor

−166.85a	0.001	110.41	24230.	−24.922	73.328	−0.07085	0.26467	—	0.1005
−160.00	0.002	109.93	14650.	−23.116	74.019	−0.06474	0.25940	0.1840	0.1019
−150.00	0.003	109.23	7355.6	−21.267	75.045	−0.05867	0.25235	0.1860	0.1038
−140.00	0.006	108.52	3882.0	−19.398	76.088	−0.05273	0.24597	0.1878	0.1058
−130.00	0.012	107.81	2143.2	−17.511	77.149	−0.04692	0.24022	0.1894	0.1077
−120.00	0.022	107.09	1232.5	−15.610	78.226	−0.04123	0.23502	0.1909	0.1095
−110.00	0.037	106.37	735.62	−13.694	79.318	−0.03568	0.23032	0.1922	0.1114
−100.00	0.062	105.65	454.14	−11.767	80.425	−0.03024	0.22608	0.1933	0.1133
−90.00	0.100	104.92	289.15	−9.829	81.546	−0.02493	0.22225	0.1943	0.1151
−80.00	0.156	104.19	189.37	−7.880	82.681	−0.01973	0.21880	0.1953	0.1170
−70.00	0.239	103.46	127.27	−5.923	83.827	−0.01464	0.21568	0.1962	0.1188
−60.00	0.355	102.73	87.583	−3.957	84.986	−0.00966	0.21288	0.1970	0.1206
−50.00	0.517	101.99	61.601	−1.983	86.155	−0.00478	0.21036	0.1978	0.1225
−40.00	0.738	101.25	44.203	0.000	87.335	0.00000	0.20810	0.1986	0.1243
−30.00	1.032	100.50	32.310	1.991	88.524	0.00469	0.20608	0.1994	0.1262
−20.00	1.419	99.75	24.022	3.989	89.721	0.00928	0.20427	0.2002	0.1280
−10.00	1.918	99.00	18.143	5.997	90.927	0.01380	0.20267	0.2011	0.1298
0.00	2.554	98.24	13.903	8.013	92.139	0.01823	0.20124	0.2020	0.1316
5.00	2.931	97.86	12.233	9.024	92.747	0.02041	0.20059	0.2024	0.1325
10.00	3.352	97.48	10.798	10.038	93.357	0.02258	0.19998	0.2029	0.1334
15.00	3.822	97.09	9.5606	11.054	93.967	0.02473	0.19941	0.2033	0.1343
20.00	4.343	96.71	8.4906	12.072	94.579	0.02686	0.19887	0.2038	0.1352
25.00	4.920	96.32	7.5621	13.093	95.192	0.02898	0.19837	0.2043	0.1361
30.00	5.557	95.93	6.7536	14.117	95.806	0.03108	0.19790	0.2048	0.1370
35.00	6.259	95.54	6.0477	15.143	96.420	0.03316	0.19747	0.2053	0.1379
40.00	7.031	95.14	5.4294	16.172	97.035	0.03523	0.19706	0.2059	0.1388
45.00	7.876	94.75	4.8863	17.203	97.650	0.03728	0.19668	0.2064	0.1397
50.00	8.800	94.35	4.4080	18.238	98.265	0.03931	0.19633	0.2070	0.1406
55.00	9.809	93.95	3.9856	19.275	98.880	0.04134	0.19601	0.2075	0.1415
60.00	10.907	93.55	3.6116	20.315	99.495	0.04334	0.19571	0.2081	0.1424
65.00	12.099	93.14	3.2795	21.358	100.109	0.04534	0.19543	0.2087	0.1433
70.00	13.392	92.73	2.9841	22.405	100.723	0.04732	0.19518	0.2093	0.1442
74.67b	14.696	92.35	2.7369	23.386	101.297	0.04916	0.19496	0.2099	0.1451
75.00	14.790	92.33	2.7206	23.455	101.337	0.04928	0.19495	0.2100	0.1452
80.00	16.301	91.91	2.4851	24.507	101.949	0.05124	0.19473	0.2106	0.1461
85.00	17.929	91.50	2.2741	25.564	102.560	0.05318	0.19454	0.2113	0.1470
90.00	19.681	91.08	2.0846	26.624	103.170	0.05511	0.19437	0.2119	0.1479
95.00	21.563	90.66	1.9142	27.687	103.778	0.05703	0.19421	0.2126	0.1489

			Velocity of	Viscosity,	Thermal Cond,	Surface
	Temp,*	c_p/c_v	Sound, ft/s	lb_m/ft · h	Btu/h · ft · ° F.	Tension,	Temp,*

° F.	Vapor	Liquid	Vapor	Liquid	Vapor	Liquid	Vapor	dyne/cm	° F.

−166.85a	1.1680	—	352.	—	—	—	—	—	−166.85
−160.00	1.1655	—	356.	—	—	—	—	—	−160.00
−150.00	1.1620	3953.	361.	—	—	—	—	35.26	−150.00
−140.00	1.1588	3895.	366.	—	—	—	—	34.44	−140.00
−130.00	1.1558	3829.	371.	—	—	—	—	33.63	−130.00
−120.00	1.1531	3758.	376.	—	—	—	—	32.82	−120.00
−110.00	1.1506	3684.	381.	—	—	—	—	32.01	−110.00
−100.00	1.1482	3609.	386.	—	—	—	—	31.21	−100.00
−90.00	1.1461	3533.	391.	—	—	—	—	30.41	−90.00
−80.00	1.1442	3457.	396.	—	—	—	—	29.62	−80.00
−70.00	1.1425	3382.	400.	—	—	—	—	28.83	−70.00
−60.00	1.1410	3308.	405.	—	—	—	—	28.04	−60.00
−50.00	1.1396	3235.	409.	—	—	—	—	27.26	−50.00
−40.00	1.1384	3163.	414.	—	—	—	—	26.49	−40.00
−30.00	1.1374	3093.	418.	—	—	—	—	25.72	−30.00
−20.00	1.1366	3024.	422.	1.889	0.0222	0.0595	—	24.95	−20.00
−10.00	1.1360	2955.	426.	1.782	0.0227	0.0587	—	24.19	−10.00
0.00	1.1356	2888.	430.	1.678	0.0231	0.0579	—	23.43	0.00
5.00	1.1354	2855.	432.	1.627	0.0233	0.0575	—	23.05	5.00
10.00	1.1354	2822.	433.	1.578	0.0236	0.0571	—	22.68	10.00
15.00	1.1353	2789.	435.	1.529	0.0238	0.0567	—	22.30	15.00
20.00	1.1354	2757.	437.	1.482	0.0240	0.0563	—	21.93	20.00
25.00	1.1355	2725.	438.	1.436	0.0243	0.0559	—	21.56	25.00
30.00	1.1356	2693.	440.	1.390	0.0245	0.0555	—	21.19	30.00
35.00	1.1358	2661.	442.	1.347	0.0247	0.0551	0.00470	20.82	35.00
40.00	1.1361	2629.	443.	1.304	0.0250	0.0548	0.00475	20.45	40.00
45.00	1.1364	2598.	444.	1.262	0.0252	0.0544	0.00480	20.08	45.00
50.00	1.1368	2567.	446.	1.222	0.0254	0.0540	0.00485	19.72	50.00
55.00	1.1373	2536.	447.	1.183	0.0256	0.0536	0.00490	19.35	55.00
60.00	1.1378	2505.	448.	1.145	0.0259	0.0532	0.00495	18.99	60.00
65.00	1.1385	2474.	450.	1.109	0.0261	0.0528	0.00501	18.63	65.00
70.00	1.1392	2444.	451.	1.073	0.0264	0.0524	0.00506	18.27	70.00
74.67b	1.1399	2415.	452.	1.041	0.0266	0.0521	0.00511	17.94	74.67
75.00	1.1400	2413.	452.	1.039	0.0266	0.0521	0.00512	17.91	75.00
80.00	1.1409	2383.	453.	1.006	0.0268	0.0517	0.00517	17.56	80.00
85.00	1.1419	2353.	454.	0.974	0.0271	0.0513	0.00523	17.20	85.00
90.00	1.1429	2323.	455.	0.943	0.0273	0.0509	0.00528	16.85	90.00
95.00	1.1441	2293.	456.	0.913	0.0276	0.0505	0.00534	16.49	95.00

*temperatures are on the ITS-90 scale
a = triple point
b = normal boiling point
c = critical point

TABLE 1B


Refrigerant 11 (Trichlorofluoromethane) Properties of Saturated Liquid and Saturated Vapor

° F.	psia	Liquid	Vapor	Liquid	Vapor	Liquid	Vapor	Liquid	Vapor

100.00	23.581	90.23	1.7605	28.754	104.384	0.05894	0.19407	0.2134	0.1498
105.00	25.743	89.81	1.6217	29.825	104.989	0.06083	0.19394	0.2141	0.1508
110.00	28.053	89.38	1.4960	30.900	105.591	0.06272	0.19383	0.2149	0.1518
115.00	30.520	88.94	1.3821	31.978	106.191	0.06459	0.19374	0.2156	0.1528
120.00	33.150	88.51	1.2787	33.060	106.788	0.06646	0.19365	0.2164	0.1538
125.00	35.950	88.07	1.1846	34.147	107.382	0.06832	0.19358	0.2172	0.1548
130.00	38.926	87.62	1.0988	35.238	107.974	0.07017	0.19352	0.2181	0.1558
135.00	42.087	87.17	1.0205	36.333	108.562	0.07200	0.19346	0.2189	0.1569
140.00	45.439	86.72	0.9489	37.433	109.146	0.07383	0.19342	0.2198	0.1580
145.00	48.989	86.26	0.8833	38.537	109.727	0.07565	0.19339	0.2207	0.1591
150.00	52.745	85.80	0.8232	39.646	110.304	0.07747	0.19336	0.2217	0.1602
160.00	60.905	84.86	0.7172	41.878	111.445	0.08107	0.19333	0.2236	0.1626
170.00	69.979	83.91	0.6273	44.130	112.566	0.08464	0.19333	0.2257	0.1650
180.00	80.030	82.93	0.5506	46.403	113.666	0.08819	0.19334	0.2279	0.1677
190.00	91.120	81.93	0.4849	48.699	114.743	0.09171	0.19337	0.2303	0.1705
200.00	103.31	80.90	0.4283	51.019	115.793	0.09521	0.19341	0.2328	0.1735
210.00	116.68	79.85	0.3793	53.364	116.815	0.09870	0.19344	0.2356	0.1768
220.00	131.28	78.77	0.3367	55.736	117.805	0.10216	0.19348	0.2385	0.1804
230.00	147.18	77.65	0.2996	58.136	118.760	0.10561	0.19351	0.2418	0.1844
240.00	164.46	76.50	0.2670	60.567	119.677	0.10905	0.19353	0.2453	0.1888
250.00	183.19	75.30	0.2384	63.032	120.551	0.11248	0.19353	0.2493	0.1937
260.00	203.43	74.06	0.2131	65.533	121.378	0.11591	0.19351	0.2537	0.1993
270.00	225.26	72.78	0.1906	68.074	122.152	0.11934	0.19346	0.2587	0.2057
280.00	248.77	71.43	0.1706	70.659	122.867	0.12278	0.19336	0.2645	0.2131
290.00	274.03	70.01	0.1528	73.294	123.513	0.12623	0.19322	0.2713	0.2219
300.00	301.12	68.51	0.1367	75.985	124.082	0.12970	0.19301	0.2794	0.2326
310.00	330.14	66.92	0.1222	78.742	124.559	0.13320	0.19273	0.2894	0.2457
320.00	361.18	65.21	0.1090	81.578	124.926	0.13675	0.19235	0.3020	0.2625
330.00	394.36	63.35	0.0970	84.510	125.159	0.14037	0.19184	0.3188	0.2848
340.00	429.78	61.29	0.0859	87.565	125.220	0.14408	0.19117	0.3423	0.3159
350.00	467.60	58.97	0.0755	90.787	125.054	0.14794	0.19026	0.3778	0.3628
360.00	507.98	56.24	0.0657	94.248	124.561	0.15203	0.18901	0.4376	0.4418
370.00	551.15	52.86	0.0561	98.092	123.541	0.15651	0.18718	0.5570	0.6042
380.00	597.49	48.25	0.0458	102.678	121.417	0.16180	0.18412	—	—
388.33c	639.27	34.59	0.0289	112.749	112.749	0.17350	0.17350	∞	∞

° F.	Vapor	Liquid	Vapor	Liquid	Vapor	Liquid	Vapor	dyne/cm	° F.

100.00	1.1454	2263.	456.	0.884	0.0278	0.0502	0.00540	16.14	100.00
105.00	1.1468	2234.	457.	0.856	0.0281	0.0498	0.00546	15.79	105.00
110.00	1.1483	2204.	458.	0.829	0.0283	0.0494	0.00552	15.45	110.00
115.00	1.1500	2174.	458.	0.804	0.0286	0.0490	0.00559	—	115.00
120.00	1.1517	2145.	459.	0.778	0.0288	0.0486	0.00565	—	120.00
125.00	1.1536	2115.	459.	0.754	0.0291	0.0483	0.00572	—	125.00
130.00	1.1557	2086.	459.	0.731	0.0293	0.0479	0.00578	—	130.00
135.00	1.1579	2057.	459.	0.708	0.0296	0.0475	0.00585	—	135.00
140.00	1.1602	2027.	459.	0.687	0.0299	0.0471	0.00592	—	140.00
145.00	1.1628	1998.	460.	0.666	0.0302	0.0468	0.00599	—	145.00
150.00	1.1655	1969.	459.	0.646	0.0304	0.0464	0.00606	—	150.00
160.00	1.1715	1910.	459.	0.607	0.0310	0.0456	0.00621	—	160.00
170.00	1.1783	1851.	458.	0.572	0.0316	0.0449	0.00637	—	170.00
180.00	1.1861	1793.	457.	0.539	0.0322	0.0442	0.00654	—	180.00
190.00	1.1950	1734.	456.	0.508	0.0328	0.0434	0.00671	—	190.00
200.00	1.2052	1675.	454.	0.479	0.0334	0.0427	0.00689	—	200.00
210.00	1.2169	1615.	451.	0.453	0.0341	0.0419	0.00707	—	210.00
220.00	1.2302	1555.	448.	0.428	0.0347	0.0412	0.00727	—	220.00
230.00	1.2456	1495.	445.	0.404	0.0354	0.0404	0.00748	—	230.00
240.00	1.2634	1434.	441.	0.383	0.0362	0.0397	0.00769	—	240.00
250.00	1.2842	1372.	437.	0.363	0.0369	0.0390	0.00792	—	250.00
260.00	1.3086	1309.	432.	0.344	0.0377	0.0382	0.00815	—	260.00
270.00	1.3375	1245.	426.	0.326	0.0385	0.0375	0.00840	—	270.00
280.00	1.3721	1180.	420.	0.310	0.0393	0.0367	0.00866	—	280.00
290.00	1.4142	1114.	413.	0.294	0.0401	0.0360	0.00893	—	290.00
300.00	1.4663	1046.	406.	0.280	0.0410	0.0352	0.00921	—	300.00
310.00	1.5322	976.	397.	—	—	—	—	—	310.00
320.00	1.6179	904.	388.	—	—	—	—	—	320.00
330.00	1.7336	830.	378.	—	—	—	—	—	330.00
340.00	1.8976	752.	366.	—	—	—	—	—	340.00
350.00	2.1476	671.	354.	—	—	—	—	—	350.00
360.00	2.5730	586.	340.	—	—	—	—	—	360.00
370.00	3.4525	499.	325.	—	—	—	—	—	370.00
380.00	—	—	—	—	—	—	—	—	380.00
388.33c	∞	0.	0.	—	—	∞	∞	0.00	388.33

TABLE 2A


Refrigerant 600 (n-Butane) Properties of Saturated Liquid and Saturated Vapor

	Pres-	Density,	Volume,	Enthalpy,	Entropy,	Specific Heat c_p,
Temp,*	sure,	lb/ft³	ft³/lb	Btu/lb	Btu/lb · ° F.	Btu/lb · ° F.

° F.	psia	Liquid	Vapor	Liquid	Vapor	Liquid	Vapor	Liquid	Vapor

−150.00	0.021	43.72	2680.0	−54.034	145.702	−0.14904	0.49595	0.4804	0.2930
−140.00	0.038	43.39	1536.9	−49.229	148.643	−0.13377	0.48522	0.4807	0.2971
−130.00	0.066	43.06	917.01	−44.419	151.622	−0.11895	0.47570	0.4815	0.3012
−120.00	0.110	42.74	567.05	−39.597	154.636	−0.10455	0.46728	0.4829	0.3055
−110.00	0.178	42.41	362.20	−34.759	157.687	−0.09051	0.45985	0.4848	0.3099
−100.00	0.278	42.08	238.26	−29.899	160.772	−0.07681	0.45332	0.4873	0.3145
−90.00	0.423	41.75	160.98	−25.011	163.890	−0.06340	0.44759	0.4903	0.3192
−80.00	0.626	41.41	111.45	−20.090	167.042	−0.05027	0.44261	0.4938	0.3241
−70.00	0.907	41.08	78.895	−15.133	170.225	−0.03739	0.43829	0.4976	0.3292
−60.00	1.285	40.74	56.999	−10.134	173.438	−0.02473	0.43458	0.5019	0.3344
−50.00	1.786	40.40	41.955	−5.091	176.679	−0.01227	0.43143	0.5065	0.3399
−40.00	2.438	40.06	31.414	0.000	179.946	0.00000	0.42878	0.5114	0.3456
−30.00	3.273	39.71	23.893	5.142	183.238	0.01210	0.42659	0.5165	0.3515
−20.00	4.327	39.36	18.436	10.337	186.552	0.02404	0.42483	0.5219	0.3576
−10.00	5.638	39.01	14.416	15.587	189.887	0.03583	0.42345	0.5275	0.3640
0.00	7.251	38.66	11.410	20.896	193.240	0.04749	0.42242	0.5334	0.3706
5.00	8.184	38.48	10.194	23.573	194.922	0.05328	0.42203	0.5364	0.3740
10.00	9.211	38.30	9.1329	26.266	196.608	0.05903	0.42171	0.5394	0.3774
15.00	10.337	38.12	8.2031	28.974	198.298	0.06475	0.42147	0.5426	0.3810
20.00	11.569	37.93	7.3863	31.698	199.991	0.07045	0.42130	0.5457	0.3845
25.00	12.914	37.75	6.6666	34.438	201.686	0.07612	0.42119	0.5489	0.3882
30.00	14.378	37.56	6.0309	37.194	203.384	0.08176	0.42115	0.5522	0.3919
31.03b	14.696	37.52	5.9090	37.765	203.735	0.08292	0.42115	0.5528	0.3927
35.00	15.969	37.38	5.4677	39.967	205.084	0.08738	0.42117	0.5555	0.3957
40.00	17.693	37.19	4.9676	42.757	206.786	0.09297	0.42125	0.5588	0.3995
45.00	19.559	37.00	4.5224	45.564	208.490	0.09854	0.42138	0.5622	0.4035
50.00	21.574	36.81	4.1251	48.389	210.194	0.10409	0.42156	0.5657	0.4074
55.00	23.746	36.62	3.7697	51.231	211.899	0.10962	0.42180	0.5692	0.4115
60.00	26.081	36.42	3.4512	54.091	213.605	0.11513	0.42208	0.5728	0.4157
65.00	28.590	36.23	3.1649	56.970	215.311	0.12062	0.42241	0.5764	0.4199
70.00	31.279	36.03	2.9072	59.867	217.017	0.12609	0.42278	0.5801	0.4242
75.00	34.157	35.83	2.6747	62.783	218.721	0.13154	0.42319	0.5839	0.4286
80.00	37.232	35.63	2.4646	65.719	220.425	0.13697	0.42364	0.5877	0.4331
85.00	40.513	35.42	2.2742	68.673	222.127	0.14239	0.42413	0.5916	0.4377
90.00	44.009	35.22	2.1015	71.648	223.827	0.14780	0.42465	0.5956	0.4424
95.00	47.728	35.01	1.9445	74.643	225.524	0.15318	0.42520	0.5997	0.4472

° F.	Vapor	Liquid	Vapor	Liquid	Vapor	Liquid	Vapor	dyne/cm	° F.

−150.00	1.1323	4976.	548.	1.945	0.0109	0.0991	0.00362	28.19	−150.00
−140.00	1.1304	4906.	556.	1.737	0.0112	0.0967	0.00381	27.41	−140.00
−130.00	1.1286	4833.	564.	1.564	0.0115	0.0943	0.00399	26.64	−130.00
−120.00	1.1268	4757.	572.	1.416	0.0118	0.0921	0.00419	25.87	−120.00
−110.00	1.1251	4678.	579.	1.290	0.0121	0.0901	0.00439	25.11	−110.00
−100.00	1.1236	4597.	587.	1.182	0.0124	0.0881	0.00459	24.35	−100.00
−90.00	1.1221	4514.	594.	1.087	0.0127	0.0862	0.00480	23.59	−90.00
−80.00	1.1208	4428.	601.	1.003	0.0130	0.0843	0.00502	22.84	−80.00
−70.00	1.1196	4341.	608.	0.930	0.0133	0.0826	0.00524	22.10	−70.00
−60.00	1.1185	4252.	614.	0.865	0.0136	0.0809	0.00547	21.36	−60.00
−50.00	1.1177	4161.	620.	0.806	0.0139	0.0793	0.00571	20.63	−50.00
−40.00	1.1170	4070.	626.	0.754	0.0143	0.0777	0.00595	19.90	−40.00
−30.00	1.1166	3977.	631.	0.706	0.0146	0.0762	0.00621	19.18	−30.00
−20.00	1.1163	3883.	637.	0.663	0.0149	0.0747	0.00647	18.46	−20.00
−10.00	1.1163	3788.	641.	0.623	0.0153	0.0733	0.00674	17.75	−10.00
0.00	1.1166	3693.	646.	0.587	0.0156	0.0719	0.00701	17.04	0.00
5.00	1.1168	3645.	648.	0.570	0.0158	0.0712	0.00716	16.69	5.00
10.00	1.1171	3597.	650.	0.554	0.0159	0.0705	0.00730	16.34	10.00
15.00	1.1175	3549.	651.	0.539	0.0161	0.0698	0.00745	16.00	15.00
20.00	1.1180	3500.	653.	0.524	0.0163	0.0691	0.00760	15.65	20.00
25.00	1.1185	3452.	655.	0.509	0.0165	0.0685	0.00775	15.31	25.00
30.00	1.1191	3403.	656.	0.495	0.0166	0.0678	0.00790	14.96	30.00
31.03b	1.1193	3393.	656.	0.492	0.0167	0.0677	0.00793	14.89	31.03
35.00	1.1198	3354.	657.	0.482	0.0168	0.0672	0.00806	14.62	35.00
40.00	1.1206	3305.	659.	0.469	0.0170	0.0665	0.00822	14.28	40.00
45.00	1.1215	3256.	660.	0.456	0.0172	0.0659	0.00838	13.94	45.00
50.00	1.1225	3207.	661.	0.444	0.0174	0.0652	0.00854	13.61	50.00
55.00	1.1236	3158.	661.	0.432	0.0176	0.0646	0.00871	13.27	55.00
60.00	1.1248	3108.	662.	0.421	0.0178	0.0639	0.00888	12.94	60.00
65.00	1.1261	3059.	662.	0.410	0.0179	0.0633	0.00905	12.61	65.00
70.00	1.1276	3009.	663.	0.400	0.0181	0.0627	0.00923	12.28	70.00
75.00	1.1291	2960.	663.	0.389	0.0183	0.0621	0.00941	11.95	75.00
80.00	1.1308	2910.	663.	0.379	0.0185	0.0614	0.00959	11.63	80.00
85.00	1.1326	2860.	663.	0.370	0.0187	0.0608	0.00977	11.30	85.00
90.00	1.1346	2810.	663.	0.360	0.0189	0.0602	0.00996	10.98	90.00
95.00	1.1367	2760.	662.	0.351	0.0191	0.0596	0.01015	10.66	95.00

*temperatures are on the IPTS-68 scale
b = normal boiling point
c = critical point

TABLE 2B


Refrigerant 600 (n-Butane) Properties of Saturated Liquid and Saturated Vapor

° F.	psia	Liquid	Vapor	Liquid	Vapor	Liquid	Vapor	Liquid	Vapor

100.00	51.679	34.80	1.8015	77.658	227.219	0.15856	0.42579	0.6038	0.4521
105.00	55.871	34.59	1.6711	80.694	228.909	0.16392	0.42640	0.6080	0.4571
110.00	60.314	34.37	1.5519	83.752	230.596	0.16927	0.42704	0.6123	0.4622
115.00	65.015	34.15	1.4428	86.831	232.278	0.17461	0.42770	0.6168	0.4675
120.00	69.986	33.93	1.3429	89.933	233.954	0.17993	0.42839	0.6213	0.4729
125.00	75.234	33.71	1.2511	93.057	235.625	0.18525	0.42909	0.6259	0.4784
130.00	80.770	33.48	1.1667	96.204	237.288	0.19056	0.42982	0.6307	0.4841
135.00	86.603	33.25	1.0889	99.375	238.945	0.19586	0.43056	0.6356	0.4900
140.00	92.743	33.02	1.0173	102.570	240.592	0.20115	0.43131	0.6406	0.4961
145.00	99.199	32.78	0.9511	105.790	242.231	0.20644	0.43208	0.6458	0.5023
150.00	105.98	32.54	0.8899	109.035	243.859	0.21172	0.43286	0.6512	0.5088
155.00	113.10	32.30	0.8332	112.306	245.476	0.21700	0.43365	0.6567	0.5156
160.00	120.57	32.05	0.7807	115.604	247.081	0.22227	0.43444	0.6625	0.5226
165.00	128.39	31.80	0.7319	118.930	248.672	0.22754	0.43524	0.6685	0.5298
170.00	136.59	31.54	0.6865	122.284	250.249	0.23281	0.43604	0.6747	0.5374
175.00	145.16	31.28	0.6443	125.668	251.809	0.23809	0.43684	0.6812	0.5454
180.00	154.12	31.01	0.6049	129.082	253.351	0.24336	0.43763	0.6880	0.5537
185.00	163.48	30.73	0.5682	132.527	254.873	0.24864	0.43842	0.6951	0.5626
190.00	173.25	30.46	0.5339	136.006	256.374	0.25392	0.43920	0.7026	0.5719
195.00	183.45	30.17	0.5018	139.518	257.851	0.25921	0.43996	0.7106	0.5817
200.00	194.09	29.88	0.4717	143.066	259.302	0.26451	0.44071	0.7190	0.5923
210.00	216.71	29.27	0.4170	150.277	262.113	0.27515	0.44215	0.7377	0.6157
220.00	241.23	28.62	0.3687	157.654	264.783	0.28585	0.44347	0.7594	0.6433
230.00	267.76	27.94	0.3256	165.218	267.276	0.29664	0.44462	0.7853	0.6766
240.00	296.42	27.20	0.2871	173.001	269.548	0.30757	0.44556	0.8173	0.7182
250.00	327.34	26.40	0.2523	181.042	271.533	0.31868	0.44619	0.8587	0.7726
260.00	360.69	25.51	0.2207	189.406	273.135	0.33005	0.44639	0.9155	0.8484
270.00	396.64	24.50	0.1915	198.197	274.203	0.34181	0.44597	1.0008	0.9633
280.00	435.43	23.32	0.1640	207.608	274.458	0.35421	0.44459	1.1490	1.1632
290.00	477.36	21.80	0.1370	218.088	273.282	0.36782	0.44144	1.4852	1.6136
300.00	522.95	19.41	0.1068	231.321	268.472	0.38481	0.43371	—	—
305.62c	550.56	14.22	0.0703	251.554	251.554	0.41093	0.41093	∞	∞

° F.	Vapor	Liquid	Vapor	Liquid	Vapor	Liquid	Vapor	dyne/cm	° F.

100.00	1.1390	2710.	662.	0.342	0.0194	0.0590	0.01035	10.34	100.00
105.00	1.1415	2660.	661.	0.333	0.0196	0.0584	0.01055	10.03	105.00
110.00	1.1442	2610.	660.	0.325	0.0198	0.0578	0.01075	9.71	110.00
115.00	1.1470	2559.	659.	0.316	0.0200	0.0572	0.01096	9.40	115.00
120.00	1.1501	2509.	657.	0.308	0.0202	0.0566	0.01117	9.09	120.00
125.00	1.1534	2459.	656.	0.301	0.0204	0.0560	0.01138	8.78	125.00
130.00	1.1570	2408.	654.	0.293	0.0207	0.0554	0.01160	8.48	130.00
135.00	1.1609	2357.	652.	0.285	0.0209	0.0548	0.01182	8.18	135.00
140.00	1.1650	2307.	650.	0.278	0.0211	0.0542	0.01205	7.88	140.00
145.00	1.1695	2256.	647.	0.271	0.0214	0.0536	0.01228	7.58	145.00
150.00	1.1744	2205.	645.	0.264	0.0216	0.0530	0.01251	7.28	150.00
155.00	1.1796	2154.	642.	0.257	0.0219	0.0524	0.01275	6.99	155.00
160.00	1.1853	2103.	639.	0.250	0.0221	0.0519	0.01300	6.70	160.00
165.00	1.1915	2052.	635.	0.243	0.0224	0.0513	0.01325	6.41	165.00
170.00	1.1982	2001.	632.	0.237	0.0227	0.0507	0.01350	6.12	170.00
175.00	1.2055	1949.	628.	0.230	0.0229	0.0501	0.01376	5.84	175.00
180.00	1.2135	1898.	624.	0.224	0.0232	0.0496	0.01403	5.56	180.00
185.00	1.2222	1846.	619.	0.218	0.0235	0.0490	0.01430	5.28	185.00
190.00	1.2318	1794.	615.	0.212	0.0238	0.0484	0.01458	5.01	190.00
195.00	1.2424	1742.	610.	0.206	0.0241	0.0479	0.01486	4.74	195.00
200.00	1.2540	1690.	604.	0.200	0.0244	0.0473	0.01516	4.47	200.00
210.00	1.2814	1585.	593.	0.188	0.0251	0.0462	0.01577	3.94	210.00
220.00	1.3158	1480.	579.	0.177	0.0258	0.0451	0.01641	3.43	220.00
230.00	1.3599	1372.	565.	0.165	0.0266	0.0440	0.01710	2.93	230.00
240.00	1.4183	1263.	548.	0.154	0.0274	0.0430	0.01784	2.45	240.00
250.00	1.4988	1152.	529.	0.143	0.0284	0.0419	0.01866	1.99	250.00
260.00	1.6157	1038.	509.	0.132	0.0295	0.0408	0.01962	1.55	260.00
270.00	1.8000	918.	485.	0.121	0.0308	0.0396	0.02082	1.14	270.00
280.00	2.1306	792.	459.	0.109	0.0325	0.0387	0.02256	0.75	280.00
290.00	2.8921	655.	428.	0.096	0.0348	0.0384	0.02571	0.40	290.00
300.00	—	—	—	0.079	0.0392	—	—	0.11	300.00
305.62c	∞	0.	0.	—	—	∞	∞	0.00	305.62

The performance index of Cycle No. 1 (cycle 20): $\frac{Q @ T_{H}}{Q Mech . Input}$
is 6.514. The per unit available energy of Cycle No. 2 (cycle 30) is 0.2006. The product of these performances, the net mechanical energy output per unit of mechanical energy per input is 6.514×0.2006=1.307. Thus, the system will sustain its own operation plus produce mechanical energy for other uses by extracting energy from the ambient environment.

The following is a list of reference numerals:

LIST FOR REFERENCE NUMERALS

(Part No.)	(Description)

10	preferred embodiment of the present invention
20	refrigeration/heat pump cycle
30	power cycle
40	compressor
50	heat exchanger
60	expansion valve
70	evaporator
80	engine
90	condenser
100	pump
110	pressure
120	enthalpy
130	pressure
140	enthalpy

All measurements disclosed herein are at standard temperature and pressure, at sea level on Earth, unless indicated otherwise. All materials used or intended to be used in a human being are biocompatible, unless indicated otherwise.
It will be understood that each of the elements described above, or two or more together may also find a useful application in other types of methods differing from the type described above. Without further analysis, the foregoing will so fully reveal the gist of the present invention 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 essential characteristics of the generic or specific aspects of this invention set forth in the appended claims. The foregoing embodiments are presented by way of example only; the scope of the present invention is to be limited only by the following claims.

Claims

1. A method of power generation comprising:

(a) a power cycle; and

(b) a heat pump cycle, the heat pump cycle supplying heat to the power cycle.

2. The method of claim 1, wherein the power cycle includes a first media and the heat pump cycle includes a second media, the first media being different from the second media.

3. The method of claim 2, wherein the first media has a first flow rate and the second media has a second flow rate, the first flow rate being different from the second flow rate.

4. The method of claim 1, wherein the heat pump cycle includes an expansion valve.

5. The method of claim 1, wherein the heat pump cycle includes an expansion turbine.

6. The method of claim 3, wherein the first media is R600 and the second media is R11.

7. The method of claim 6, wherein the flow rate of the second media is about two times the flow rate of the second media.

8. The method of claim 1, wherein the heat pump cycle includes a heat exchanger for rejecting heat and the power cycle uses this heat exchanger as a source of heat.

9. A method of removing heat from a space comprising:

(a) a power cycle;

(b) a heat pump cycle, the heat pump cycle supplying heat to the power cycle; and

(c) the heat pump cycle removing heat from the space.

10. A method of adding heat to a space comprising:

(a) a power cycle;

(c) the power cycle adding heat to the space.

11. A method of removing heat from a material in a process comprising:

(a) a power cycle;

(c) the heat pump cycle removing heat from the material.

12. A method of adding heat to a material in a process comprising:

(a) a power cycle;

(c) the power cycle adding heat to the material.

13. The invention substantially as shown and described herein.