WEATHER-VANING AIR-COOLED HEAT EXCHANGERS

Abstract

An air-cooler assembly comprising a plurality of air-coolers (1), wherein the air-coolers (1) are arranged on a duct (15), the duct having the shape of a straight prism having a polygonal cross section, and wherein the duct has one air inlet (14) for taking in cooling air to be distributed to all air-coolers (1), is described. A floater (10) for LNG production and a method for LNG production using the air-cooler assembly is also described.

Claims

1. An air-cooler assembly comprising: a plurality of air-coolers arranged on a duct; wherein the duct has the shape of a straight prism having a polygonal cross section and one air inlet, the air inlet being for taking in cooling air to be distributed to all of the plurality of air-coolers; and wherein the plurality of air coolers are arranged at the side walls of the air cooler duct so that air for cooling the plurality of air coolers is withdrawn from inside of the air cooler duct and released into the surroundings.

2. The air cooler assembly according to claim 1, wherein the length axis of the duct is substantially horizontally arranged.

3. The air cooler arrangement according to claim 1, wherein the air inlet is provided with at least one fan.

4. The air cooler assembly according to claim 1, wherein the air inlet is provided with separators for separating liquid and particles from the incoming air.

5. The air cooler assembly according to claim 1, wherein the air inlet is provided with at least one spray nozzle for humidifying and cooling the incoming air.

6. The air cooler assembly according to claim 5, wherein a filter for removal of water droplets is arranged downstream of the at least one spray nozzle.

7. A floater for LNG production, the floater comprising: a plurality of air-coolers for obtaining the cooling capacity needed; wherein the air-coolers are arranged on a duct having the shape of a straight prism of polygonal cross section; wherein the duct has one air inlet for taking in cooling air to be distributed to all of the plurality of air-coolers; and wherein the air coolers are arranged at the side walls of the air cooler duct so that air for cooling the plurality of air coolers is withdrawn from the inside of the air cooler duct and released into the surroundings.

8. The floater according to claim 7, wherein the floater is anchored via a turret and swivel and is allowed to weather-vane to keep the air inlet upwind.

9. The floater according to claim 7, wherein the floater is an elongated ship-shaped floater having a bow end and an aft end, wherein the turret and swivel are arranged at the bow end of the floater and wherein the duct is arranged substantially parallel with the length axis of the floater.

10. A method for producing LNG from natural gas onboard a floater, the method comprising the steps of: bringing pre-treated natural gas onboard a floater; cooling the natural gas to produce LNG by repeated cycles comprising compression, cooling and expansion of a refrigerant and heat exchange between the cold refrigerant and the natural gas to cool the natural gas; wherein the cooling of the refrigerant during the production of LNG is performed via an air cooler assembly as defined in claim 1 arranged on at least one duct arranged so that all of the plurality of air coolers are receiving air from the inside of said at least one duct, and wherein the air used in the plurality of air coolers is released to the surroundings through the plurality of air coolers.

11. The method of claim 10, wherein the at least one duct is oriented so that the air inlet thereof is upwind relative to the plurality of air coolers arranged on the duct.

Description

BRIEF DESCRIPTION OF DRAWINGS

[0046] FIG. 1 shows a traditional arrangement of an air cooler on a rack, and the air flow in and out of the air cooler;

[0047] FIG. 2 illustrates air coolers arranged at a horizontally arranged cantilever;

[0048] FIG. 3 illustrates air coolers arranged at a tilted cantilever;

[0049] FIG. 4 illustrates an alternative cantilever having both horizontal and tilted areas for arrangement of coolers;

[0050] FIG. 5 illustrates the movement of a turret anchored vessel or floater as response to wind;

[0051] FIG. 6 is a cross section through a cooler channel according to the present invention;

[0052] FIG. 7 is a cross section of an alternative cooler channel according to present invention;

[0053] FIG. 8 is a side view of cooler channel according to the present invention arranged on a floater; and

[0054] FIG. 9 is a bird's eye's view of the cooler and floater as shown in FIG. 8.

DETAILED DESCRIPTION OF THE INVENTION

[0055] LNG plants with associated power production will according to the present invention be located on offshore floaters 10 as illustrated in FIGS. 5, 8, 9. The floater is preferably ship-shaped, i.e. formed as an elongated floating hull, having a bow-shaped forward end and an aft end. The floater 10 is anchored with one or more anchors which are connected to the floater via a turret, anchored by anchor lines C, and associated bearing and swivel system 11 arranged at or close to the bow of the floater. The skilled person will understand that the term turret is used to encompass a turret anchoring and loading/unloading system as is widely used in offshore operations, and any other corresponding solutions that can be used for anchoring a vessel allowing the vessel to rotate with the wind and that comprises connections for piping.

[0056] Preferably, the natural gas to be cooled and liquefied is pre-treated by one or more of the following processes: [0057] gas sweetening, i.e. removal of unwanted acid gases from the natural gas, [0058] dehydration, i.e. removal of water that may otherwise cause formation of hydrates from the gas, [0059] Hg removal, [0060] full or partial NGL processing, i.e. separation of the NGL from the gas and/or receiving NGL separated from the gas on the floaters, and fractionation of the NGL into saleable products, typically ethane, propane, butane and a heavier C5+ fraction, and [0061] compression of the pre-processed natural gas.

[0062] The pre-treatment is performed to reduce the processing onboard the floater to liquefaction only, and to avoid separation of NGL that has to be treated separately.

[0063] The pre-treated natural gas to be liquefied is supplied via a gas pipe 9 (see FIG. 8) connected to the turret and swivel 11. The floater 10 is free to rotate by the power of the wind about the turret, so that the floater 10 will weathervane as indicated by arrows 12 by means of the action of the wind indicated by 13, to keep the bow substantially up against the wind. Not shown thrusters may be arranged at the floater to adjust the orientation of the floater in the case that the wind is too weak to turn the floater into the preferred orientation. The skilled person will also understand that it may be preferred to position the floater so that the bow is not pointing directly up against the wind, but deviates at an angle of e.g. 5 to 20 degrees from the upwind direction, to allow any gas leakages at the deck to blow out of the deck partly sideways.

[0064] The LNG liquefied onboard the floater may be stored in buffer tanks in the floater hull and loaded for export onto not illustrated LNG shuttle tankers made fast to the floater to load LNG, and thereafter transporting the LNG to its destination. Normally, such LNG shuttle tankers will make fast to one side of the floater.

[0065] Liquefaction will be accomplished using known technologies, either efficient base load liquefaction plants or simpler peak shaving liquefaction technologies. Liquefaction processes are powered by compressors with inter- and after-coolers, where compressors and coolers reduce the enthalpy of refrigerant(s).

[0066] The low-enthalpy refrigerant(s) is (are) introduced into LNG exchanger(s) where the pre-treated natural gas is pre-cooled, liquefied and sub-cooled. The resulting LNG is stable at atmospheric pressure and about 163 C. The refrigerant, having higher enthalpy when exiting the LNG exchanger(s), is returned to the compressor suction side.

[0067] The air coolers are according to the present invention arranged on one or more air cooler duct(s) 15 being arranged along one side of the floater. The air cooler duct 15 may have any convenient cross section. The air cooler duct 15 has preferably a straight polygonal prism shape, and has a substantially horizontal length axis. The illustrated embodiments of FIGS. 8 and 9, have rectangular or rhombic cross sections, but the skilled person will understand that different polygonal cross sections are applicable. The length of the air cooler duct may correspond to the total length of the floater, but may be somewhat shorter, such as 2 to 20% shorter than the floater. The air duct has an air intake opening 14 in the end thereof close to the front end, or bow, of the floater, and an air outlet 21 opening at the end closest to the aft of the floater 10.

[0068] Due to the weather-vaning of the floater, the air intake opening 14 will be upwind, and the air outlet is downwind, ascertaining that the air released from the air coolers is not returned into the air coolers. This optimizes the air cooling effect.

[0069] A weather hood 17 is preferably arranged in front of the air intake opening 14 to stop or substantially reduce ingress of seawater into the air duct 15. The skilled person will understand that the weather hood 17 conveniently comprises a metal grid or screen arranged so that air is allowed to flow through, but which stops a substantial part of water following the airflow. Downstream of the weather hood 17, separators 18 are arranged for stopping water solids, drops and droplets above a given size. Preferably, droplets and solids being larger 50 microns in diameter are stopped. More preferred solids and droplets having a size larger than 30, such as 20 microns, are stopped by the weather hood and separators. The separators 18 may be any kind of packing known by the skilled person to be applicable for said task.

[0070] Spray nozzles 19 for humidifying of the incoming air may be provided downstream of the separators 18. The water used for humidifying is fresh water or desalinated water to avoid salt depositions inside the duct 15. A filter 20 is preferably arranged downstream of the spray nozzles to remove excess droplets from the water spray. By spraying water into the airflow, the air may be cooled from dry bulb to wet bulb temperature, which may reduce the temperature by, for example, about 5 C. The water used for spraying should be distilled water, transported to the floater on a supply vessel.

[0071] One or more fan(s) 16 is (are) arranged in the air intake 14 for the duct 15 to ascertain sufficient airflow into the duct 15. The illustrated fan(s) 16 is (are) arranged downstream of the filter 20. The fan(s) 16 might alternatively be arranged between the separators 18 and the filter 20.

[0072] Air coolers 1 are arranged at the side walls of the air cooler duct 15 so that air for cooling of the coolers 1 is withdrawn from the inside of the air cooler duct 15, and released into the surroundings. This arrangement, together with the weather-vaning of the floater, ascertains that the hot air released from the air coolers is not recycled into the same or a neighbouring air cooler.

[0073] Louvers 21 are preferably arranged at the aft end of the duct 15, to ascertain a slight overpressure inside the duct compared to the surrounding pressure. By keeping an overpressure inside the duct of e.g. 0.002 bar, air ingress into the duct, other than from the air intake 14, may be avoided. The louvers 21, or any other convenient control means, may be adjusted to maintain such a slight overpressure.

[0074] In order to use air coolers at all, the liquefaction plants must be adapted such that refrigerants in the compressor inter- and after-cooler systems are warmer than normal and therefore able to transfer waste heat into hot ambient air. Persons skilled in the art know how to do this, but doing so will always increase the specific compressor duty and hence the cooling duty.

[0075] The increased compressor duty and the increased cooling duty carry very large cost in terms of reduced liquefaction capacity, in particular on a CLSO where the available power and space are limited. Compared to building a second floater, it would be much more cost efficient if the compressor duty could be reduced, even when air coolers are used, and increase the liquefaction capacity accordingly.

[0076] The compressor duty will be reduced if the air cooling capacity is increased by increasing the number of air coolers, if fouling of the air cooler heat transfer surfaces is reduced, and if hot air recirculation over the air coolers is minimized in all weather conditions. In addition, the air cooler capacity is increased if the air temperature is reduced, for example on hot days, by water spray, which reduces the temperature from the dry bulb temperature to the lower wet bulb temperature.

[0077] This cooler arrangement increases the space available for air coolers substantially, compared to the normal use where air is discharged in the upwards direction only. This cooler arrangement also ascertains that the hot air is not redirected into the air coolers, as the cooling air is introduced into the duct at the windward end. By directing the flow or released hot air upwards and downward, no transversally directed forces that my rotate the floater is created by the air coolers. The skilled person will understand that the duct 15 may be arranged outside of the deck of the floater as described, or may be arranged above the deck. Additionally, more than one duct may be arranged at one floater, such as two or more air ducts, according to the need thereof.

[0078] Dependent on the configuration of the duct 15, air coolers 1 may be arranged at two or more of the surfaces of the air duct 15. FIG. 7 illustrates an air duct having a rhombic cross section, and where lengths sections through the opposite corners of the cross section are vertical and horizontal, respectively. The air coolers 1 are arranged at all four side walls of the duct 15 as illustrated in FIG. 7, and the air coolers are symmetrically arranged about horizontal lengths section through the top and bottom corners of the duct, so that transversally directed forces resulting from the action of the fans in the air coolers, counteract each other, and resulting in no transversal forces on the floater.

[0079] The resulting prevailing wind direction relative to the floater ascertains that the hot air leaving the air coolers is blow away from the air intake of the duct 15. As mentioned above, the turret and swivel arrangement 11 on the floater 10 allows the floater to weathervane or turn such that the bow heads substantially into the wind, such as directly into the wind or deviating e.g. 2 to 20 degrees from heading direction into the wind. Preferably, the duct and air coolers are arranged at the leeward or downwind side of the floater if the floater has an orientation deviating from pointing directly into the wind. It may be preferred to arrange the turret or to construct the floater so that the floater does not weather vane with the bow directly into the wind. A prevailing incoming wind direction deviating e.g. from 5 to 15 degrees form heading directly into the wind, may be preferable to ascertain that any gas due to gas leaks on the floater is blown partly sideways and away from the air coolers, not onto the floater deck. An automatic orientation by weather-vaning deviating from direct headwind as described here may be obtained by arranging the turret to one side of the length axis of the floater, and/or by using the superstructure onboard the floater as a windsail turning the floater to one side.

[0080] The skilled person will understand the details and variations of the anchored turret, the bearing arrangement allowing the floater to weather-vane, and the swivel enabling gas transfer from the fixed pipeline direction into the variable floater direction, all of which is shown as item 11 in FIG. 5.

[0081] Air cooler duty may be described by the following equation:

Q=UA*LMTD

where

Q=Duty, W

[0082] UA=air cooler size, W/ C.
LMTD=logarithmic mean temperature difference (between air and process fluid in the air coolers)

[0083] As an example, air coolers with and UA of 1.4e+6 W/ C. would occupy a footprint area of 300 m.sup.2. If the LMTD is 30 C., the total cooling capacity would be 42 MW. If the LMTD for these coolers is reduced to 15 C., the duty or capacity to cool process fluids is reduced to 21 MW. However, in this case, the process fluid or refrigerant temperature would be much closer to the air temperature, i.e. colder. In most cases, this will improve the process efficiency significantly. The duty of the air coolers has been reduced by reducing the LMTD, but can be increased according to this invention by using the duct with free space both upwards and downwards, doubling the number of air coolers. Then, the duty is brought back up to 42 MW, while maintaining the LMTD of 15 C. and the correspondingly colder refrigerant temperatures.

[0084] A second example shows the operating conditions for the duct for a specific air cooling duty. Consider a floater 350 m long, with a 300 m rectangular duct 15 m wide and 12 m high. The total area for air coolers, assuming ample space for access and maintenance, is 3000 m.sup.2 for air coolers facing upwards, and the same for air coolers facing downwards. The total air cooler area is 6,000 m.sup.2. This gives a total UA of 1.4 e+6(6000/300) W/ C., or 28 MW/ C. Furthermore, the LMTD is 22 C., which gives a total cooling duty of 2822 MW or 616 MW.

[0085] For a base load liquefaction system with capacity 400 metric tons LNG per hour, the cooling duty is 236.9 MW according to Table 1. With a cooling capability of 616 MW, the production capacity is 400(616/236.9) metric tons per hour, or about 1040 metric tons LNG per hour.

[0086] Table 2 gives an overview of the duct and air cooler operating conditions for this example. The mass flow of air is 12,300 kg/s and the air velocity at the duct inlet is 57 m/s. This velocity is gradually reduced to near zero at the aft duct outlet because air is consumed by the air coolers. The total pressure drop in the duct inlet and the duct itself is about 0.006 bar. An 8.5 MW fan is required to overcome this pressure drop.

TABLE-US-00002 TABLE 2 Example of air duct and air cooler operating conditions Variable Unit Value Total cooling duty MW 616 Air heat capacity kJ/kg-K 1.0 Air temperature C. 20 Air temperature rise in air coolers C. 50 Air mass flow kg/s 12300 Air volume flow m3/s 10200 Air velocity in duct inlet m/s 57 Air velocity in duct outlet m/s ~0 Air duct inlet filter pressure drop bar 0.005 Air duct pressure drop bar 0.001 Total air duct pressure drop bar 0.006 Fan duty MW 8.5

[0087] A very effective air-duct inlet filter has been assumed, similar to filters used in gas turbines in coastal areas. A less efficient filter or an enlarged air intake will reduce the pressure drop and reduce the fan power requirement such as to 2 or 3 MW. The airflow is large, but can be reduced by increasing the air temperature rise in the air coolers. This will reduce the air velocity in the duct, and further reduce the fan duty.

[0088] A person skilled in the art will know that increasing the air temperature rise in the air coolers may be done by reducing the number of stages in a train of compressors and intercoolers in the cooling system, such as from three to two stages, while maintaining the total pressure increase. This will significantly increase the discharge temperature from the remaining compressor stage(s), feeding the air coolers with much warmer process fluid, which therefore can heat the air to a higher temperature. As an illustration, instead of heating the air from 20 to 80 C., it may be heated from 20 to 140 C., reducing the airflow by about 50%. Compressors which can work with fewer stages and higher pressure increase over each stage may for example employ supersonic shock wave technologies instead of conventional turbo-compressor technology

[0089] A third example shows how compressor duty is reduced when increased space for air cooling is available, such as in a duct where air from air coolers can be discharged vertically downwards in addition to vertically upwards. The compressor could be an integral part of a natural gas liquefaction process or some general gas compression process.

[0090] Consider a compressor system comprising a first stage compressor, an air-cooled intercooler, a second stage compressor and an air cooled after-cooler. Methane is compressed from 2 to 6 bara in the first stage, and from 6 to 11.5 bara in the second stage. The methane flow rate is 1.0 e+6 kg/h. Pressure drop in the air coolers is minimal and therefore ignored in this example.

[0091] Compressor stage 1 has a duty of 69.8 MW in all cases. Air cooler 1 has an UA of 1.4 e+6 W/ C. when the available footprint is 300 m2. When the footprint increases, the UA and air flow increase proportionally. The result of this is that the methane is cooled more, to a temperature that is closer to the inlet air temperature. In case 1, the methane temperature is 60 C. after the intercooler. In case 2, which has 50% more air cooling capacity, the methane temperature is 40 C. out of the intercooler. In case 3, with two times the cooling area available relative to case 1, the methane temperature has decreased to 29 C. downstream of the intercooler.

[0092] The colder methane, which flows to compressor stage 2, has a lower volume, and therefore the duty of compressor 2 decreases from 44.3 to 40.2 MW, or by about 10%, when the air cooler capacity is increased by a factor of two.

[0093] The compressor after-cooler capacity is also increased from case 1 to case 3. It gets a lower methane inlet temperature, 126.6 C. in case 1, 104.4 C. in case 2, and 92.0 C. in case 3 with the largest intercooler. The result of this, plus increased after-cooler capacity, is much reduced after-cooler outlet temperature, starting with 60.4 C. in case 1, 35.7 C. in case 2 and 25.9 C. in case 3. If the compressed and cooled methane is used in a refrigeration system, the colder gas from case 3 will be far more efficient.

TABLE-US-00003 TABLE 3 The second stage compressor duty is reduced in cases 2 and 3, relative to case 1. Case 1 Case 2 Case 3 Source of 1.0 * air cooler 1.5 * air cooler 2.0 * air Process data Variable Unit area area cooler area Compr 1 CH4 Flow kg/h 1.0e+6 1.0e+6 1.0e+6 P(in) bara 2.0 2.0 2.0 P(out) bara 6.0 6.0 6.0 T(in) C. 20.0 20.0 20.0 T(out) C. 126.7 126.7 126.7 Duty MW 69.8 69.8 69.8 Air cooler 1 CH4 Flow kg/h 1.0e+6 1.0e+6 1.0e+6 T(in) C. 126.7 126.7 126.7 T(out) C. 60.0 40.0 29.0 Air Flow kg/h 2.0e+6 3.0e+6 4.0e6 T(in) C. 20.0 20.0 20.0 T(out) C. 100.8 89.3 78.3 Air Q MW 45.4 58.4 65.4 cooler LMDT C. 32.5 27.8 23.4 UA W/ C. 1.40e+6 2.1e+6 2.8e+6 Footprint m2 300 450 600 Compr 2 CH4 Flow kg/h 1.0e+6 1.0e+6 1.0e+6 P(in) bara 6.0 6.0 6.0 P(out) bara 11.5 11.5 11.5 T(in) C. 60.0 40.0 29.0 T(out) C. 126.6 104.4 92.0 Duty MW 44.3 41.6 40.2 Air cooler 2 CH4 Flow kg/h 1.0e+6 1.0e+6 1.0e+6 T(in) C. 126.6 104.4 92.0 T(out) C. 60.4 35.7 25.9 Air Flow kg/h 2.0e+6 3.0e+6 4.0e6 T(in) C. 20. 20.0 20.0 T(out) C. 100.9 74.7 59.1 Air Q MW 45.5 46.0 43.8 cooler LMDT C. 32.5 21.9 15.6 UA W/ C. 1.40e+6 2.1e+6 2.8e+6 Footprint m2 300 450 600

[0094] A fourth example is a compressor after-cooler, cooled by water circulating between the after-cooler and air cooler. This indirect cooling of the compressed gas may simplify the system and improve its safety. This example shows that indirect cooling is more efficient, and the after-cooler becomes much smaller, when the air cooling capacity is increased according to this invention.

[0095] Consider a compressor, which compresses 1.0 e+6 kg/h methane from 2 to 6 bara. The after-cooler is a methane/water heat exchanger. Cold water flows into the after-cooler, where it is heated. The hot water is then pumped to an air cooler, which removes the same amount of energy as supplied in the methane/water after-cooler. Results are shown in Table 4.

TABLE-US-00004 TABLE 4 Effect of larger air cooler area on an indirect compressor cooling system Case 1 Case 2 Case 3 Source of 1.0 * air cooler 1.5 * air cooler 2.0 * air Process data Variable Unit area area cooler area Compr 1 CH4 Flow kg/h 1.0e+6 1.0e+6 1.0e+6 P(in) bara 2.0 2.0 2.0 P(out) bara 6.0 6.0 6.0 T(in) C. 20.0 20.0 20.0 T(out) C. 126.7 126.7 126.7 Duty MW 69.8 69.8 69.8 CH4/ CH4 Flow kg/h 1.0e+6 1.0e+6 1.0e+6 water T(in) C. 126.7 126.7 126.7 exchanger T(out) C. 65.0 65.0 65.0 Water Flow kg/h 5.0e+5 5.0e+5 5.0e+5 T(in) C. 53.0 31.8 24.3 T(out) C. 122.4 101.7 94.3 Exchanger Q MW 42.2 42.2 42.2 LMDT C. 7.5 28.9 36.4 UA W/ C. 5.60e+6 1.45e+6 1.15e+6 Air cooler Water Flow kg/h 5.0e+5 5.0e+5 5.0e+5 T(in) C. 122.4 101.7 94.3 T(out) C. 53.0 31.8 24.3 Air Flow kg/h 2.0e+6 3.0e+6 4.0e+6 T(in) C. 20.0 20.0 20.0 T(out) C. 95.0 70.1 57.7 Air Q MW 42.2 42.2 42.2 cooler LMDT C. 30.1 20.1 15.0 UA W/ C. 1.4e+6 2.1e+6 2.8e+6 Footprint m2 300 450 600

[0096] The compressor operation is the same for cases 1, 2 and 3. The cooling of the methane in the after-cooler is also the same, although the advantage with larger air cooler might have been used to cool the methane to a lower temperature.

[0097] The advantage with larger air coolers in this example is, as Table 4 shows, to provide colder cooling water to the methane/water heat exchanger. This means that, for the same duty, the LMDT of the water/methane heat exchanger is increased from 7.5 C. in case 1, to 28.9 C. in case 2 and further to 36.4 C. in case 3. The heat exchanger UA, or size, is reduced correspondingly. This saves space and cost in the compressor after-cooler exchanger. The air cooler footprint, made possible according to this invention, increases the airflow and air cooler UA proportionally from case 1 to cases 2 and 3. As a result, the size of process equipment, in this case the water/methane exchanger, is reduced, freeing up valuable space on the floater deck.

[0098] A fifth example is a steam cycle, which is used for power supply on many floaters. This example shows that the steam cycle becomes more efficient, and the power output increases, when the air cooling capacity is increased according to this invention. Low-pressure steam from a steam turbine flows to an air cooler where the steam is condensed. The condensate is pumped to a heat source, typically a boiler, where it is vaporized and super-heated. The high-pressure steam drives the steam turbine.

TABLE-US-00005 TABLE 5 Steam turbine system efficiency increases when more air coolers are employed Case 2 Case 3 Case 1 1.5 * air 2.0 * air Source of 1.0 * air cooler cooler cooler Process data Variable Unit area area area Heater H2O Flow kg/h 31960 31343 31056 (Evaporator, P(in) bara 25.0 25.0 25.0 super- P(out) bara 20.0 20.0 20.0 heater) T(in) C. 56.1 43.3 37.1 T(out) C. 300 300 300 Duty MW 25 25 25 Expander H2O Flow kg/h 31960 31343 31056 T(in) C. 300 300 300 T(out) C. 56.8 44.0 37.9 P(in) bara 20 20 20 P(out) bara 0.171 0.090 0.065 Power MW 6.18 6.64 6.86 Air cooled H2O Flow kg/h 31960 31343 31056 condenser T(in) C. 56.8 44.0 37.9 T(out) C. 55.8 43.0 36.9 Air Flow kg/h 2.0e+6 3.0e+6 4.0e+6 T(in) C. 20 20 20 T(out) C. 53.7 41.9 36.3 Condenser Duty MW 18.85 18.39 18.16 data LMDT C. 13.5 8.8 6.5 UA W/m2 1.4e+6 2.1e+6 2.8e+6 Footprint m2 300 450 600 Pump H2O Flow kg/h 31960 31343 31056 P(in) Bare 0.171 0.090 0.065 P(out) Bare 25 25 25 T(in) C. 55.8 43.0 36.9 T(out) C. 56.1 43.3 37.1 Duty MW 0.03 0.03 0.03

[0099] Results are shown in Table 5. Similar to examples three and four, air cooler footprint is increased from 300 m.sup.2 to 450 and 600 m.sup.2 for cases 1, 2 and 3, respectively.

[0100] The heater duty and the pressure and temperature from the boiler are the same in each case. The steam conditions will therefore not affect the system efficiency. For the expander or steam turbine, the outlet pressure decreases when the air cooling capacity is increased from case 1 to cases 2 and 3. As a result, the power output increases from 6.18 to 6.64 and 6.86 MW when the allowable air cooler footprint is increased by 50 and 100%, respectively. This is an 11% increase in the power output. There is no significant effect on the condensate pump, except a small decrease in condensate flow rate for cases 2 and 3.

[0101] For a person skilled in the art, and depending on permits and environmental conditions, it would be possible to optimize the system by partial use of sea water for cooling, for example using a submerged pipe in which hot water is introduced, flows and is cooled by conduction of heat to the surrounding sea water, exits and is returned to the process for re-use as coolant, by different distribution of NGL fractionation duties between the terminal and the CLSO, and by using alternative liquefaction processes such as N2 refrigerant for smaller systems. In addition, the floater turret and associated swivel may be located in the bow or on the forward deck; the available space in the cantilever and/or duct, freed up by mounting some air coolers for vertical downward discharge of air, may be used for other equipment; the duct may have rectangular, rhombic or other shape; the air cooling capacity may be extended by mounting some coolers elsewhere on the floater; a distance may be provided from the air duct to the first air coolers to further prevent air recirculation; and the sequence of apparatus in the duct inlet may be modified such as using chillers to cool the air instead of water spray.