ATBECHDEDKESFRGBGRITLILUNLSEMCPTIE......FI..MKCYAL..................................................JBDM Ver 0.1.63 (23 May 2017) - 2100000/01936129EUROPEAN PATENT SPECIFICATIONB120190102EP07110803.9199907232008072820090306enenen20190102201901200806252008262019010220190120181126F01K 25/06 20060101AFI20080515BHEP deVerfahren und Vorrichtung zur Umwandlung von Wärme in NutzenergieenMethod and apparatus of converting heat to useful energyfrProcédé et appareil de conversion de la chaleur en énergie utileEP-A- 0 649 985US-A- 4 346 561US-A- 4 573 321US-A- 4 756 16299305850.2107083019990723KALINA, Alexander, I.105 Glen Garry Way,Hillsborough,, CA 94010.USPELLETIER, Richard, I.3872 Pastana Way,Livermore,, CA 94550USRHODES, Lawrence, B.1060 Florence Road,Livermore,, CA 94550USKCT Power Limited101776720NMM/P416796EPc/o Chapman Davis LLP 2 Chapel CourtLondon SE1 1HHGBManley, Nicholas Michaelet al100027938WP Thompson 8th Floor 1 Mann IslandLiverpool L3 1BPGBATBECHCYDEDKESFIFRGBGRIEITLILUMCNLPTSEAL20080728MK2008072820080702200827 Background of the Invention

The invention relates to implementing a thermodynamic cycle to convert heat to useful form.

Thermal energy can be usefully converted into mechanical and then electrical form. Methods of converting the thermal energy of low temperature heat sources into electric power present an important area of energy generation. There is a need for increasing the efficiency of the conversion of such low temperature heat to electric power.

Thermal energy from a heat source can be transformed into mechanical and then electrical form using a working fluid that is expanded and regenerated in a closed system operating on a thermodynamic cycle. The working fluid can include components of different boiling temperatures, and the composition of the working fluid can be modified at different places within the system to improve the efficiency of operation. Systems that convert low temperature heat into electric power are described in Alexander I. Kalina's U.S. Pat. Nos. 4,346,561; 4,489,563; 4,982,568; and 5,029,444 . In addition, systems with multicomponent working fluids are described in Alexander I. Kalina's U.S. Pat. Nos. 4,548,043; 4,586,340, 4,604,867; 4,732,005; 4,763,480, 4,899,545; 5,095,708; 5,440,882; 5,572,871 and 5,649,426.

US-A-4,573,321 discloses a multi-step process for generating energy from a source heat flow, comprising passing a heated media having a mixture of a low volatility component and a high volatility component into a phase separator. The vaporous working fluid is withdrawn from the phase separator and passed into a work zone, such as a turbine, wherein the fluid is expanded. The expanded vaporous working fluid is withdrawn from the work zone and passed into a direct contact condenser or absorber. The separated weak solution is withdrawn from the phase separator and passed into counter-current heat exchange relationship in an interchanger with a portion of media from the direct contact condenser or absorber. The media from the direct contact condenser or absorber is withdrawn and passed into a fluid pressurizing zone. A portion of the media is then pumped into the interchanger where the media is heated and passed into counter-current heat exchange relationship in a trim heater with a portion of the source heat flow. The remaining portion of the media from the fluid pressurizing zone is pumped into counter-current heat exchange relationship in a regenerator with the remaining portion of the source heat flow. The heated media flows from the trim heater and the regenerator are combined to form the heated media and the cycle repeated.

EP-A-0,649,985 discloses a thermal power generator for generating electric power by utilizing a high heat source and a low heat source, comprising an evaporator, a vapor-liquid separator, and an absorber and a regenerator, to increase thermal efficiency of an evaporator and a condenser, and to reduce cost for building apparatuses

US-A-4,756,162 discloses method for utilising sensible heat energy supplied by a high-temperature heating fluid, employing a multi-component working fluid thermodynamic cycle, wherein a solution rich in a lower boiling component is heated in a vapor generator in counter-current heat exchange with the heating fluid to produce a vapor-fluid mixture which is separated in a rectifier into a lean solution and a vapor mixture. The enthalpy of the vapor mixture is optionally increased in a superheater by counter-current heat exchange with said heating fluid at its highest temperature; the vapor mixture is then expanded thereby to perform the function of the cycle; and the spent vapor mixture is dissolved in said lean solution in an absorber so as to regenerate the rich solution. The rich solution leaving the absorber is compressed and divided into a first and second parts. The first part is heated by counter-current heat exchange with said lean solution drawn from the rectifier, whereafter said first part of the rich solution is recycled to the vapor generator, whereas the second part of the rich solution extracts additional heat from the heating fluid leaving the vapor generator, by counter-current heat exchange, and is then fed into the rectifier for counter-current mass and heat exchange with the vapor-liquid mixture formed in the vapor generator.

Summary of the Invention

In accordance with a first aspect of the invention, there is provided a method for implementing a thermodynamic cycle, having the features of claim 1.

In accordance with a second aspect of the invention, there is provided an apparatus for implementing a thermodynamic cycle, having the features of claim 9.

Embodiments of the invention may include one or more of the following advantages. Embodiments of the invention can achieve efficiency of conversion of low temperature heat to electric power that exceeds the efficiency of standard Rankine cycles.

Other advantages and features of the invention will be apparent from the following detailed description of particular embodiments and from the claims.

Brief description of the drawings

The accompanying Figures 1 and 2 and the description thereof, illustrate the invention by way of example. In the drawings:-

Detailed Description of the Invention

Referring to Fig. 1, a system for implementing a thermodynamic cycle to obtain useful energy (e.g., mechanical and then electrical energy) from an external heat source is shown. In the described example, the external heat source is a stream of low temperature waste-heat water that flows in the path represented by points 25-26 through heat exchanger HE-5 and heats working stream 117-17 of the closed thermodynamic cycle. Table 1 presents the conditions at the numbered points indicated on Fig. 1. A typical output from the system is presented in Table 5.

The working stream of the Fig. 1 system is a multicomponent working stream that includes a low boiling component and a high boiling component. Such a preferred working stream may be an ammonia-water mixture, two or more hydrocarbons, two or more freons, mixtures of hydrocarbons and freons, or the like. In general, the working stream may be mixtures of any number of compounds with favorable thermodynamic characteristics and solubility. In a particularly preferred embodiment, a mixture of water and ammonia is used. In the system shown in Fig. 1, the working stream has the same composition from point 13 to point 19.

Beginning the discussion of the Fig. 1 system at the exit of turbine T, the stream at point 34 is referred to as the expanded, spent rich stream. This stream is considered "rich" in lower boiling point component. It is at a low pressure and will be mixed with a leaner, absorbing stream having parameters as at point 12 to produce the working stream of intermediate composition having parameters as at point 13. The stream at point 12 is considered "lean" in lower boiling point component.

At any given temperature, the working stream (of intermediate composition) at point 13 can be condensed at a lower pressure than the richer stream at point 34. This permits more power to be extracted from the turbine T, and increases the efficiency of the process.

The working stream at point 13 is partially condensed. This stream enters heat exchanger HE-2, where it is cooled and exits the heat exchanger HE-2 having parameters as at point 29. It is still partially, not completely, condensed. The stream now enters heat exchanger HE-1 where it is cooled by stream 23-24 of cooling water, and is thereby completely condensed, obtaining parameters as at point 14. The working stream having parameters as at point 14 is then pumped to a higher pressure obtaining parameters as at point 21. The working stream at point 21 then enters heat exchanger HE-2 where it is recuperatively heated by the working stream at points 13-29 (see above) to a point having parameters as at point 15. The working stream having parameters as at point 15 enters heat exchanger HE-3 where it is heated and obtains parameters as at point 16. In a typical design, point 16 may be precisely at the boiling point but it need not be. The working stream at point 16 is split into two substreams; first working substream 117 and second working substream 118. The first working substream having parameters as at point 117 is sent into heat exchanger HE-5, leaving with parameters as at point 17. It is heated by the external heat source, stream 25-26. The other substream, second working substream 118, enters heat exchanger HE-4 in which it is heated recuperatively, obtaining parameters as at point 18. The two working substreams, 17 and 18, which have exited heat exchangers HE-4 and HE-5, are combined to form a heated, gaseous working stream having parameters as at point 19. This stream is in a state of partial, or possibly complete, vaporization. In the preferred embodiment, point 19 is only partially vaporized. The working stream at point 19 has the same intermediate composition which was produced at point 13, completely condensed at point 14, pumped to a high pressure at point 21, and preheated to point 15 and to point 16. It enters the separator S. There, it is separated into a rich saturated vapor, termed the "heated gaseous rich stream" and having parameters as at point 30, and a lean saturated liquid, termed the "lean stream" and having parameters as at point 7. The lean stream (saturated liquid) at point 7 enters heat exchanger HE-4 where it is cooled while heating working stream 118-18 (see above) . The lean stream at point 9 exits heat exchanger HE-4 having parameters as at point 8. It is throttled to a suitably chosen pressure, obtaining parameters as at point 9.

Returning now to point 30, the heated gaseous rich stream (saturated vapor) exits separator S. This stream enters turbine T where it is expanded to lower pressures, providing useful mechanical energy to turbine T used to generate electricity. A partially expanded stream having parameters as at point 32 is extracted from the turbine T at an intermediate pressure (approximately the pressure as at point 9) and this extracted stream 32 (also referred to as a "second portion" of a partially expanded rich stream, the "first portion" being expanded further) is mixed with the lean stream at point 9 to produce a combined stream having parameters as at point 10. The lean stream having parameters as at point 9 serves as an absorbing stream for the extracted stream 32. The resulting stream (lean stream and second portion) having parameters as at point 10 enters heat exchanger HE-3 where it is cooled, while heating working stream 15-16, to a point having parameters as at point 11. The stream having parameters as at point 11 is then throttled to the pressure of point 34, obtaining parameters as at point 12.

Returning to turbine T, not all of the turbine inflow was extracted at point 32 in a partially expanded state. The remainder, referred to as the first portion, is expanded to a suitably chosen low pressure and exits the turbine T at point 34. The cycle is closed.

In the embodiment shown in Fig. 1, the extraction at point 32 has the same composition as the streams at points 30 and 34. In the embodiment shown in Fig. 2, the turbine is shown as first turbine stage T-1 and second turbine stage T-2, with the partially expanded rich stream leaving the higher pressure stage T-1 of the turbine at point 31. Conditions at the numbered points shown on Fig. 2 are presented in Table 2. A typical output from the Fig. 2 system is presented in Table 6.

Referring to Fig. 2, the partially expanded rich stream from first turbine stage T-1 is divided into a first portion at 33 that is expanded further at lower pressure turbine stage T-2, and a second portion at 32 that is combined with the lean stream at 9. The partially expanded rich stream enters separator S-2, where it is separated into a vapor portion and a liquid portion. The composition of the second portion at 32 may be chosen in order to optimize its effectiveness when it is mixed with the stream at point 9. Separator S-2 permits stream 32 to be as lean as the saturated liquid at the pressure and temperature obtained in the separator S-2; in that case, stream 33 would be a saturated vapor at the conditions obtained in the separator S-2. By choice of the amount of mixing at stream 133, the amount of saturated liquid and the saturated vapor in stream 32 can be varied.

Referring to Fig. 3, this embodiment does not form part of the invention and differs from the embodiment of Fig. 1, in that the heat exchanger HE-4 has been omitted, and there is no extraction of a partially expanded stream from the turbine stage. In the Fig. 3 embodiment, the hot stream exiting the separator S is admitted directly into heat exchanger HE-3. Conditions at the numbered points shown on Fig. 3 are presented in Table 3. A typical output from the system is presented in Table 7.

Referring to Fig. 4, this embodiment does not form part of the invention and differs from the Fig. 3 embodiment in omitting heat exchanger HE-2.
Conditions at the numbered points shown on Fig. 4 are presented in Table 4. A typical output from the system is presented in Table 8. While omitting heat exchanger HE-2 reduces the efficiency of the process, it may be economically advisable in circumstances where the increased power given up will not pay for the cost of the heat exchanger.

In general, standard equipment may be utilized in carrying out the method of this invention. Thus, equipment such as heat exchangers, tanks, pumps, turbines, valves and fittings of the type used in a typical Rankine cycles, may be employed in carrying out the method of this invention.

In the described embodiments of the invention, the working fluid is expanded to drive a turbine of conventional type. However, the expansion of the working fluid from a charged high pressure level to a spent low pressure level to release energy may be effected by any suitable conventional means known to those skilled in the art. The energy so released may be stored or utilized in accordance with any of a number of conventional methods known to those skilled in the art.

The separators of the described embodiments can be conventionally used gravity separators, such as conventional flash tanks. Any conventional apparatus used to form two or more streams having different compositions from a single stream may be used to form the lean stream and the enriched stream from the fluid working stream.

The condenser may be any type of known heat rejection device. For example, the condenser may take the form of a heat exchanger, such as a water cooled system, or another type of condensing device.

Various types of heat sources may be used to drive the cycle of this invention. Table 1 # P Mpa (psiA) X T°C (°F) H KJ/kg (BTU/lb) G/G30 Flow kg/hr (lb/hr) Phase 7 2.24 (325.22) .5156 94.9 (202.81) 191.4 (82.29) .5978 125,544 (276,778) SatLiquid 8 2.10 (305.22) .5156 76.4 (169.52) 103.6 (44.55) .5978 125,544 (276,778) Liq 28° 9 1.48 (214.26) .5156 76.4 (169.50) 103.6 (44.55) .5978 125,544 (276,778) Wet .9997 10 1.48 (214.26) .5533 76.4 (169.52) 210.0 (90.30) .6513 136,780 (301,549) Wet .9191 11 1.34 (194.26) .5533 37.7 (99.83) -69.3 (-29.79) .6513 136,780 (301,549) Liq 53° 12 0.59 (85.43) .5533 37.5 (99.36) -69.3 (-29.79) .6513 136,780 (301,549) Wet .9987 13 0.59 (85.43) .7000 37.6 (99.83) 405.7 (174.41) 1 210,021 (463,016) Wet.6651 14 0.58 (84.43) .7000 22.4 (72.40) -88.7 (-38.12) 1 210,021 (463,016) SatLiquid 15 2.41 (350.22) .7000 34.9 (94.83) -30.4 (-13.08) 1 210,021 (463,016) Liq 73° 16 2.31 (335.22) .7000 73.6 (164.52) 151.5 (65.13) 1 210,021 (463,016) SatLiquid 117 2.31 (335.22) .7000 73.6 (164.52) 151.5 (65.13) .8955 210,021 (463,016) SatLiquid 17 2.24 (325.22) .7000 95.2 (203.40) 704.6 (302.92) .8955 188,068 (414,621) Wet .5946 118 2.31 (335.22) .7000 73.6 (164.52) 151.5 (65.13) .1045 210,021 (463,016) SatLiquid 18 2.24 (325.22) .7000 92.1 (197.81) 653.6 (281.00) .1045 21,952 (48,395) Wet .6254 19 2.24 (325.22) .7000 94.9 (202.81) 699.2 (300.63) 1 210,021 (463,016) Wet .5978 21 2.45 (355.22) .7000 22.9 (73.16) -85.5 (-36.76) 1 210,021 (463,016) Liq 96° 29 0.59 (84.93) .7000 35.0 (95.02) 350.6 (150.73) 1 210,021 (463,016) Wet .6984 30 2.24 (325.22) .9740 94.9 (202.81) 1454.0 (625.10) .4022 84,476 (186,238) SatVapor 32 1.48 (214.69) .9740 76.8 (170.19) 1399.2 (601.53) .0535 11,236 (24,771) Wet .0194 34 0.59 (85.43) .9740 40.3 (104.60) 1292.7 (555.75) .3487 73,240 (161,467) Wet .0467 23 • Water 18.0 (64.40) 75.4 (32.40) 9.8669 2,072,245 (4,568,519) 24 • Water 28.6 (83.54) 119.9 (51.54) 9.8669 2,072,245 (4,568,519) 25 • Water 98.0 (208.40) 410.3 (176,40) 5.4766 1,150,196 (2,535,750) 26 • Water 76.4 (169.52) 319.9 (137.52) 5.4766 1,150,196 (2,535,750)
<b>Table 2</b> # P Mpa (psiA) X T°C (°F) H KJ/kg (BTU/lb) G/G30 Flow kg/hr (lb/hr) Phase 7 2.24 (325.22) .5156 94.9 (202.81) 191.4 (82.29) .5978 125,544 (276,778) SatLiquid 8 2.10 (305.22) .5156 76.4 (169.52) 103.6 (44.55) .5978 125,544 (276,778) Liq 28° 9 1.48 (214.19) .5156 76.4 (169.48) 103.6 (44.55) .5978 125,544 (276,778) Wet.997 10 1.48 (214.19) .5523 76.4 (169.52) 207.5 (89.23) .6570 137,990 (304,216) Wet .921 11 1.34 (194.19) .5523 37.6 (99.74) -69.3 (-29.96) .6570 137,990 (304,216) Liq 53° 12 0.59 (85.43) .5523 37.5 (99.53) -69.3 (-29.96) .6570 137,990 (304,216) Wet .9992 13 0.59 (85.43) .7000 37.6 (99.74) 404.6 (173.96) 1 210,021 (463,016) Wet.6658 14 0.58 (84.43) .7000 22.4 (72.40) -88.7 (-38.12) 1 210,021 (463,016) SatLiquid 15 2.41 (350.22) .7000 34.9 (94.74) -30.7 (-13.18) 1 210,021 (463,016) Liq 73° 16 2.31 (335.22) .7000 73.6 (164.52) 15.15 (65.13) 1 210,021 (463,016) SatLiquid 117 2.31 (335.22) .7000 73.6 (164.52) 151.5 (65.13) .8955 210,021 (463,016) SatLiquid 17 2.24 (325.22) .7000 95.2 (203.40) 704.6 (302.92) .8955 188,068 (414,621) Wel.5946 118 2.31 (335.22) .7000 73.6 (164.52) 151.5 (65.13) .1045 210,021 (463,016) SatLiquid 18 2.24 (325.22) .7000 92.1 (197.81) 653.6 (281.00) .1045 21,952 (48,395) Wet.6254 19 2.24 (325.22) .7000 94.9 (202.81) 699.2 (300.63) 1 210,021 (463,016) Wet .5978 21 2.31 (355.22) .7000 22.9 (73.16) -85.5 (-36.76) 1 210,021 (463,016) Liq 96° 29 0.59 (84.93) .7000 35.0 (94.96) 349.8 (150.38) 1 210,021 (463,016) Wet.6989 30 2.24 (325.22) .9740 94.9 (202.81) 1454.0 (625.10) .4022 84,476 (186,238) SatVapor 31 1.48 (214.69) .9740 77.0 (170.63) 1400.5 (602.12) .4022 84,476 (186,238) Wet .0189 32 1.48 (214.69) .9224 77.0 (170.63) 1255.9 (539.93) .0593 11,236 (27,437) Wel.1285 33 1.48 (214.69) .9829 77.0 (170.63) 1425.5 (612.87) .3430 72,030 (158,800) SatVapor 34 0.59 (85.43) .9829 39.0 (102.18) 1313.3 (564.60) .3430 72,030 (158,800) Wet.0294 35 1.48 (214.69) .5119 77.0 (170.63) 105.7 (45.44) .0076 1,600 (3,527) SatLiquid 23 • Water 18.0 (64.40) 75.4 (32.40) 9.8666 2,072,245 (4,568,371) 24 • Water 28.6 (83.50) 119.8 (51.50) 9.8666 2,072,245 (4,568,371) 25 • Water 98.0 (208.40) 410.3 (176.40) 5.4766 1,150,196 (2,535,750) 26 • Water 76.4 (169.52) 319.9 (137,52) 5.4766 1,150,196 (2,535,750)
<b>Table 3</b> # P Mpa (psiA) X T°C (°F) H KJ/kg (BTU/1b) G/G30 Flow kg/hr (lb/hr) Phase 10 2.01 (291.89) .4826 95.2 (203.40) 187.8 (80.72) .6506 133,576 (294,484) SatLiquid 11 1.87 (271.89) .4826 42.8 (109.02) -54.8 (-23.56) .6506 133,576 (294,484) Liq 89° 12 0.52 (75.35) .4826 42.8 (109.07) -54.8 (-23.56) .6506 133,576 (294,484) Wet .9994 13 0.52 (75.35) .6527 42.8 (109.02) 418.7 (180.50) 1 205,317 (452,648) Wet .6669 14 0.51 (74.35) .6527 22.4 (72.40) -110.3 (-47.40) 1 205,317 (452,648) SatLiquid 15 2.18 (316.89) .6527 40.0 (103.99) -28.9 (-12.43) 1 205,317 (452,648) Liq 64° 16 2.08 (301.89) .6527 73.6 (164.52) 128.9 (55.41) 1 205,317 (452,648) SatLiquid 17 2.01 (291.89) .6527 95.2 (203.40) 635.5 (273.22) 1 205,317 (452,648) Wet .6506 21 2.22 (321.89) .6527 22.8 (73.04) -107.4 (-46.18) 1 205,317 (452,648) Liq 97° 29 0.51 (74.85) .6527 38.2 (100.84) 341.4 (146.74) 1 205,317 (452,648) Wet.7104 30 2.01 (291.89) .9693 95.2 (203.40) 1469.2 (631.64) .3494 71,741 (158,164) SatVapor 34 0.52 (75.35) .9693 42.55 (108.59) 1303.6 (560.44) .3494 71,741 (158,164) Wet .0474 23 • Water 18.0 (64.40) 75.4 (32.40) 8.1318 1,669,606 (3,680,852) 24 • Water 31.2 (88.27) 130.9 (56.27) 8.1318 1,669,606 (3,680,852) 25 • Water 98 (208.40) 410.3 (176.40) 5.6020 1,150,196 (2,535,750) 26 • Water 76.4 (169.52) 319.9 (137.52) 5.6020 1,150,196 (2,535,750)
<b>Table 4</b> # P Mpa (psiA) X T°C (°F) H KJ/kg (BTU/lb) G/G30 Flow kg/hr (lb/hr) Phase 10 1.48 (214.30) .4059 95.2 (203.40) 186.5 (80.05) .7420 179,411 (395,533) SatLiquid 11 1.34 (194.30) .4059 25.4 (77.86) -128.6 (-55.30) .7420 179,411 (395,533) Liq 118° 12 0.36 (52.48) .4059 25.7(78.17) -128.6 (-55.30) .7420 179,411 (395,533) Liq 32° 29 0.36 (52.48) .5480 40.3 (104.46) 247.6 (106.44) 1 241,801 (533.080) Wet .7825 14 0.36 (51.98) .5480 22.4 (72.40) -139.7 (-60.06) 1 241,801 (533.080) SatLiquid 21 1.68 (244.30) .5480 22.7 (72.83) -137.6 (-59.16) 1 241,801 (533.080) Liq 98° 16 1.55 (224.30) .5480 73.6 (164.52) 96.0 (41.26) 1 241,801 (533.080) SatLiquid 17 1.48 (214.30) .5480 95.2 (203.40) 526.1 (226.20) 1 241,801 (533.080) Wet .742 30 1.48 (214.30) .9567 95.2 (203.40) 1503.7 (646.49) .2580 62,389 (137,546) SatVapor 34 0.36 (52.48) .9567 45.7 (114.19) 1329.4 (571.55) .2580 62,389 (137,546) Wet.0473 23 • Water 18 (64.40) 75.4 (32.40) 5.7346 1,386,640 (3,057,018) 24 • Water 34.2 (93.43) 142.9 (61.43) 5.7346 1,386,640 (3,057,018) 25 • Water 98 (208.40) 410.3 (176.40) 4.7568 1,150,197 (2,535,750) 26 • Water 76.4 (169.52) 319.9 (137.52) 4.7568 1,150,197 (2,535,750)
<b>Table 5</b> Performance Summary KCS34 Case 1 Heat in 28893.87 kW 553.08 KJ/kg (237.78 BTU/lb) Heat rejected 25638.63 kW 490.76 KJ/kg (210.99 BTU/lb) ∑ Turbine enthalpy drops 3420.86 kW 65.48 KJ/kg (28.15 BTU/lb) Turbine Work 3184.82 kW 60.96 KJ/kg (26.21 BTU/lb) Feed pump ΔH 1.36, power 175.97 kW 3.37 KJ/kg (1.45 BTU/lb) Feed + Coolant pump power 364.36 kW 6.978 KJ/kg (3.00 BTU/lb) Net Work 2820.46 kW 53.99 KJ/kg (23.21 BTU/lb) Gross Output 3184.82 kWe Cycle Output 3008.85 kWe Net Output 2820.46 kWe Net thermal efficiency 9.76% Second law limit 17.56% Second law efficiency 55.58% Specific Brine Consumption 407.73 kg/kW hr (899.05 1b/kW hr) Specific Power Output 2.45 Watt hr/kg (1.11 Watt hr/lb)
<b>Table 6</b> Performance Summary KCS34 Case 2 Turbine mass flow 58.34 kg/s 463016 lb/hr Pt 30 Volume flow 4044.45 l/s 514182 ft^3/hr Heat in 28893.87 kW 212.93 BTU/lb Heat rejected 25578.48 kW 188.50 BTU/lb ∑ Turbine enthalpy drops 3500.33 kW 25.80 BTU/lb Turbine Work 3258.81 kW 24.02 BTU/lb Feed pump ΔH 1.36, power 196.51 kW 1.45 BTU/lb Feed + Coolant pump power 408.52 kW 3.01 BTU/lb Net Work 2850.29 kW 21.00 BTU/lb Gross Output 3258.81 kWe Cycle Output 3062.30 kWe Net Output 2850.29 kWe Net thermal efficiency 9.86 % Second law limit 17.74 % Second law efficiency 55.60 % Specific Brine Consumption 889.65 lb/kW hr Specific Power Output 1.12 Watt hr/lb
<b>Table 7</b> Performance Summary KCS34 Case 3 Turbine mass flow 57.03 kg/s 452648 lb/hr Pt 30 Volume flow 4474.71 l/s 568882 ft^3/hr Heat in 28893.87 kW 217.81 BTU/lb Heat rejected 25754.18 kW 194.14 BTU/lb ∑ Turbine enthalpy drops 3300.55 kW 24.88 BTU/lb Turbine Work 3072.82 kW 23.16 BTU/lb Feed pump ΔH 1.21, power 170.92 kW 1.29 BTU/lb Feed + Coolant pump power 341.75 kW 2.58 BTU/lb Net Work 2731.07 kW 20.59 BTU/lb Gross Output 3072.82 kWe Cycle Output 2901.89 kWe Net Output 2731.07 kWe Net thermal efficiency 9.45 % Second law limit 17.39 % Second law efficiency 54.34 % Specific Brine Consumption 928.48 lb/kW hr Specific Power Output 1.08 Watt hr/lb Heat to Steam Boiler 15851.00 kW 577.22 BTU/lb Heat Rejected 10736.96 kW 390.99 BTU/lb
 <b>Table 8</b> Performance Summary KCS34 Case 4 Turbine mass flow 67.17 kg/s 533080 lb/hr Pt 30 Volume flow 7407.64 l/s 941754 ft^3/hr Heat in 28893.87 kW 184.94 BTU/lb Heat rejected 26012.25 kW 166.50 BTU/lb ∑ Turbine enthalpy drops 3020.89 kW 19.34 BTU/lb Turbine Work 2812.45 kW 18.00 BTU/lb Feed pump ΔH .89, power 147.99 kW 0.95 BTU/lb Feed + Coolant pump power 289.86 kW 1.86 BTU/lb Net Work 2522.59 kW 16.15 BTU/lb Gross Output 2812.45 kWe Cycle Output 2664.46 kWe Net Output 2522.59 kWe Net thermal efficiency 8.73 % Second law limit 17.02 % Second law efficiency 51.29 % Specific Brine Consumption 1005.22 lb/kW hr Specific Power Output 0.99 Watt hr/lb

A method for implementing a thermodynamic cycle comprising: separating a heated gaseous working stream at a first separator(S)including a low boiling point component and a higher boiling point component to provide a heated gaseous rich stream having relatively more of said low boiling point component and a lean stream having relatively less of said low boiling point component, expanding said heated gaseous rich stream to transform the energy of the stream into useable form and to provide an expanded, spent rich stream (34), combining said lean stream and said expanded, spent rich stream (34)to provide said working stream, wherein, after said combining and before said separating, said working stream is condensed by transferring heat to a low temperature source at a first heat exchanger (HE-1), and said working stream is thereafter pumped to a higher pressure, splitting said working stream into a first working substream (117) and a second working substream (118), and heating said first working substream (117) with an external source of heat (HE-5) to provide a heated first working substream (17), characterised in that the method comprises heating the second working substream (118) with heat from said lean stream thereby producing a heated second working substream (18) having a first set of thermodynamic characteristics, and combining said heated first working substream (17) with said heated second working substream (18) having the first set of thermodynamic characteristics to form the heated gaseous working stream. A method as claimed in claim 1, further comprising transferring, at a second heat exchanger (HE-2), heat from said working stream, prior to said working stream being condensed, to said working stream after said working stream has been pumped to said higher pressure and prior to said heating with said external source of heat. A method as claimed in claim 2, further comprising transferring, at a third heat exchanger (HE-3), heat from said lean stream to said working stream after said working stream has received heat at said second heat exchanger (HE-2) and prior to said splitting. A method as claimed in any one of the preceding claims, wherein said expanding takes place in a first expansion step and a second expansion step,
said heated gaseous rich stream being partially expanded to provide a partially expanded rich stream in said first expansion step,
further comprising dividing said partially expanded rich stream into a first portion and a second portion (34),
wherein said first portion (33)is expanded to provide said expanded, spent rich stream in said second expansion step, and
further comprising combining said second portion (34) with said lean stream before said combining of said lean stream and said expanded, spent rich stream. A method as claimed in claim 4, wherein said dividing includes separating said partially expanded rich stream into a vapor portion and a liquid portion, said first portion (33) including at least some of said vapor portion, and said second portion (34) including said liquid portion. A method as claimed in claim 4, further comprising combining some of said vapor portion with said liquid portion to provide said second portion (34). A method as claimed claim 6, further comprising transferring, at a heat exchanger (HE-3), heat from said lean stream and said second portion (34) to said working stream before said working stream has been split into the first working substream (117) and the second working substream (118). A method as claim in any of the preceding claims, further comprising extracting a partially expanded stream from a turbine (T) and mixing said partially expanded stream with said lean stream to produce a mixed lean stream. Apparatus for implementing a thermodynamic cycle comprising: a separator(S) to divide a heated gaseous working stream including a low boiling point component and a higher boiling point component, to provide a heated gaseous rich stream having relatively more of said low boiling point component and a lean stream having relatively less of said low boiling point component, an expander that is connected to receive at least a portion of said heated gaseous working stream and transform the energy of the stream into useable form and to output an expanded stream, a mixer that combines said expanded rich stream and said lean stream (12) a first heat exchanger (HE-1) and a pump that are connected between said expander and said separator(S), said first heat exchanger (HE-1) condensing said expanded stream by transferring heat to a low temperature source, and said pump thereafter pumping said expanded stream to a higher pressure to form the working stream, a stream splitter (16) connected to split said working stream, after said pumping into a first working substream (117) and a second working substream (118), a heat exchanger to heat the first working substream with an external source of heat (HE-5), a heat exchanger (HE-4) to heat the second working substream with the lean stream from the separator(s), a second mixer that combines the first heated working substream with the second working substream, and a second heat exchanger (HE-2) connected to transfer heat from said working stream (13), prior to said working stream being fully condensed , to said working stream (21) after said working stream has been pumped to said higher pressure at said pump and prior to said working stream being split at said stream splitter, characterised in that the heated second working substream has a first set of thermodynamic characteristics, and that the combined heated first working substream and heated second working substream having the first set of thermodynamic characteristics form the gaseous working stream. An apparatus as claimed in claim 9 , further comprising a third heat exchanger (HE-3) connected to transfer heat from said lean stream to said working stream after said working stream has received heat at said second heat exchanger (HE-2) and prior to said working stream being split at said stream splitter. The apparatus as claimed in claim 9, wherein said expander includes a first expansion stage and a second expansion stage,
said first expansion stage being connected to receive said heated gaseous rich stream and to output a partially expanded rich stream,
further comprising a second separator (S-2) that is connected to receive said partially expanded rich stream and divide it into a first portion (33) and a second portion (32),
wherein said second stage is connected to receive said first portion and expands said first portion to provide said expanded, spent rich stream (34), and
further comprising a third stream mixer that is connected to combine said second portion (32) with said lean stream before said lean stream is combined with said expanded, spent rich stream at said first stream mixer. An apparatus as claimed in claim 11, wherein said second separator (S-2) is connected to receive said partially expanded rich stream and to separate it into a vapor portion and a liquid portion, said first portion (33) including at least some of said vapor portion, and said second portion (32) including said liquid portion. An apparatus as claimed in claim 11, wherein said second separator (S-2) includes a fourth stream mixer connected to combine some of said vapor portion from said second separator (S-2) with said liquid portion from said second separator (S-2) to provide said second portion (32). An apparatus as claimed in claim 11, further comprising a heat exchanger (HE-3) connected to transfer heat from said lean stream and said second portion (32) to said working stream prior to said working stream being split at said stream splitter. Verfahren zum Implementieren eines thermodynamischen Zyklus, das Folgendes umfasst: Trennen eines erwärmten, gasförmigen Arbeitsstroms an einer ersten Trennvorrichtung (S), der eine Komponente mit niedrigem Siedepunkt und eine Komponente mit höherem Siedepunkt umfasst, um einen erwärmten, gasförmigen fetten Strom mit relativ mehr der Komponente mit niedrigem Siedepunkt und einen mageren Strom mit relativ weniger der Komponente mit niedrigem Siedepunkt bereitzustellen, Expandieren des erwärmten, gasförmigen fetten Stroms, um die Energie des Stroms in nutzbare Form zu wandeln und einen expandierten, erschöpften fetten Strom (34) bereitzustellen, Zusammenführen des mageren Stroms und des expandierten, erschöpften fetten Stroms (34), um den Arbeitsstrom bereitzustellen, wobei, nach dem Zusammenführen und vor dem Trennen, der Arbeitsstrom kondensiert wird, indem Wärme an einem ersten Wärmetauscher (HE-1) auf eine Niedertemperaturquelle übertragen wird und der genannte Arbeitsstrom danach auf einen höheren Druck gepumpt wird, Spalten des Arbeitsstroms in einen ersten Arbeitsunterstrom (117) und einen zweiten Arbeitsunterstrom (118), und Erwärmen des ersten Arbeitsunterstroms (117) mit einer externen Wärmequelle (HE-5), um einen erwärmten ersten Arbeitsunterstrom (17) bereitzustellen, dadurch gekennzeichnet, dass das Verfahren das Erwärmen des zweiten Arbeitsunterstroms (118) mit Wärme von dem mageren Strom umfasst, wodurch ein erwärmter zweiter Arbeitsunterstrom (18) mit einem ersten Satz von thermodynamischen Eigenschaften erzeugt wird, und Zusammenführen des erwärmten ersten Arbeitsunterstroms (17) mit dem erwärmten zweiten Arbeitsunterstrom (18) mit dem ersten Satz von thermodynamischen Eigenschaften, um den erwärmten, gasförmigen Arbeitsstrom zu bilden. Verfahren nach Anspruch 1, weiter umfassend das Übertragen, an einem zweiten Wärmetauscher (HE-2), von Wärme von dem Arbeitsstrom, bevor der Arbeitsstrom kondensiert wird, auf den Arbeitsstrom, nachdem der Arbeitsstrom auf den höheren Druck gepumpt wurde und vor dem Erwärmen mit der externen Wärmequelle. Verfahren nach Anspruch 2, weiter umfassend das Übertragen, an einem dritten Wärmetauscher (HE-3), von Wärme von dem mageren Strom auf den Arbeitsstrom, nachdem der Arbeitsstrom Wärme an dem zweiten Wärmetauscher (HE-2) empfangen hat und vor dem Spalten. Verfahren nach einem der vorangehenden Ansprüche, wobei das Expandieren in einem ersten Expansionsschritt und einem zweiten Expansionsschritt stattfindet,
wobei der erwärmte, gasförmige fette Strom teilweise expandiert wird, um einen teilweise expandierten fetten Strom in dem ersten Expansionsschritt bereitzustellen,
weiter umfassend das Teilen des teilweise expandierten fetten Stroms in einen ersten Anteil und einen zweiten Anteil (34),
wobei der erste Anteil (33) expandiert wird, um den expandierten, erschöpften fetten Strom in dem zweiten Expansionsschritt bereitzustellen, und
weiter umfassend das Zusammenführen des zweiten Anteils (34) mit dem mageren Strom vor dem Zusammenführen des mageren Stroms und des expandierten, erschöpften fetten Stroms. Verfahren nach Anspruch 4, wobei das Teilen das Trennen des teilweise expandierten fetten Stroms in einen Dampfanteil und einen Flüssiganteil umfasst, wobei der erste Anteil (33) mindestens einen Teil des Dampfanteils umfasst und der zweite Anteil (34) den Flüssiganteil umfasst. Verfahren nach Anspruch 4, weiter umfassend das Zusammenführen eines Teils des Dampfanteils mit dem Flüssiganteil, um den zweiten Anteil (34) bereitzustellen. Verfahren nach Anspruch 6, weiter umfassend das Übertragen, an einem Wärmetauscher (HE-3), von Wärme von dem mageren Strom und dem zweiten Anteil (34), auf den Arbeitsstrom, bevor der Arbeitsstrom in den ersten Arbeitsunterstrom (117) und den zweiten Arbeitsunterstrom (118) gespalten wurde. Verfahren nach einem der vorangehenden Ansprüche, weiter umfassend das Extrahieren eines teilweise expandierten Stroms von einer Turbine (T) und das Mischen des teilweise expandierten Stroms mit dem mageren Strom, um einen gemischten mageren Strom zu erzeugen. Vorrichtung zum Implementieren eines thermodynamischen Zyklus, die Folgendes umfasst: eine Trennvorrichtung (S) zum Trennen eines eine Komponente mit niedrigem Siedepunkt und eine Komponente mit höherem Siedepunkt umfassenden erwärmten, gasförmigen Arbeitsstroms, um einen erwärmten, gasförmigen fetten Strom mit relativ mehr der Komponente mit niedrigem Siedepunkt und einen mageren Strom mit relativ weniger der Komponente mit niedrigem Siedepunkt bereitzustellen, eine Expansionsvorrichtung, die dazu angeschlossen ist, mindestens einen Anteil des erwärmten, gasförmigen Arbeitsstroms zu empfangen und die Energie des Stroms in nutzbare Form zu wandeln und einen expandierten Strom auszugeben, eine Mischvorrichtung, die den expandierten fetten Strom und den mageren Strom (12) zusammenführt, einen ersten Wärmetauscher (HE-1) und eine Pumpe (P), die zwischen der Expansionsvorrichtung und der Trennvorrichtung (S) angeschlossen sind, wobei der erste Wärmetauscher (HE-1) den expandierten Strom kondensiert, indem er Wärme auf eine Niedertemperaturquelle überträgt und die Pumpe danach den expandierten Strom auf einen höheren Druck pumpt, um den Arbeitsstrom zu bilden, einen Stromspalter (16), der dazu angeschlossen ist, den Arbeitsstrom nach dem Pumpen in einen ersten Arbeitsunterstrom (117) und einen zweiten Arbeitsunterstrom (118) zu spalten, einen Wärmetauscher zum Erwärmen des ersten Arbeitsunterstroms mit einer externen Wärmequelle (HE-5), einen Wärmetauscher (HE-4) zum Erwärmen des zweiten Arbeitsunterstroms mit dem mageren Strom von der Trennvorrichtung (S), eine zweite Mischvorrichtung, die den ersten erwärmten Arbeitsunterstrom mit dem zweiten Arbeitsunterstrom zusammenführt, und einen zweiten Wärmetauscher (HE-2), der dazu angeschlossen ist, bevor der Arbeitsstrom vollständig kondensiert ist, Wärme von dem Arbeitsstrom (13) auf den Arbeitsstrom (21) zu übertragen, nachdem der Arbeitsstrom an der Pumpe auf einen höheren Druck gepumpt wurde und bevor der Arbeitsstrom an dem Stromspalter gespalten wird, dadurch gekennzeichnet, dass der erwärmte zweite Arbeitsunterstrom einen ersten Satz von thermodynamischen Eigenschaften aufweist und dass der zusammengeführte, erwärmte erste Arbeitsunterstrom und der erwärmte zweite Arbeitsunterstrom, die den gleichen Satz von thermodynamischen Eigenschaften aufweisen, den gasförmigen Arbeitsstrom bilden. Vorrichtung nach Anspruch 9, weiter umfassend einen dritten Wärmetauscher (HE-3), der dazu angeschlossen ist, Wärme von dem mageren Strom auf den Arbeitsstrom zu übertragen, nachdem der Arbeitsstrom Wärme an dem zweiten Wärmetauscher (HE-2) empfangen hat und bevor der Arbeitsstrom an dem Stromspalter gespalten wird. Vorrichtung nach Anspruch 9, wobei die Expansionsvorrichtung eine erste Expansionsstufe und eine zweite Expansionsstufe umfasst,
wobei die erste Expansionsstufe dazu angeschlossen ist, den erwärmten, gasförmigen fetten Strom zu empfangen und einen teilweise expandierten fetten Strom auszugeben,
weiter umfassend eine zweite Trennvorrichtung (S-2), die dazu angeschlossen ist, den teilweise expandierten fetten Strom zu empfangen und ihn in einen ersten Anteil (33) und einen zweiten Anteil (32) zu teilen,
wobei die zweite Stufe dazu angeschlossen ist, den ersten Anteil zu empfangen und den ersten Anteil expandiert, um den expandierten, erschöpften fetten Strom (34) bereitzustellen, und
weiter umfassend eine dritte Strommischvorrichtung, die dazu angeschlossen ist, den zweiten Anteil (32) mit dem mageren Strom zusammenzuführen, bevor der magere Strom mit dem expandierten, erschöpften fetten Strom an der ersten Strommischvorrichtung zusammengeführt wird. Vorrichtung nach Anspruch 11, wobei die zweite Trennvorrichtung (S-2) dazu angeschlossen ist, den teilweise expandierten fetten Strom zu empfangen und ihn in einen Dampfanteil und einen Flüssiganteil zu trennen, wobei der erste Anteil (33) mindestens einen Teil der Dampfanteils umfasst und der zweite Anteil (32) den Flüssiganteil umfasst. Vorrichtung nach Anspruch 11, wobei die zweite Trennvorrichtung (S-2) eine vierte Strommischvorrichtung umfasst, die dazu angeschlossen ist, einen Teil des Dampfanteils von der zweiten Trennvorrichtung (S-2) mit dem Flüssiganteil von der zweiten Trennvorrichtung (S-2) zusammenzuführen, um den zweiten Anteil (32) bereitzustellen. Vorrichtung nach Anspruch 11, weiter umfassend einen Wärmetauscher (HE-3), der dazu angeschlossen ist, Wärme von dem mageren Strom und dem zweiten Anteil (32) auf den Arbeitsstrom zu übertragen, bevor der Arbeitsstrom an dem Stromspalter gespalten wird. Procédé pour mettre en oeuvre un cycle thermodynamique comprenant les opérations consistant à : séparer un flux de travail gazeux chauffé au niveau d'un premier séparateur (S) incluant un composant à faible point d'ébullition et un composant à point d'ébullition plus élevé afin de fournir un flux riche gazeux chauffé ayant une quantité relativement plus importante dudit composant à faible point d'ébullition et un flux pauvre ayant une quantité relativement moins importante dudit composant à faible point d'ébullition, effectuer la détente dudit flux riche gazeux chauffé afin de transformer l'énergie du flux en une forme utilisable, et de fournir un flux riche épuisé détendu (34), combiner ledit flux pauvre et ledit flux riche épuisé détendu (34) afin de fournir ledit flux de travail, dans lequel, après ladite combinaison et avant ladite séparation, ledit flux de travail est condensé par suite du transfert de chaleur vers une source à basse température au niveau d'un premier échangeur de chaleur (HE-1), et ledit flux de travail est ensuite pompé jusqu'à une pression plus élevée, fractionner ledit flux de travail en un premier sous-flux de travail (117) et en un deuxième sous-flux de travail (118), et chauffer ledit premier sous-flux de travail (117) à l'aide d'une source externe de chaleur (HE-5) afin de fournir un premier sous-flux de travail chauffé (17), caractérisé en ce que le procédé comprend le chauffage du deuxième sous-flux de travail (118) à l'aide de la chaleur en provenance dudit flux pauvre, permettant par conséquent de produire un deuxième sous-flux de travail chauffé (18) ayant un premier ensemble de caractéristiques thermodynamiques, et combiner ledit premier sous-flux de travail chauffé (17) avec ledit deuxième sous-flux de travail chauffé (18) ayant le premier ensemble de caractéristiques thermodynamiques afin de former le flux de travail gazeux chauffé. Procédé tel que revendiqué dans la revendication 1, comprenant en outre l'opération consistant à transférer, au niveau d'un deuxième échangeur de chaleur (HE-2), de la chaleur en provenance dudit flux de travail, avant que ledit flux de travail ne soit condensé, vers ledit flux de travail après que ledit flux de travail ait été pompé jusqu'à ladite pression plus élevée et avant ledit chauffage à l'aide de ladite source externe de chaleur. Procédé tel que revendiqué dans la revendication 2, comprenant en outre l'opération consistant à transférer, au niveau d'un troisième échangeur de chaleur (HE-3), de la chaleur en provenance dudit flux pauvre vers ledit flux de travail après que ledit flux de travail ait reçu de la chaleur au niveau dudit deuxième échangeur de chaleur (HE-2) et avant ledit fractionnement. Procédé tel que revendiqué dans l'une quelconque des revendications précédentes, dans lequel ladite détente a lieu dans une première étape de détente et une deuxième étape de détente,
ledit flux riche gazeux chauffé étant partiellement détendu afin de fournir un flux riche partiellement détendu dans ladite première étape de détente,
comprenant en outre la division dudit flux riche partiellement détendu en une première portion et en une deuxième portion (34),
dans lequel ladite première portion (33) est soumise à une détente afin de fournir ledit flux riche épuisé détendu dans ladite deuxième étape de détente, et
comprenant en outre la combinaison de ladite deuxième portion (34) avec ledit flux pauvre avant ladite combinaison dudit flux pauvre et dudit flux riche épuisé détendu. Procédé tel que revendiqué dans la revendication 4, dans lequel ladite division inclut la séparation dudit flux riche partiellement détendu en une portion vapeur et une portion liquide, ladite première portion (33) incluant au moins une certaine quantité de ladite portion vapeur, et ladite deuxième portion (34) incluant ladite portion liquide. Procédé tel que revendiqué dans la revendication 4, comprenant en outre la combinaison d'une certaine quantité de ladite portion vapeur avec ladite portion liquide afin de fournir ladite deuxième portion (34). Procédé tel que revendiqué dans la revendication 6, comprenant en outre l'opération consistant à transférer, au niveau d'un échangeur de chaleur (HE-3), la chaleur en provenance dudit flux pauvre et de ladite deuxième portion (34) vers ledit flux de travail avant que ledit flux de travail ne soit fractionné dans le premier sous-flux de travail (117) et le deuxième sous-flux de travail (118). Procédé tel que revendiqué dans l'une quelconque des revendications précédentes, comprenant en outre les opérations consistant à extraire un flux partiellement détendu en provenance d'une turbine (T), et à mélanger ledit flux partiellement détendu avec ledit flux pauvre afin de produire un flux pauvre mélangé. Appareil pour mettre en oeuvre un cycle thermodynamique comprenant : un séparateur (S) pour diviser un flux de travail gazeux chauffé incluant un composant à faible point d'ébullition et un composant à point d'ébullition plus élevé, afin de fournir un flux riche gazeux chauffé ayant une quantité relativement plus importante dudit composant à faible point d'ébullition et un flux pauvre ayant une quantité relativement moins importante dudit composant à faible point d'ébullition, un dispositif de détente qui est raccordé de façon à recevoir au moins une portion dudit flux de travail gazeux chauffé et à transformer l'énergie du flux en une forme utilisable et à délivrer en sortie un flux détendu, un mélangeur qui combine ledit flux riche détendu et ledit flux pauvre (12), un premier échangeur de chaleur (HE-1) et une pompe qui sont raccordés entre ledit dispositif de détente et ledit séparateur (S), ledit premier échangeur de chaleur (HE-1) condensant ledit flux détendu grâce au transfert de chaleur vers une source de température faible, et ladite pompe pompant ultérieurement ledit flux détendu jusqu'à une pression plus élevée afin de former le flux de travail, un dispositif de fractionnement de flux (16) raccordé de façon à fractionner ledit flux de travail, après ledit pompage en un premier sous-flux de travail (117) et un deuxième sous-flux de travail (118), un échangeur de chaleur étant destiné à chauffer le premier sous-flux de travail à l'aide d'une source externe de chaleur (HE-5), un échangeur de chaleur (HE-4) pour chauffer le deuxième sous-flux de travail à l'aide du flux pauvre en provenance du séparateur (S), un deuxième mélangeur qui combine le premier sous-flux de travail chauffé avec le deuxième sous-flux de travail, et un deuxième échangeur de chaleur (HE-2) raccordé de façon à transférer la chaleur en provenance dudit flux de travail (13), avant que ledit flux de travail ne soit entièrement condensé, vers ledit flux de travail (21) après que ledit flux de travail ait été pompé jusqu'à ladite pression plus élevée au niveau de ladite pompe et avant que ledit flux de travail ne soit fractionné au niveau dudit dispositif de fractionnement de flux, caractérisé en ce que le deuxième sous-flux de travail chauffé a un premier ensemble de caractéristiques thermodynamiques, et que le premier sous-flux de travail chauffé et le deuxième sous-flux de travail chauffé combinés ayant le premier ensemble de caractéristiques thermodynamiques forment le flux de travail gazeux. Appareil tel que revendiqué dans la revendication 9, comprenant en outre un troisième échangeur de chaleur (HE-3) raccordé de façon à transférer la chaleur en provenance dudit flux pauvre vers ledit flux de travail après que ledit flux de travail ait reçu de la chaleur au niveau dudit deuxième échangeur de chaleur (HE-2) et avant que ledit flux de travail ne soit fractionné au niveau dudit dispositif de fractionnement de flux. Appareil tel que revendiqué dans la revendication 9, dans lequel ledit dispositif de détente inclut un premier étage de détente et un deuxième étage de détente,
ledit premier étage de détente étant raccordé de façon à recevoir ledit flux riche gazeux chauffé et à délivrer en sortie un flux riche partiellement détendu,
comprenant en outre un deuxième séparateur (S-2) qui est raccordé de façon à recevoir ledit flux riche partiellement détendu et à le diviser en une première portion (33) et en une deuxième portion (32),
dans lequel ledit deuxième étage est raccordé de façon à recevoir ladite première portion et effectue la détente de ladite première portion afin de fournir ledit flux riche épuisé détendu (34), et
comprenant en outre un troisième mélangeur de flux qui est raccordé de façon à combiner ladite deuxième portion (32) avec ledit flux pauvre avant que ledit flux pauvre ne soit combiné avec ledit flux riche épuisé détendu au niveau dudit premier mélangeur de flux. Appareil tel que revendiqué dans la revendication 11, dans lequel ledit deuxième séparateur (S-2) est raccordé de façon à recevoir ledit flux riche partiellement détendu et à le séparer en une portion vapeur et une portion liquide, ladite première portion (33) incluant au moins une certaine quantité de ladite portion vapeur, et ladite deuxième portion (32) incluant ladite portion liquide. Appareil tel que revendiqué dans la revendication 11, dans lequel ledit deuxième séparateur (S-2) inclut un quatrième mélangeur de flux raccordé de façon à combiner une certaine quantité de ladite portion vapeur en provenance dudit deuxième séparateur (S-2) avec ladite portion liquide en provenance dudit deuxième séparateur (S-2) afin de fournir ladite deuxième portion (32). Appareil tel que revendiqué dans la revendication 11, comprenant en outre un échangeur de chaleur (HE-3) raccordé de façon à transférer la chaleur en provenance dudit flux pauvre et de ladite deuxième portion (32) vers ledit flux de travail avant que ledit flux de travail ne soit fractionné au niveau dudit dispositif de fractionnement de flux.
REFERENCES CITED IN THE DESCRIPTION

This list of references cited by the applicant is for the reader's convenience only. It does not form part of the European patent document. Even though great care has been taken in compiling the references, errors or omissions cannot be excluded and the EPO disclaims all liability in this regard.

Patent documents cited in the description