CA2812605A1 - Use of refrigeration loops to chill inlet air to gas turbine - Google Patents
Use of refrigeration loops to chill inlet air to gas turbine Download PDFInfo
- Publication number
- CA2812605A1 CA2812605A1 CA2812605A CA2812605A CA2812605A1 CA 2812605 A1 CA2812605 A1 CA 2812605A1 CA 2812605 A CA2812605 A CA 2812605A CA 2812605 A CA2812605 A CA 2812605A CA 2812605 A1 CA2812605 A1 CA 2812605A1
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- Prior art keywords
- temperature
- refrigerant
- inlet air
- refrigeration
- lng
- Prior art date
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- Abandoned
Links
- 238000005057 refrigeration Methods 0.000 title claims abstract description 117
- 239000003507 refrigerant Substances 0.000 claims abstract description 69
- 238000000034 method Methods 0.000 claims abstract description 66
- 238000004519 manufacturing process Methods 0.000 claims abstract description 19
- 238000003860 storage Methods 0.000 claims abstract description 9
- 238000000926 separation method Methods 0.000 claims abstract description 5
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 104
- 239000007789 gas Substances 0.000 claims description 98
- 239000003949 liquefied natural gas Substances 0.000 claims description 95
- 239000003345 natural gas Substances 0.000 claims description 48
- 239000013529 heat transfer fluid Substances 0.000 claims description 35
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 30
- 238000001816 cooling Methods 0.000 claims description 29
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims description 18
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 claims description 12
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 claims description 9
- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 claims description 9
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 6
- 239000000203 mixture Substances 0.000 claims description 6
- 239000001294 propane Substances 0.000 claims description 6
- WTPUKBUYGDXTOF-UHFFFAOYSA-N F[C](Cl)Br Chemical compound F[C](Cl)Br WTPUKBUYGDXTOF-UHFFFAOYSA-N 0.000 claims description 4
- OHMHBGPWCHTMQE-UHFFFAOYSA-N 2,2-dichloro-1,1,1-trifluoroethane Chemical compound FC(F)(F)C(Cl)Cl OHMHBGPWCHTMQE-UHFFFAOYSA-N 0.000 claims description 3
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 claims description 3
- ZJCFOZHHYJVNNP-UHFFFAOYSA-N F[C]Br Chemical compound F[C]Br ZJCFOZHHYJVNNP-UHFFFAOYSA-N 0.000 claims description 3
- 229910021529 ammonia Inorganic materials 0.000 claims description 3
- KYKAJFCTULSVSH-UHFFFAOYSA-N chloro(fluoro)methane Chemical compound F[C]Cl KYKAJFCTULSVSH-UHFFFAOYSA-N 0.000 claims description 3
- WGCNASOHLSPBMP-UHFFFAOYSA-N hydroxyacetaldehyde Natural products OCC=O WGCNASOHLSPBMP-UHFFFAOYSA-N 0.000 claims description 3
- 238000004064 recycling Methods 0.000 claims 1
- 239000003570 air Substances 0.000 description 60
- 239000012080 ambient air Substances 0.000 description 6
- 239000000356 contaminant Substances 0.000 description 6
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 4
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 4
- PXGOKWXKJXAPGV-UHFFFAOYSA-N Fluorine Chemical compound FF PXGOKWXKJXAPGV-UHFFFAOYSA-N 0.000 description 4
- 229910052799 carbon Inorganic materials 0.000 description 4
- 150000001875 compounds Chemical class 0.000 description 4
- 239000003651 drinking water Substances 0.000 description 4
- 235000020188 drinking water Nutrition 0.000 description 4
- 229910052731 fluorine Inorganic materials 0.000 description 4
- 239000011737 fluorine Substances 0.000 description 4
- 239000001257 hydrogen Substances 0.000 description 4
- 229910052739 hydrogen Inorganic materials 0.000 description 4
- 125000004435 hydrogen atom Chemical class [H]* 0.000 description 4
- 239000003621 irrigation water Substances 0.000 description 4
- 230000001932 seasonal effect Effects 0.000 description 4
- 230000008016 vaporization Effects 0.000 description 4
- 238000009834 vaporization Methods 0.000 description 4
- 230000010354 integration Effects 0.000 description 3
- WKBOTKDWSSQWDR-UHFFFAOYSA-N Bromine atom Chemical compound [Br] WKBOTKDWSSQWDR-UHFFFAOYSA-N 0.000 description 2
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 2
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 2
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 2
- 150000001412 amines Chemical class 0.000 description 2
- GDTBXPJZTBHREO-UHFFFAOYSA-N bromine Substances BrBr GDTBXPJZTBHREO-UHFFFAOYSA-N 0.000 description 2
- 229910052794 bromium Inorganic materials 0.000 description 2
- 229910002092 carbon dioxide Inorganic materials 0.000 description 2
- 239000001569 carbon dioxide Substances 0.000 description 2
- 239000000460 chlorine Substances 0.000 description 2
- 229910052801 chlorine Inorganic materials 0.000 description 2
- 230000006835 compression Effects 0.000 description 2
- 238000007906 compression Methods 0.000 description 2
- 239000012153 distilled water Substances 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- RLQJEEJISHYWON-UHFFFAOYSA-N flonicamid Chemical compound FC(F)(F)C1=CC=NC=C1C(=O)NCC#N RLQJEEJISHYWON-UHFFFAOYSA-N 0.000 description 2
- 239000012530 fluid Substances 0.000 description 2
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 2
- 239000011593 sulfur Substances 0.000 description 2
- RAHZWNYVWXNFOC-UHFFFAOYSA-N sulfur dioxide Inorganic materials O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 2
- 238000004378 air conditioning Methods 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 238000006731 degradation reaction Methods 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
Classifications
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
- F25B27/00—Machines, plants or systems, using particular sources of energy
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
- F01D—NON-POSITIVE DISPLACEMENT MACHINES OR ENGINES, e.g. STEAM TURBINES
- F01D15/00—Adaptations of machines or engines for special use; Combinations of engines with devices driven thereby
- F01D15/005—Adaptations for refrigeration plants
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F02—COMBUSTION ENGINES; HOT-GAS OR COMBUSTION-PRODUCT ENGINE PLANTS
- F02C—GAS-TURBINE PLANTS; AIR INTAKES FOR JET-PROPULSION PLANTS; CONTROLLING FUEL SUPPLY IN AIR-BREATHING JET-PROPULSION PLANTS
- F02C7/00—Features, components parts, details or accessories, not provided for in, or of interest apart form groups F02C1/00 - F02C6/00; Air intakes for jet-propulsion plants
- F02C7/12—Cooling of plants
- F02C7/14—Cooling of plants of fluids in the plant, e.g. lubricant or fuel
- F02C7/141—Cooling of plants of fluids in the plant, e.g. lubricant or fuel of working fluid
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F02—COMBUSTION ENGINES; HOT-GAS OR COMBUSTION-PRODUCT ENGINE PLANTS
- F02C—GAS-TURBINE PLANTS; AIR INTAKES FOR JET-PROPULSION PLANTS; CONTROLLING FUEL SUPPLY IN AIR-BREATHING JET-PROPULSION PLANTS
- F02C7/00—Features, components parts, details or accessories, not provided for in, or of interest apart form groups F02C1/00 - F02C6/00; Air intakes for jet-propulsion plants
- F02C7/12—Cooling of plants
- F02C7/14—Cooling of plants of fluids in the plant, e.g. lubricant or fuel
- F02C7/141—Cooling of plants of fluids in the plant, e.g. lubricant or fuel of working fluid
- F02C7/143—Cooling of plants of fluids in the plant, e.g. lubricant or fuel of working fluid before or between the compressor stages
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
- F25B49/00—Arrangement or mounting of control or safety devices
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
- F25J1/0022—Hydrocarbons, e.g. natural gas
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/006—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the refrigerant fluid used
- F25J1/008—Hydrocarbons
- F25J1/0082—Methane
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/006—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the refrigerant fluid used
- F25J1/008—Hydrocarbons
- F25J1/0085—Ethane; Ethylene
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/006—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the refrigerant fluid used
- F25J1/008—Hydrocarbons
- F25J1/0087—Propane; Propylene
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/006—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the refrigerant fluid used
- F25J1/008—Hydrocarbons
- F25J1/0092—Mixtures of hydrocarbons comprising possibly also minor amounts of nitrogen
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/006—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the refrigerant fluid used
- F25J1/0097—Others, e.g. F-, Cl-, HF-, HClF-, HCl-hydrocarbons etc. or mixtures thereof
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0228—Coupling of the liquefaction unit to other units or processes, so-called integrated processes
- F25J1/0235—Heat exchange integration
- F25J1/0236—Heat exchange integration providing refrigeration for different processes treating not the same feed stream
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
- F25J1/0279—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc.
- F25J1/0281—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc. characterised by the type of prime driver, e.g. hot gas expander
- F25J1/0283—Gas turbine as the prime mechanical driver
Abstract
As described herein, a method and system for operating a refrigeration system are provided. In the present methods and systems, a portion of the refrigerant from the refrigeration system is used for reducing the temperature of inlet air entering the gas turbine. The refrigeration system disclosed herein can be used for LNG production, air separation, food storage, or ice-making.
Description
USE OF REFRIGERATION LOOPS TO CHILL INLET MR TO GAS
TURBINE
[0001] This application is co-pending to U.S. Patent Application entitled "Method to Maximize LNG Plant Capacity in All Seasons", filed 30 December 2010, Attorney Docket No. 70205.0221US01, the contents of which are herein incorporated by reference in their entirety.
Field of the Invention
TURBINE
[0001] This application is co-pending to U.S. Patent Application entitled "Method to Maximize LNG Plant Capacity in All Seasons", filed 30 December 2010, Attorney Docket No. 70205.0221US01, the contents of which are herein incorporated by reference in their entirety.
Field of the Invention
[0002] The present application relates to a method and system which maximizes gas turbine output for a refrigerant loop. The method consumes a small amount of refrigerant and utilizes the refrigeration to chill the inlet air to the gas turbine ((iT) machines used in the refrigeration system. This approach enhances the gas turbine power output and efficiency which, in turn, increases the production of the plant. The gain in efficiency in production can compensate for the consumption of refrigerant.
Backuround of the Invention
Backuround of the Invention
[0003] Gas turbines are commonly used for driving compressors in refrigeration systems. For example, gas turbines are used in to drive refrigeration compressors in LNG production, air separation, food storage and ice making.
[0004] Gas turbines are constant volume machines and their output depends on the mass flow of air through the turbine. Over the years various technologies have been developed to increase the amount of useful power that gas turbines are able to produce.
One way of increasing the power output of a gas turbine is to cool the turbine inlet air prior to compressing it in the compressor. Cooling inlet air increases the air mass flow through the turbine, increasing turbine output and reducing heat rate. Cooling the inlet air also increases the turbine's efficiency.
One way of increasing the power output of a gas turbine is to cool the turbine inlet air prior to compressing it in the compressor. Cooling inlet air increases the air mass flow through the turbine, increasing turbine output and reducing heat rate. Cooling the inlet air also increases the turbine's efficiency.
[0005] Degradation of gas turbine output power with a rise in ambient air temperature further poses a serious problem. Cooling inlet air can address the problems associated with rising ambient temperatures.
[0006] Various systems have been devised for chilling the inlet air.
One system uses evaporative cooling, another uses a chiller to chill water that is then run through a coil. However, a continuing need exists for a turbine inlet air cooling system and method which is efficient and does not drain the system of power.
Summary of the Invention 100071 As described herein, a method and system for maximizing gas turbine output for a refrigeration loop are provided. The method and system provide a gain in energy efficiency of the gas turbine while compensating for an amount of energy required for consuming a portion of refrigerant.
100081 In one embodiment disclosed herein is an integrated system for refrigeration. The system comprises (a) a refrigeration system comprising a refrigeration loop for air-chilling; (b) a gas turbine for driving a compressor for the refrigeration system; (c) a heat exchanger for consuming a portion of refrigerant from the refrigeration system and cooling a heat transfer fluid; and (d) a second heat exchanger for reducing the temperature of inlet air entering the gas turbine with the heat transfer fluid.
[00091 In another embodiment disclosed herein is an integrated method of maximizing gas turbine output for a refrigeration loop. The method comprises (a) operating a refrigeration loop for chilling processes; (b) operating a gas turbine to drive a compressor for a the refrigeration loop; (c) gasifying a portion of refrigerant from the refrigeration system; and (d) reducing the temperature of inlet air entering the gas turbines by exchanging heat with the gasified portion of refrigerant either directly or indirectly.
[000101 In an additional embodiment disclosed herein is an integrated method of operating a gas turbine used in a refrigeration loop. The method comprises (a) operating a gas turbine to drive a compressor for a refrigeration system comprising a refrigeration loop and (b) chilling inlet air entering the gas turbine by (i) exchanging heat with a refrigerant in the refrigeration loop; or (ii) cooling a heat transfer fluid with a refrigerant in the refrigeration loop, and chilling inlet air entering the gas turbine by exchanging heat with the heat transfer fluid; or both (i) and (ii). In the method the refrigerant in the refrigeration loop comprises methane, ethane, propane, ammonia, a hydrofluorocarbon, a chlorofluorocarbon, a hydrochlorofluorocarbon, a bromofluorocarbon, a bromochlorofluorocarbon, or any combination thereof; and the heat transfer fluid comprises methanol, ethanol, a glycol and water mixture, or any combination thereof. In this method the gas turbine and refrigeration system can be used to produce LNG and the method further comprises cooling and condensing a natural gas stream by reducing the temperature of the natural gas using the refrigeration system.
1000111 In another embodiment disclosed herein is an integrated liquefied natural gas (LNG) system. The system comprises (a) an inlet stream comprising natural gas; (b) a refrigeration system for reducing the temperature of the natural gas and condensing the natural gas to produce LNG; (c) a gas turbine for driving a compressor for the refrigeration system; (d) a first vaporization heat exchanger for regasifying a portion of the LNG and cooling a heat transfer fluid; (e) a second vaporization heat exchanger for consuming a portion of refrigerant from the refrigeration system and cooling the heat transfer fluid; and (f) a third heat exchanger for reducing the temperature of inlet air entering the gas turbine with the heat transfer fluid. The integrated system can further comprise an outlet pipeline for supplying the regasified portion of the LNG to the domestic gas market.
[000121 In a further embodiment discloses herein is an integrated method for operating a liquefied natural gas (LNG) plant, the method comprising: (i) cooling and condensing a natural gas stream. in a refrigeration system to produce liquefied natural gas (LNG); (ii) operating a gas turbine to drive a compressor for the refrigeration system;
(iii) regasifying a portion of the LNG; (iv) consuming a portion of the refrigerant from the refrigeration system; and (iv) reducing the temperature of inlet air entering the gas turbine by exchanging heat with the regasified portion of the LNG and with the consumed portion of the refrigerant directly or indirectly.
Brief Description of the Drawines 1000131 Figure 1 illustrates an embodiment of the proposed refrigeration loop.
[OHM Figure 2 is a graph showing the monthly temperature variations at three locations for LNG and domestic natural gas production.
Detailed Description of the Invention 100151 In the prc-:c.rit methods and systems, a portion of refrigerant from the refrigeration system is utilized to cool the inlet air to the gas turbines in the refrigeration system, either directly or indirectly.
Definitions PON In accordance with this detailed description, the following abbreviations and definitions apply. It must be noted that as used herein, the singular forms "a", "an", and "the" include plural referents unless the context clearly dictates otherwise. Thus, for example, reference to "gas turbine" includes a plurality of such.
[00017] Unless otherwise stated, the following terms used in the specification and claims have the meanings given below:
[00018] "LNG" is liquefied natural gas. Natural gas from the well can consist of various hydrocarbons and contaminants; natural gas for the domestic market is comprised primarily of methane. At ambient temperature and pressure, LNG
exists as a gas, but it can be cooled and/or pressurized to provide a liquid, which facilitates storage and transportation.
[00019] "Remote location or market" means a location that is not readily accessible or economically feasible to access by pipeline. For example, a remote location or market can be at least over a thousand miles away from the natural gas source and/or is separated in geography such that it is not accessible by pipeline, for example, separated by oceans or other large, deep bodies of water.
[000201 "Local market" means a location that is within a distance and geography from the natural gas source so that the natural gas may be supplied as a gas by pipeline.
For example, local markets can be at any distance within several thousand miles from the natural gas source and is accessible by pipeline.
[00021] "Direct" in the context of heat exchange means that the heat exchange between the refrigerant and the inlet air is direct with no intermediate heat transfer fluid involved.
1000221 "Indirect" in the context of heat exchange means that the heat exchange between the refrigerant and the inlet air involves an intermediate heat transfer fluid.
Accordingly, the temperature of inlet air entering the gas turbine is reduced by exchanging heat with the refrigerant through a heat transfer fluid system.
[00023] "Integrated" means that the steps or units of the system or interconnected so that when operating together greater efficiencies are realized in comparison to when operating independently.
1000241 A "hydrofluorocarbon" means a compound containing carbon, hydrogen, and fluorine.
[00025] A "chlorofluorocarbon" means a compound containing carbon, hydrogen, fluorine, and chlorine.
[00026] A "bromofluorocarbon" means a compound containing carbon, hydrogen, fluorine, and bromine.
1000271 A bromochlorofluorcarbon means a compound containing carbon, hydrogen, fluorine, bromine, and chlorine.
100028i "Substantially all" means at least 90 % and up to 100 %.
1000291 "Optional" or "optionally" means that the subsequently described event or circumstance may, but need not, occur, and that the description includes instances where the event or circumstance occurs and instances in which it does not.
[00030] Most refrigeration systems utilize one or more gas turbines to drive the refrigeration compressors. Power generators are also driven by gas turbines in refrigeration systems. The combined output and efficiency of all gas turbines determines the total capacity of the refrigeration system. Refrigeration systems driven by one or more gas turbines are utilized in LNG production, air separation, food storage, and ice-making.
[00031] For example, LNG plants utilize one or more gas turbines to drive the refrigeration compressors required to liquefy the natural gas and power generators are also driven by gas turbines in the LNG plants. In LNG plants, a portion of the natural gas collected may also be utilized as a fuel for power generation for the LNG
plant, including for the gas turbines. The combined output and efficiency of all gas turbines determines the total capacity of the LNG plant.
[00032] The present application provides a method and a system which maximizes refrigeration systems driven by gas turbines in all seasons. In the present methods and systems substantially a small portion of refrigerant from the refrigeration system is consumed and the cooling from this process is used to reduce the temperature of inlet air entering gas turbines of the refrigeration system. The portion of refrigerant utilized for cooling the inlet air may be recycled to the refrigeration system.
[00033] Accordingly, with the present method and system, integration is utilized to increase the gas turbine power output and to efficiently provide refrigeration. Thus, the present method and system provide a gain in the efficiency in the refrigeration system operated by gas turbines.
[00034] One embodiment of the present method and system relates to LNG
production and the refrigeration facility is a LNG liquefaction plant. In LNG
methods and systems, natural gas is produced from a field or well. The produced supply of natural gas is collected. The LNG liquefaction plant is utilized to process substantially all of the natural gas stream. The inlet air to the gas turbines can be chilled with a portion of refrigerant from the refrigeration system. Optionally, the inlet air to the gas turbines can also be cooled with a portion of LNG, which is regasified.
1000351 in the present methods and systems, the effect of monthly temperature variation of the location on the capacity of the refrigeration facility is stabilized. The capacity of the refrigeration facility can be sensitive to environmental temperature variation. The capacity of the refrigeration facility is determined by the total output of the gas turbine machines in the refrigeration system and it is challenging to maintain the power output at a stable and maximum level.
1000361 According to the present methods and system, it has been surprisingly discovered that consuming a portion of the refrigerant from the refrigeration system and using the cooling effect to cool the inlet air for the gas turbines can maintain the power output of the facility at a stable and maximum level. By making inlet air to gas turbines stable and constant throughout the entire year, the plant (or capital) utilization efficiency is also greatly improved. The gain in energy efficiency by reducing the temperature of the inlet air entering the gas turbines can compensate for the consumption of refrigerant.
The optimal degrees of chilling are machine-specific.
1000371 The refrigeration system comprises a refrigeration loop. The refrigeration system can comprise a single stage or multi stage refrigeration loop. For example, the multistage refrigeration loop can be a two stage, three stage or four stage loop. In one embodiment, the refrigeration system comprises a two or three stage refrigeration loop.
When a multistage refrigeration loop is used, the consumed portion of refrigerant can come from the first stage of the refrigeration loop.
1000381 The refrigerant used in the refrigeration system can be any suitable refrigerant. Suitable refrigerants include methane, ethane, propane, ammonia, a hydrofluorocarbon, a chlorofluorocarbon, a hydrochlorofluorocarbon, a bromofluorocarbon, a bromochlorofluorcarbon, or any combination thereof [000391 The heat transfer can be indirect and involve the use of a heat transfer fluid. Any suitable heat transfer fluids can be used. Suitable heat transfer fluids include methanol, ethanol, a glycol and water mixture, or any combination thereof.
1000401 In one embodiment the refrigerant is propane and the heat transfer fluid is methanol.
1000411 The heat transfer can be either direct or indirect. The inlet air entering the gas turbine can be chilled by exchanging heat with a refrigerant in the refrigeration loop.
The inlet air can be chilled by exchanging heat with a heat transfer fluid, which has been cooled by exchanging heat with a refrigerant in the refrigeration loop. The inlet air can also be chilled by both.
100042] in one embodiment, the temperature of the inlet air entering the gas turbines can be reduced by 10 to 4017 from the ambient temperature of the refrigeration system. In an embodiment, the temperature of the inlet air entering the gas turbines can be reduced by at least 20 F from the ambient temperature. In another embodiment, the temperature of the inlet air entering the gas turbines can be reduced to a temperature in a range of from about 40 to 55 F or 45 to 55 'F. In an additional embodiment, the temperature of the inlet air entering the gas turbine can be reduced from an ambient temperature in a range of from about 60 to about 120 F to a temperature in a range of from about 45 to about 55 F. In a further embodiment, the temperature of the inlet air entering the gas turbine can be reduced from an ambient temperature in a range of from about 80 to about 120 F to a temperature in a range of from about 42 to about 60 "F.
1000431 In one embodiment, the efficiency of the gas turbines is increased by at least 3 %. The efficiency may be increased by at least 3 % by reducing the temperature of the inlet air from an ambient temperature of 90 F to a temperature of 50 F.
100044] By maintaining the inlet air for the gas turbines at a constant low temperature, the amount of power generated by the turbine remains high regardless of the ambient air temperature. By carefully regulating the refrigerant to be consumed for cooling, it is possible to control the refrigeration supply and maintain the inlet air to a gas turbine at a cool and stable level. Thus, the gas turbine output and efficiency can be maximized in all seasons and in all climates.
1000451 For facilities in tropical regions that have high average temperatures, which relatively stable, the present system and methods can be utilized to lower the average values to maximize turbine output. In the Arctic with low temperatures and large seasonal variations, the present system and methods can be utilized to mitigate the seasonal variations. In the desert with high average temperatures and large seasonal variation, the present system and methods can be utilized to lower the average temperature and maintain the stability of the temperature. Figure 2 is a graph showing the monthly temperature variations at three locations. The portion of the refrigerant to be consumed is utilized to control the inlet air temperature and maintain the power output at a steady, maximum level. Therefore, facilities for refrigeration, including facilities for LNG production, can be built at a variety of locations without concern that the ambient
One system uses evaporative cooling, another uses a chiller to chill water that is then run through a coil. However, a continuing need exists for a turbine inlet air cooling system and method which is efficient and does not drain the system of power.
Summary of the Invention 100071 As described herein, a method and system for maximizing gas turbine output for a refrigeration loop are provided. The method and system provide a gain in energy efficiency of the gas turbine while compensating for an amount of energy required for consuming a portion of refrigerant.
100081 In one embodiment disclosed herein is an integrated system for refrigeration. The system comprises (a) a refrigeration system comprising a refrigeration loop for air-chilling; (b) a gas turbine for driving a compressor for the refrigeration system; (c) a heat exchanger for consuming a portion of refrigerant from the refrigeration system and cooling a heat transfer fluid; and (d) a second heat exchanger for reducing the temperature of inlet air entering the gas turbine with the heat transfer fluid.
[00091 In another embodiment disclosed herein is an integrated method of maximizing gas turbine output for a refrigeration loop. The method comprises (a) operating a refrigeration loop for chilling processes; (b) operating a gas turbine to drive a compressor for a the refrigeration loop; (c) gasifying a portion of refrigerant from the refrigeration system; and (d) reducing the temperature of inlet air entering the gas turbines by exchanging heat with the gasified portion of refrigerant either directly or indirectly.
[000101 In an additional embodiment disclosed herein is an integrated method of operating a gas turbine used in a refrigeration loop. The method comprises (a) operating a gas turbine to drive a compressor for a refrigeration system comprising a refrigeration loop and (b) chilling inlet air entering the gas turbine by (i) exchanging heat with a refrigerant in the refrigeration loop; or (ii) cooling a heat transfer fluid with a refrigerant in the refrigeration loop, and chilling inlet air entering the gas turbine by exchanging heat with the heat transfer fluid; or both (i) and (ii). In the method the refrigerant in the refrigeration loop comprises methane, ethane, propane, ammonia, a hydrofluorocarbon, a chlorofluorocarbon, a hydrochlorofluorocarbon, a bromofluorocarbon, a bromochlorofluorocarbon, or any combination thereof; and the heat transfer fluid comprises methanol, ethanol, a glycol and water mixture, or any combination thereof. In this method the gas turbine and refrigeration system can be used to produce LNG and the method further comprises cooling and condensing a natural gas stream by reducing the temperature of the natural gas using the refrigeration system.
1000111 In another embodiment disclosed herein is an integrated liquefied natural gas (LNG) system. The system comprises (a) an inlet stream comprising natural gas; (b) a refrigeration system for reducing the temperature of the natural gas and condensing the natural gas to produce LNG; (c) a gas turbine for driving a compressor for the refrigeration system; (d) a first vaporization heat exchanger for regasifying a portion of the LNG and cooling a heat transfer fluid; (e) a second vaporization heat exchanger for consuming a portion of refrigerant from the refrigeration system and cooling the heat transfer fluid; and (f) a third heat exchanger for reducing the temperature of inlet air entering the gas turbine with the heat transfer fluid. The integrated system can further comprise an outlet pipeline for supplying the regasified portion of the LNG to the domestic gas market.
[000121 In a further embodiment discloses herein is an integrated method for operating a liquefied natural gas (LNG) plant, the method comprising: (i) cooling and condensing a natural gas stream. in a refrigeration system to produce liquefied natural gas (LNG); (ii) operating a gas turbine to drive a compressor for the refrigeration system;
(iii) regasifying a portion of the LNG; (iv) consuming a portion of the refrigerant from the refrigeration system; and (iv) reducing the temperature of inlet air entering the gas turbine by exchanging heat with the regasified portion of the LNG and with the consumed portion of the refrigerant directly or indirectly.
Brief Description of the Drawines 1000131 Figure 1 illustrates an embodiment of the proposed refrigeration loop.
[OHM Figure 2 is a graph showing the monthly temperature variations at three locations for LNG and domestic natural gas production.
Detailed Description of the Invention 100151 In the prc-:c.rit methods and systems, a portion of refrigerant from the refrigeration system is utilized to cool the inlet air to the gas turbines in the refrigeration system, either directly or indirectly.
Definitions PON In accordance with this detailed description, the following abbreviations and definitions apply. It must be noted that as used herein, the singular forms "a", "an", and "the" include plural referents unless the context clearly dictates otherwise. Thus, for example, reference to "gas turbine" includes a plurality of such.
[00017] Unless otherwise stated, the following terms used in the specification and claims have the meanings given below:
[00018] "LNG" is liquefied natural gas. Natural gas from the well can consist of various hydrocarbons and contaminants; natural gas for the domestic market is comprised primarily of methane. At ambient temperature and pressure, LNG
exists as a gas, but it can be cooled and/or pressurized to provide a liquid, which facilitates storage and transportation.
[00019] "Remote location or market" means a location that is not readily accessible or economically feasible to access by pipeline. For example, a remote location or market can be at least over a thousand miles away from the natural gas source and/or is separated in geography such that it is not accessible by pipeline, for example, separated by oceans or other large, deep bodies of water.
[000201 "Local market" means a location that is within a distance and geography from the natural gas source so that the natural gas may be supplied as a gas by pipeline.
For example, local markets can be at any distance within several thousand miles from the natural gas source and is accessible by pipeline.
[00021] "Direct" in the context of heat exchange means that the heat exchange between the refrigerant and the inlet air is direct with no intermediate heat transfer fluid involved.
1000221 "Indirect" in the context of heat exchange means that the heat exchange between the refrigerant and the inlet air involves an intermediate heat transfer fluid.
Accordingly, the temperature of inlet air entering the gas turbine is reduced by exchanging heat with the refrigerant through a heat transfer fluid system.
[00023] "Integrated" means that the steps or units of the system or interconnected so that when operating together greater efficiencies are realized in comparison to when operating independently.
1000241 A "hydrofluorocarbon" means a compound containing carbon, hydrogen, and fluorine.
[00025] A "chlorofluorocarbon" means a compound containing carbon, hydrogen, fluorine, and chlorine.
[00026] A "bromofluorocarbon" means a compound containing carbon, hydrogen, fluorine, and bromine.
1000271 A bromochlorofluorcarbon means a compound containing carbon, hydrogen, fluorine, bromine, and chlorine.
100028i "Substantially all" means at least 90 % and up to 100 %.
1000291 "Optional" or "optionally" means that the subsequently described event or circumstance may, but need not, occur, and that the description includes instances where the event or circumstance occurs and instances in which it does not.
[00030] Most refrigeration systems utilize one or more gas turbines to drive the refrigeration compressors. Power generators are also driven by gas turbines in refrigeration systems. The combined output and efficiency of all gas turbines determines the total capacity of the refrigeration system. Refrigeration systems driven by one or more gas turbines are utilized in LNG production, air separation, food storage, and ice-making.
[00031] For example, LNG plants utilize one or more gas turbines to drive the refrigeration compressors required to liquefy the natural gas and power generators are also driven by gas turbines in the LNG plants. In LNG plants, a portion of the natural gas collected may also be utilized as a fuel for power generation for the LNG
plant, including for the gas turbines. The combined output and efficiency of all gas turbines determines the total capacity of the LNG plant.
[00032] The present application provides a method and a system which maximizes refrigeration systems driven by gas turbines in all seasons. In the present methods and systems substantially a small portion of refrigerant from the refrigeration system is consumed and the cooling from this process is used to reduce the temperature of inlet air entering gas turbines of the refrigeration system. The portion of refrigerant utilized for cooling the inlet air may be recycled to the refrigeration system.
[00033] Accordingly, with the present method and system, integration is utilized to increase the gas turbine power output and to efficiently provide refrigeration. Thus, the present method and system provide a gain in the efficiency in the refrigeration system operated by gas turbines.
[00034] One embodiment of the present method and system relates to LNG
production and the refrigeration facility is a LNG liquefaction plant. In LNG
methods and systems, natural gas is produced from a field or well. The produced supply of natural gas is collected. The LNG liquefaction plant is utilized to process substantially all of the natural gas stream. The inlet air to the gas turbines can be chilled with a portion of refrigerant from the refrigeration system. Optionally, the inlet air to the gas turbines can also be cooled with a portion of LNG, which is regasified.
1000351 in the present methods and systems, the effect of monthly temperature variation of the location on the capacity of the refrigeration facility is stabilized. The capacity of the refrigeration facility can be sensitive to environmental temperature variation. The capacity of the refrigeration facility is determined by the total output of the gas turbine machines in the refrigeration system and it is challenging to maintain the power output at a stable and maximum level.
1000361 According to the present methods and system, it has been surprisingly discovered that consuming a portion of the refrigerant from the refrigeration system and using the cooling effect to cool the inlet air for the gas turbines can maintain the power output of the facility at a stable and maximum level. By making inlet air to gas turbines stable and constant throughout the entire year, the plant (or capital) utilization efficiency is also greatly improved. The gain in energy efficiency by reducing the temperature of the inlet air entering the gas turbines can compensate for the consumption of refrigerant.
The optimal degrees of chilling are machine-specific.
1000371 The refrigeration system comprises a refrigeration loop. The refrigeration system can comprise a single stage or multi stage refrigeration loop. For example, the multistage refrigeration loop can be a two stage, three stage or four stage loop. In one embodiment, the refrigeration system comprises a two or three stage refrigeration loop.
When a multistage refrigeration loop is used, the consumed portion of refrigerant can come from the first stage of the refrigeration loop.
1000381 The refrigerant used in the refrigeration system can be any suitable refrigerant. Suitable refrigerants include methane, ethane, propane, ammonia, a hydrofluorocarbon, a chlorofluorocarbon, a hydrochlorofluorocarbon, a bromofluorocarbon, a bromochlorofluorcarbon, or any combination thereof [000391 The heat transfer can be indirect and involve the use of a heat transfer fluid. Any suitable heat transfer fluids can be used. Suitable heat transfer fluids include methanol, ethanol, a glycol and water mixture, or any combination thereof.
1000401 In one embodiment the refrigerant is propane and the heat transfer fluid is methanol.
1000411 The heat transfer can be either direct or indirect. The inlet air entering the gas turbine can be chilled by exchanging heat with a refrigerant in the refrigeration loop.
The inlet air can be chilled by exchanging heat with a heat transfer fluid, which has been cooled by exchanging heat with a refrigerant in the refrigeration loop. The inlet air can also be chilled by both.
100042] in one embodiment, the temperature of the inlet air entering the gas turbines can be reduced by 10 to 4017 from the ambient temperature of the refrigeration system. In an embodiment, the temperature of the inlet air entering the gas turbines can be reduced by at least 20 F from the ambient temperature. In another embodiment, the temperature of the inlet air entering the gas turbines can be reduced to a temperature in a range of from about 40 to 55 F or 45 to 55 'F. In an additional embodiment, the temperature of the inlet air entering the gas turbine can be reduced from an ambient temperature in a range of from about 60 to about 120 F to a temperature in a range of from about 45 to about 55 F. In a further embodiment, the temperature of the inlet air entering the gas turbine can be reduced from an ambient temperature in a range of from about 80 to about 120 F to a temperature in a range of from about 42 to about 60 "F.
1000431 In one embodiment, the efficiency of the gas turbines is increased by at least 3 %. The efficiency may be increased by at least 3 % by reducing the temperature of the inlet air from an ambient temperature of 90 F to a temperature of 50 F.
100044] By maintaining the inlet air for the gas turbines at a constant low temperature, the amount of power generated by the turbine remains high regardless of the ambient air temperature. By carefully regulating the refrigerant to be consumed for cooling, it is possible to control the refrigeration supply and maintain the inlet air to a gas turbine at a cool and stable level. Thus, the gas turbine output and efficiency can be maximized in all seasons and in all climates.
1000451 For facilities in tropical regions that have high average temperatures, which relatively stable, the present system and methods can be utilized to lower the average values to maximize turbine output. In the Arctic with low temperatures and large seasonal variations, the present system and methods can be utilized to mitigate the seasonal variations. In the desert with high average temperatures and large seasonal variation, the present system and methods can be utilized to lower the average temperature and maintain the stability of the temperature. Figure 2 is a graph showing the monthly temperature variations at three locations. The portion of the refrigerant to be consumed is utilized to control the inlet air temperature and maintain the power output at a steady, maximum level. Therefore, facilities for refrigeration, including facilities for LNG production, can be built at a variety of locations without concern that the ambient
7 air temperatures will affect the efficiency. During cold seasons or climates, the air conditioning requirement provided by the consumed refrigerant is reduced.
[000361 The gain in gas turbine output and efficiency can compensate for cost for the additional refrigerant that is consumed. The gain may be measured over the seasonal variations for climates with cold seasons and the additional production during colder seasons can be used to compensate for the additional energy required for initial refrigeration durin.g wanner seasons.
1000471 One embodiment of the method and system is illustrated in Figure 1. A
refrigeration system is provided for air-chilling. The refrigeration system comprises a two stage refrigeration loop. A gas turbine drives a compressor for the refrigeration system. In the system, a portion of refrigerant is consumed and used for cooling the inlet air entering the gas turbine of the refrigeration system. The refrigerant can cool the inlet air either directly or indirectly through the use of an intermediate heat transfer fluid.
1000481 In one embodiment a heat exchanger transfers heat from the portion of refrigerant to be consumed and cools an intermediate heat transfer fluid. A
second heat transfer exchanger exchanges heat from the intermediate heat transfer fluid and reduces the temperature of inlet air entering the gas turbine. The second heat exchanger can comprise a cooling coil at an inlet of the gas turbine.
[00049] In one embodiment, the portion of refrigerant to be consumed is withdrawn from the first refrigeration loop. The portion of refrigerant to be consumed can be in a range of from 5 to 25% by weight of the total refrigerant. In one embodiment the portion of refrigerant to be consumed can be in a range of from about 10 to 25% by weight of the total refrigerant.
1000501 The refrigerant prior to reducing the temperature of the inlet air can be at a temperature of about -45 to about 45 F. In another embodiment, the refrigerant prior to reducing the temperature of the inlet air can be at a temperature of about -45 to about 30 F. When an intermediate heat transfer fluid is utilized for indirect heat transfer, the temperature of the heat transfer fluid prior to reducing the temperature of the inlet air can be at a temperature of about -45 to about 30 F. In another embodiment, the temperature of the heat transfer fluid prior to reducing the temperature of the inlet air can be at a temperature of about -45 to about 0 F. In a two stage refrigeration loop, the temperature of the refrigerant in the second loop can be in the range of about -100 to about 0 F.
[00051] After the cooling is complete, at least a portion of the consumed refrigerant can be recycled back to the refrigeration loop if desired.
[000361 The gain in gas turbine output and efficiency can compensate for cost for the additional refrigerant that is consumed. The gain may be measured over the seasonal variations for climates with cold seasons and the additional production during colder seasons can be used to compensate for the additional energy required for initial refrigeration durin.g wanner seasons.
1000471 One embodiment of the method and system is illustrated in Figure 1. A
refrigeration system is provided for air-chilling. The refrigeration system comprises a two stage refrigeration loop. A gas turbine drives a compressor for the refrigeration system. In the system, a portion of refrigerant is consumed and used for cooling the inlet air entering the gas turbine of the refrigeration system. The refrigerant can cool the inlet air either directly or indirectly through the use of an intermediate heat transfer fluid.
1000481 In one embodiment a heat exchanger transfers heat from the portion of refrigerant to be consumed and cools an intermediate heat transfer fluid. A
second heat transfer exchanger exchanges heat from the intermediate heat transfer fluid and reduces the temperature of inlet air entering the gas turbine. The second heat exchanger can comprise a cooling coil at an inlet of the gas turbine.
[00049] In one embodiment, the portion of refrigerant to be consumed is withdrawn from the first refrigeration loop. The portion of refrigerant to be consumed can be in a range of from 5 to 25% by weight of the total refrigerant. In one embodiment the portion of refrigerant to be consumed can be in a range of from about 10 to 25% by weight of the total refrigerant.
1000501 The refrigerant prior to reducing the temperature of the inlet air can be at a temperature of about -45 to about 45 F. In another embodiment, the refrigerant prior to reducing the temperature of the inlet air can be at a temperature of about -45 to about 30 F. When an intermediate heat transfer fluid is utilized for indirect heat transfer, the temperature of the heat transfer fluid prior to reducing the temperature of the inlet air can be at a temperature of about -45 to about 30 F. In another embodiment, the temperature of the heat transfer fluid prior to reducing the temperature of the inlet air can be at a temperature of about -45 to about 0 F. In a two stage refrigeration loop, the temperature of the refrigerant in the second loop can be in the range of about -100 to about 0 F.
[00051] After the cooling is complete, at least a portion of the consumed refrigerant can be recycled back to the refrigeration loop if desired.
8 1000521 The gas turbine of the refrigeration compressors condenses water vapor from the ambient air of the facility. The power generator for the facility may also condense water vapor from the ambient air. This condensed water is distilled quality water. Accordingly, the condensed water can be collected and used for other uses in the plant. For example, it can be used for wet compression, evaporative cooling, and/or fogging the inlet air to the gas turbines. The water can be used as plant process water such as hydrogen sulfide removal by passing natural gas through water or amine based solution. The water can be used for compressor circulation cooling and inlet humidity adjustment. Because it is distilled quality water, it can also be used for any use for which distilled water may be needed in the area of the plant. For example, it can be used as a source for drinking water or irrigation water as well. A source for drinking water or irrigation water may be particularly useful in desert locations.
[00053] The gas turbine according to the methods and systems described herein can be used to drive a compressor in the refrigeration system. The gas turbine can also be used to drive a steam generator or can be configured to generate electricity.
Refrigeration systems driven by the one or more gas turbines can be utilized in LNG
production, air separation, food storage, and ice-making.
[000541 In one embodiment, the presently claimed integrated refrigeration system and method can be used in a liquefied natural gas system. The liquefied natural gas system can have addition integration for chilling the inlet air of the gas turbines. Such an integrated LNG system and method are described in U.S. Patent Application entitled "Method to Maximize LNG Plant Capacity", filed 30 December 2010, Attorney Docket No. 70205.022 ISO!, the contents of which are herein incorporated by reference in their entirety. In this integrated liquefied natural gas system, natural gas is produced from a field or well and the produced supply of natural gas is collected as an inlet stream.
[00055] The inlet stream of natural gas is fed to a refrigeration system for reducing the temperature of the natural gas and condensing the natural gas to produce LNG (a liquefaction and refrigeration unit. The refrigeration system may be a single stage or multistage stage refrigeration loop. One or more gas turbines drive a compressor for the refrigeration system.
1000561 The liquefied product is then sent to a storage tank. From the storage tank, LNG can be collected to ship or transport to a remote market.
[00057] According to the integrated LNG system and method, a portion of the LNG is taken from the collection/storage tank for regasification. The portion of LNG is
[00053] The gas turbine according to the methods and systems described herein can be used to drive a compressor in the refrigeration system. The gas turbine can also be used to drive a steam generator or can be configured to generate electricity.
Refrigeration systems driven by the one or more gas turbines can be utilized in LNG
production, air separation, food storage, and ice-making.
[000541 In one embodiment, the presently claimed integrated refrigeration system and method can be used in a liquefied natural gas system. The liquefied natural gas system can have addition integration for chilling the inlet air of the gas turbines. Such an integrated LNG system and method are described in U.S. Patent Application entitled "Method to Maximize LNG Plant Capacity", filed 30 December 2010, Attorney Docket No. 70205.022 ISO!, the contents of which are herein incorporated by reference in their entirety. In this integrated liquefied natural gas system, natural gas is produced from a field or well and the produced supply of natural gas is collected as an inlet stream.
[00055] The inlet stream of natural gas is fed to a refrigeration system for reducing the temperature of the natural gas and condensing the natural gas to produce LNG (a liquefaction and refrigeration unit. The refrigeration system may be a single stage or multistage stage refrigeration loop. One or more gas turbines drive a compressor for the refrigeration system.
1000561 The liquefied product is then sent to a storage tank. From the storage tank, LNG can be collected to ship or transport to a remote market.
[00057] According to the integrated LNG system and method, a portion of the LNG is taken from the collection/storage tank for regasification. The portion of LNG is
9 regasified in a regasification unit. The portion of the LNG to be regasified can be in the range of from 5% to 25% by weight of the total LNG produced. In another embodiment, the portion of the LNG to be regasified can be in the range of from 10% to 20%
by weight of the total LNG produced. The regasification unit can be a vaporization heat exchanger for regasifying the portion of the LNG and cooling a heat transfer fluid. The heat transfer fluid can comprise methanol, ethanol, propane, an ethylene glycol and water mixture or any combination thereof. The heat transfer fluid can also take additional heat or refrigeration from auxiliary sources.
1000581 in the present methods and system, the heat transfer fluid takes additional refrigeration from the refrigeration loop comprising refrigerant. A second vaporization heat exchanger is present for consuming a portion of the refrigerant of the refrigeration loop and further cooling the heat transfer fluid.
[000591 A third heat exchanger is utilized for reducing the temperature of inlet air entering the gas turbine with the heat transfer fluid. This heat exchanger can comprise a cooling coil at an inlet of the gas turbine.
[000601 Thus, the portion of LNG to be regasified and the refrigerant to be consumed releases refrigeration and this is used to reduce the temperature of inlet air entering gas turbines of the refrigeration system in the LNG plant either directly or indirectly. As such, the temperature of inlet air is reduced by exchanging heat either directly or indirectly with the regasified portion of the LNG and the refrigerant. In one embodiment, the heat is exchanged indirectly through the use of an intermediate heat transfer fluid.
1000611 In this integrated LNG method and system, the regasified portion of LNG can be supplied to an outlet pipeline for supplying the regasified LNG to the domestic gas market.
[000621 The regasified LNG can be supplied to a natural gas pipeline for domestic or local natural gas production. By taking the inlet natural gas stream and creating LNG
and then using the regasified LNG as the stream for the local natural gas market, the natural gas stream for the local market has any contaminants removed by the LNG
process. Therefore, a separate facility is not required to remove contaminants, such as sulfur and carbon dioxide, from the natural gas before providing it to the domestic energy market.
1000631 If the regasified portion of the LNG is not needed for domestic natural gas production, or it is not all needed, the regasified LNG, or a portion of the regasified LNG, can be recycled to the refrigeration system to provide LNG.
[000641 The regasified LNG does not require an additional separate cleaning facility prior to use as domestic natural gas because it is cleaned sufficiently in the liquefaction process. Accordingly, the regasified portion of the LNG can be exported directly by pipeline for use in a local or domestic natural gas market.
Because the regasified LNG has substantially all contaminants removed by the LNG process, the regasified LNG is cleaner than natural gas typically recovered for local or domestic market production. Natural gas recovered for local or domestic market production is processed to remove contaminants, such as sulfur and carbon dioxide, to meet pipeline specifications.
[00065] The regasified LNG can also be used to blend with natural gas directly collected for domestic production to meet pipeline specifications. When the regasified LNG is blended with natural gas, the natural gas can be processed less severely removing fewer contaminants so that the natural gas alone would not meet pipeline specifications.
But the blend can meet pipeline specifications. The regasified LNG can be blended with natural gas, which has been not processed or has been processed less severely, and the blend meets pipeline specifications. For example, in cooler seasons it may be possible to blend high purity, regasified LNG with unprocessed or less processed natural gas and meet pipeline specifications for domestic gas production.
[000661 The gas turbine of the refrigeration compressors condenses water vapor from the ambient air of the facility. The power generator for the LNG plant may also condense water vapor from the ambient air. This condensed water is distilled quality water. Accordingly, the condensed water can be collected and used for other uses in the plant. For example, it can be used for wet compression, evaporative cooling, and/or fogging the inlet air to the gas turbines. The water can be used as plant process water such as hydrogen sulfide removal by passing natural gas through water or amine based solution. The water can be used for compressor circulation cooling and inlet humidity adjustment. Because it is distilled quality water, it can also be used for any use for which distilled water may be needed in the area of the plant. For example, it can be used as a source for drinking water or irrigation water as well. A source for drinking water or irrigation water may be particularly useful in desert locations.
1000671 Accordingly, with the present method and system, integration is utilized to increase the gas turbine power output in the LNG plant and to provide a natural gas stream suitable for the domestic or local natural gas market. The gain in energy efficiency by reducing the temperature of the inlet air entering the gas turbines can compensate for the amount of energy required to produce the portion of LNG, which is later regasified and can compensate for the refrigerant that is consumed.
1000681 In the integrated methods for operating a liquefied natural gas plant as disclosed herein, a single liquefied natural gas plant is utilized to create natural gas for a local gas market and liquefied natural gas for transport to a remote market.
The process comprises cooling and condensing a natural gas stream in a LNG facility comprising a refrigeration system to produce LNG. One or more gas turbines are used to operate compressors for the refrigeration system of the LNG plant. A portion of the LNG is taken to be regasified. A portion of the refrigerant from the refrigeration is system is consumed. The temperature of inlet air entering the gas turbines of the refrigeration system is reduced by exchanging heat with the portion of the LNG to be regasified and with the refrigerant to be consumed, either directly or indirectly. In certain embodiments, an intermediate heat transfer fluid is used to take refrigeration from the portion of the LNG to be regasified and from the consumed refrigerant and the intermediate heat transfer fluid is used to cool the inlet air. The LNG
produced from the facility is shipped to remote markets and at least a portion of the regasified LNG can be supplied to an outlet pipeline for local gas markets.
1000691 In the presently disclosed methods and system, the improvement comprises consuming a portion of the refrigerant to cool inlet air to the gas turbines. In the integrated LNG method and systems, the improvement further comprises converting substantially all of the produced natural gas stream from a well or field to LNG and then regasifying a portion. In regasifying a portion of the LNG, the regasification process is also used to chill inlet air to gas turbines used in the refrigeration system of the LNG
plant. This approach enhances the GT power output and efficiency which, in turn, increases the LNG production of the plant. The gain in efficiency in LNG
production can compensate for the additional cost in energy and consumption of the refrigerant.
1000701 While the invention has been described in detail and with reference to specific embodiments thereof, it will be apparent to one skilled in the art that various changes and modifications can be made without departing from the spirit and scope thereof.
by weight of the total LNG produced. The regasification unit can be a vaporization heat exchanger for regasifying the portion of the LNG and cooling a heat transfer fluid. The heat transfer fluid can comprise methanol, ethanol, propane, an ethylene glycol and water mixture or any combination thereof. The heat transfer fluid can also take additional heat or refrigeration from auxiliary sources.
1000581 in the present methods and system, the heat transfer fluid takes additional refrigeration from the refrigeration loop comprising refrigerant. A second vaporization heat exchanger is present for consuming a portion of the refrigerant of the refrigeration loop and further cooling the heat transfer fluid.
[000591 A third heat exchanger is utilized for reducing the temperature of inlet air entering the gas turbine with the heat transfer fluid. This heat exchanger can comprise a cooling coil at an inlet of the gas turbine.
[000601 Thus, the portion of LNG to be regasified and the refrigerant to be consumed releases refrigeration and this is used to reduce the temperature of inlet air entering gas turbines of the refrigeration system in the LNG plant either directly or indirectly. As such, the temperature of inlet air is reduced by exchanging heat either directly or indirectly with the regasified portion of the LNG and the refrigerant. In one embodiment, the heat is exchanged indirectly through the use of an intermediate heat transfer fluid.
1000611 In this integrated LNG method and system, the regasified portion of LNG can be supplied to an outlet pipeline for supplying the regasified LNG to the domestic gas market.
[000621 The regasified LNG can be supplied to a natural gas pipeline for domestic or local natural gas production. By taking the inlet natural gas stream and creating LNG
and then using the regasified LNG as the stream for the local natural gas market, the natural gas stream for the local market has any contaminants removed by the LNG
process. Therefore, a separate facility is not required to remove contaminants, such as sulfur and carbon dioxide, from the natural gas before providing it to the domestic energy market.
1000631 If the regasified portion of the LNG is not needed for domestic natural gas production, or it is not all needed, the regasified LNG, or a portion of the regasified LNG, can be recycled to the refrigeration system to provide LNG.
[000641 The regasified LNG does not require an additional separate cleaning facility prior to use as domestic natural gas because it is cleaned sufficiently in the liquefaction process. Accordingly, the regasified portion of the LNG can be exported directly by pipeline for use in a local or domestic natural gas market.
Because the regasified LNG has substantially all contaminants removed by the LNG process, the regasified LNG is cleaner than natural gas typically recovered for local or domestic market production. Natural gas recovered for local or domestic market production is processed to remove contaminants, such as sulfur and carbon dioxide, to meet pipeline specifications.
[00065] The regasified LNG can also be used to blend with natural gas directly collected for domestic production to meet pipeline specifications. When the regasified LNG is blended with natural gas, the natural gas can be processed less severely removing fewer contaminants so that the natural gas alone would not meet pipeline specifications.
But the blend can meet pipeline specifications. The regasified LNG can be blended with natural gas, which has been not processed or has been processed less severely, and the blend meets pipeline specifications. For example, in cooler seasons it may be possible to blend high purity, regasified LNG with unprocessed or less processed natural gas and meet pipeline specifications for domestic gas production.
[000661 The gas turbine of the refrigeration compressors condenses water vapor from the ambient air of the facility. The power generator for the LNG plant may also condense water vapor from the ambient air. This condensed water is distilled quality water. Accordingly, the condensed water can be collected and used for other uses in the plant. For example, it can be used for wet compression, evaporative cooling, and/or fogging the inlet air to the gas turbines. The water can be used as plant process water such as hydrogen sulfide removal by passing natural gas through water or amine based solution. The water can be used for compressor circulation cooling and inlet humidity adjustment. Because it is distilled quality water, it can also be used for any use for which distilled water may be needed in the area of the plant. For example, it can be used as a source for drinking water or irrigation water as well. A source for drinking water or irrigation water may be particularly useful in desert locations.
1000671 Accordingly, with the present method and system, integration is utilized to increase the gas turbine power output in the LNG plant and to provide a natural gas stream suitable for the domestic or local natural gas market. The gain in energy efficiency by reducing the temperature of the inlet air entering the gas turbines can compensate for the amount of energy required to produce the portion of LNG, which is later regasified and can compensate for the refrigerant that is consumed.
1000681 In the integrated methods for operating a liquefied natural gas plant as disclosed herein, a single liquefied natural gas plant is utilized to create natural gas for a local gas market and liquefied natural gas for transport to a remote market.
The process comprises cooling and condensing a natural gas stream in a LNG facility comprising a refrigeration system to produce LNG. One or more gas turbines are used to operate compressors for the refrigeration system of the LNG plant. A portion of the LNG is taken to be regasified. A portion of the refrigerant from the refrigeration is system is consumed. The temperature of inlet air entering the gas turbines of the refrigeration system is reduced by exchanging heat with the portion of the LNG to be regasified and with the refrigerant to be consumed, either directly or indirectly. In certain embodiments, an intermediate heat transfer fluid is used to take refrigeration from the portion of the LNG to be regasified and from the consumed refrigerant and the intermediate heat transfer fluid is used to cool the inlet air. The LNG
produced from the facility is shipped to remote markets and at least a portion of the regasified LNG can be supplied to an outlet pipeline for local gas markets.
1000691 In the presently disclosed methods and system, the improvement comprises consuming a portion of the refrigerant to cool inlet air to the gas turbines. In the integrated LNG method and systems, the improvement further comprises converting substantially all of the produced natural gas stream from a well or field to LNG and then regasifying a portion. In regasifying a portion of the LNG, the regasification process is also used to chill inlet air to gas turbines used in the refrigeration system of the LNG
plant. This approach enhances the GT power output and efficiency which, in turn, increases the LNG production of the plant. The gain in efficiency in LNG
production can compensate for the additional cost in energy and consumption of the refrigerant.
1000701 While the invention has been described in detail and with reference to specific embodiments thereof, it will be apparent to one skilled in the art that various changes and modifications can be made without departing from the spirit and scope thereof.
Claims
What is claimed is:
1. An integrated system for refrigeration comprising:
(a) a refrigeration system comprising a refrigeration loop for air-chilling;
(b) a gas turbine for driving a compressor for the refrigeration system;
(c) a heat exchanger for consuming a portion of refrigerant from the refrigeration system and cooling a heat transfer fluid; and (d) a second heat exchanger for reducing the temperature of inlet air entering the gas turbine with the heat transfer fluid.
2. The integrated system of claim 1, wherein the portion of the refrigerant consumed is in a range from 5% to 25% by weight or wherein the portion of the refrigerant consumed is in a range from 10% to 20% by weight.
3. The integrated system of claim 1, wherein the second heat exchanger comprises a cooling coil at an inlet of the gas turbine.
4. The integrated system of claim 1, wherein the temperature of the inlet air entering the gas turbine is reduced to a temperature in a range from about 45 to about °F.
5. The integrated system of claim 1, wherein the refrigerant prior to reducing the temperature of the inlet air is at a temperature of from about -45 to about 45 °F.
6. The integrated system of claim 1, wherein the heat transfer fluid prior to reducing the temperature of the inlet air is at a temperature of from about -45 to about 30 °F.
7. The integrated system of claim 1, wherein the refrigerant comprises propane and the heat transfer fluid comprises methanol.
8. An integrated method of maximizing gas turbine output for a refrigeration loop comprising:
(a) operating a refrigeration loop for chilling processes;
(b) operating a gas turbine to drive a compressor for a the refrigeration loop;
(c) gasifying a portion of refrigerant from the refrigeration system; and (d) reducing the temperature of inlet air entering the gas turbines by exchanging heat with the gasified portion of refrigerant either directly or indirectly.
9. The integrated method of claims 1 or 8, wherein the refrigeration is for LNG
production, air separation, food storage, or ice-making.
10. The integrated method of claims 1 or 8, comprising a single stage, two stage, or three stage refrigeration loop.
11. The integrated method of claims 1 or 8, wherein the refrigerant comprises methane, ethane, propane, ammonia, a hydrofluorocarbon, a chlorofluorocarbon, a hydrochlorofluorocarbon, a bromofluorocarbon, a bromochlorofluorocarbon, or any combination thereof.
12. The integrated method of claims 1 or 8, wherein a gain in energy efficiency by reducing the temperature of the inlet air entering the gas turbine compensates for an amount of energy required for chilling and consuming the portion of refrigerant in step (c).
13. The integrated method of claim 8, wherein the temperature of inlet air is reduced by exchanging heat indirectly with the regasified portion of refrigerant using an intermediate heat transfer fluid.
14. The integrated method of claims 1 or 8, wherein the heat transfer fluid comprises methanol, ethanol, a glycol and water mixture, or any combination thereof.
15. The integrated method of claims 1 or 8, wherein the temperature of the inlet air entering the gas turbine is reduced by 10 to 40 °F from ambient temperature.
16. The integrated method of claims 1 or 8, wherein the temperature of the inlet air entering the gas turbine is reduced from an ambient temperature in a range from about 60 to about 120 °F to a temperature in a range from about 45 to about 55 is increased by at least 3 % by reducing the temperature of the inlet air from 90 to 50 °F.
18. The integrated method of claim 8, further comprising recycling at least a portion of the consumed refrigerant to the refrigeration loop.
19. The method of claim 8, further comprising a step of collecting water condensed from reducing the temperature of the inlet air.
20. An integrated method for operating a liquefied natural gas (LNG) plant, the method comprising:
(i) cooling and condensing a natural gas stream in a refrigeration system to produce liquefied natural gas (LNG);
(ii) operating a gas turbine to drive a compressor for the refrigeration system;
(iii) regasifying a portion of the LNG;
(iv) consuming a portion of the refrigerant from the refrigeration system; and (iv) reducing the temperature of inlet air entering the gas turbine by exchanging heat with the regasified portion of the LNG and with the consumed portion of the refrigerant directly or indirectly.
21. The integrated method of claim 20 further comprising supplying at least a portion of the regasified portion of the LNG to an outlet pipeline.
1. An integrated system for refrigeration comprising:
(a) a refrigeration system comprising a refrigeration loop for air-chilling;
(b) a gas turbine for driving a compressor for the refrigeration system;
(c) a heat exchanger for consuming a portion of refrigerant from the refrigeration system and cooling a heat transfer fluid; and (d) a second heat exchanger for reducing the temperature of inlet air entering the gas turbine with the heat transfer fluid.
2. The integrated system of claim 1, wherein the portion of the refrigerant consumed is in a range from 5% to 25% by weight or wherein the portion of the refrigerant consumed is in a range from 10% to 20% by weight.
3. The integrated system of claim 1, wherein the second heat exchanger comprises a cooling coil at an inlet of the gas turbine.
4. The integrated system of claim 1, wherein the temperature of the inlet air entering the gas turbine is reduced to a temperature in a range from about 45 to about °F.
5. The integrated system of claim 1, wherein the refrigerant prior to reducing the temperature of the inlet air is at a temperature of from about -45 to about 45 °F.
6. The integrated system of claim 1, wherein the heat transfer fluid prior to reducing the temperature of the inlet air is at a temperature of from about -45 to about 30 °F.
7. The integrated system of claim 1, wherein the refrigerant comprises propane and the heat transfer fluid comprises methanol.
8. An integrated method of maximizing gas turbine output for a refrigeration loop comprising:
(a) operating a refrigeration loop for chilling processes;
(b) operating a gas turbine to drive a compressor for a the refrigeration loop;
(c) gasifying a portion of refrigerant from the refrigeration system; and (d) reducing the temperature of inlet air entering the gas turbines by exchanging heat with the gasified portion of refrigerant either directly or indirectly.
9. The integrated method of claims 1 or 8, wherein the refrigeration is for LNG
production, air separation, food storage, or ice-making.
10. The integrated method of claims 1 or 8, comprising a single stage, two stage, or three stage refrigeration loop.
11. The integrated method of claims 1 or 8, wherein the refrigerant comprises methane, ethane, propane, ammonia, a hydrofluorocarbon, a chlorofluorocarbon, a hydrochlorofluorocarbon, a bromofluorocarbon, a bromochlorofluorocarbon, or any combination thereof.
12. The integrated method of claims 1 or 8, wherein a gain in energy efficiency by reducing the temperature of the inlet air entering the gas turbine compensates for an amount of energy required for chilling and consuming the portion of refrigerant in step (c).
13. The integrated method of claim 8, wherein the temperature of inlet air is reduced by exchanging heat indirectly with the regasified portion of refrigerant using an intermediate heat transfer fluid.
14. The integrated method of claims 1 or 8, wherein the heat transfer fluid comprises methanol, ethanol, a glycol and water mixture, or any combination thereof.
15. The integrated method of claims 1 or 8, wherein the temperature of the inlet air entering the gas turbine is reduced by 10 to 40 °F from ambient temperature.
16. The integrated method of claims 1 or 8, wherein the temperature of the inlet air entering the gas turbine is reduced from an ambient temperature in a range from about 60 to about 120 °F to a temperature in a range from about 45 to about 55 is increased by at least 3 % by reducing the temperature of the inlet air from 90 to 50 °F.
18. The integrated method of claim 8, further comprising recycling at least a portion of the consumed refrigerant to the refrigeration loop.
19. The method of claim 8, further comprising a step of collecting water condensed from reducing the temperature of the inlet air.
20. An integrated method for operating a liquefied natural gas (LNG) plant, the method comprising:
(i) cooling and condensing a natural gas stream in a refrigeration system to produce liquefied natural gas (LNG);
(ii) operating a gas turbine to drive a compressor for the refrigeration system;
(iii) regasifying a portion of the LNG;
(iv) consuming a portion of the refrigerant from the refrigeration system; and (iv) reducing the temperature of inlet air entering the gas turbine by exchanging heat with the regasified portion of the LNG and with the consumed portion of the refrigerant directly or indirectly.
21. The integrated method of claim 20 further comprising supplying at least a portion of the regasified portion of the LNG to an outlet pipeline.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US12/982,187 US20120167618A1 (en) | 2010-12-30 | 2010-12-30 | Use of refrigeration loops to chill inlet air to gas turbine |
| US12/982,187 | 2010-12-30 | ||
| PCT/US2011/065067 WO2012091933A1 (en) | 2010-12-30 | 2011-12-15 | Use of refrigeration loops to chill inlet air to gas turbine |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA2812605A1 true CA2812605A1 (en) | 2012-07-05 |
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ID=46379528
Family Applications (1)
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|---|---|---|---|
| CA2812605A Abandoned CA2812605A1 (en) | 2010-12-30 | 2011-12-15 | Use of refrigeration loops to chill inlet air to gas turbine |
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| US (1) | US20120167618A1 (en) |
| AU (1) | AU2011352950B2 (en) |
| CA (1) | CA2812605A1 (en) |
| GB (1) | GB2505539A (en) |
| WO (1) | WO2012091933A1 (en) |
| ZA (1) | ZA201301676B (en) |
Cited By (1)
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| CN105222446A (en) * | 2015-10-10 | 2016-01-06 | 华电电力科学研究院 | The LNG cold energy that utilizes of two-stage heat exchange is adopted to prepare the apparatus and method of common ice and Ozone Ice |
Families Citing this family (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB2494400B (en) * | 2011-09-06 | 2017-11-22 | Highview Entpr Ltd | Method and apparatus for power storage |
| ITCO20110073A1 (en) * | 2011-12-23 | 2013-06-24 | Nuovo Pignone Spa | SYSTEM INCLUDING A CONDENSED WATER RECOVERY DEVICE |
| CN103557675B (en) * | 2013-10-30 | 2015-05-27 | 河南开元空分集团有限公司 | Cryogenic distillation liquidation system and method for synthesis ammonia chemical tail gas |
| CA3032641C (en) * | 2016-08-16 | 2021-02-02 | Exxonmobil Upstream Research Company | System and method for liquefying natural gas with turbine inlet cooling |
| CN114876641A (en) * | 2022-06-14 | 2022-08-09 | 西安热工研究院有限公司 | Gas turbine inlet air cooling system utilizing LNG gasification cold energy and working method thereof |
Family Cites Families (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4951460A (en) * | 1989-01-11 | 1990-08-28 | Stewart & Stevenson Services, Inc. | Apparatus and method for optimizing the air inlet temperature of gas turbines |
| JP2688267B2 (en) * | 1990-02-13 | 1997-12-08 | 大阪瓦斯株式会社 | Method and device for liquefying and storing natural gas and supplying it after revaporization |
| TW421704B (en) * | 1998-11-18 | 2001-02-11 | Shell Internattonale Res Mij B | Plant for liquefying natural gas |
| US6324867B1 (en) * | 1999-06-15 | 2001-12-04 | Exxonmobil Oil Corporation | Process and system for liquefying natural gas |
| WO2002097252A1 (en) * | 2001-05-30 | 2002-12-05 | Conoco Inc. | Lng regasification process and system |
| JP4162989B2 (en) * | 2002-12-27 | 2008-10-08 | 株式会社前川製作所 | Cold heat utilization method and apparatus using LNG |
-
2010
- 2010-12-30 US US12/982,187 patent/US20120167618A1/en not_active Abandoned
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2011
- 2011-12-15 WO PCT/US2011/065067 patent/WO2012091933A1/en active Application Filing
- 2011-12-15 AU AU2011352950A patent/AU2011352950B2/en not_active Ceased
- 2011-12-15 GB GB1303959.9A patent/GB2505539A/en not_active Withdrawn
- 2011-12-15 CA CA2812605A patent/CA2812605A1/en not_active Abandoned
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2013
- 2013-03-05 ZA ZA2013/01676A patent/ZA201301676B/en unknown
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105222446A (en) * | 2015-10-10 | 2016-01-06 | 华电电力科学研究院 | The LNG cold energy that utilizes of two-stage heat exchange is adopted to prepare the apparatus and method of common ice and Ozone Ice |
Also Published As
| Publication number | Publication date |
|---|---|
| GB201303959D0 (en) | 2013-04-17 |
| GB2505539A (en) | 2014-03-05 |
| AU2011352950A1 (en) | 2013-03-21 |
| US20120167618A1 (en) | 2012-07-05 |
| AU2011352950B2 (en) | 2015-04-09 |
| WO2012091933A1 (en) | 2012-07-05 |
| ZA201301676B (en) | 2014-07-30 |
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