|Publication number||US3195316 A|
|Publication date||Jul 20, 1965|
|Filing date||Aug 2, 1963|
|Priority date||Aug 2, 1963|
|Publication number||US 3195316 A, US 3195316A, US-A-3195316, US3195316 A, US3195316A|
|Inventors||James B Maher, Mair James|
|Original Assignee||Chicago & Bridge & Iron Compan|
|Export Citation||BiBTeX, EndNote, RefMan|
|Patent Citations (5), Referenced by (24), Classifications (32)|
|External Links: USPTO, USPTO Assignment, Espacenet|
July 90, 1965 2,195,316
J. B. MAHER ETAL .METHANE LIQUEFACTION' SYSTEM Filed Aug. 2., 1963 PROPA NE CYCLE.
I000 ps'lcl IOO F ETHYLENE CYC LE MAIN VAPOPIZING STATION l5 psfa INVENTORS James 8. Maker arm James Jim? 7? I ATTORNEYS United States Patent 3,195,316 METHANE LIQUEFACTIGN SYTEM James B. Maher and James Mair, Chicago, 11., assignors to Chicago Bridge 8: Iron Company, Chicago, Ill., a corporation of Illinois Filed Aug. 2, 1963, Ser. No. 299,506 3 Claims. (Cl. 62'-52) This invention relates to apparatus and methods for storing materials which are normally gases at ambient tempertaures and pressures in the form of liquids. More particularly, this invention is concerned with novel processes and apparatus for liquefying methane, such as in the form of natural gas, and subsequently storing the gas in liquefied form.
Large amounts of methane, usually in the form of natural gas, are used in heating residences, apartments, ofiices and public buildings as well as in cooking. In addition, industry employs large amounts of the gas in processing operations of a wide variety.
The demand for gas varies seasonally as well as daily. Larger amounts of gas are needed during the winter season in the northern parts of the United States than during the warmer periods of the year. The same is true of the southern parts of the country but to a lesser extent. In addition, the demand for gas varies during the day, with lesser amounts being required during evening hours than during the daylight period. This is because industry employs larger amounts, generally, during the daylight hours and because home consumption is generally greater due to cooking during the daylight and early evening hours than in the nighttime.
Natural gas in distributed by means of pipelines which are usually unable to provide suflicient gas to supply the demand at peak periods.
In many areas of the country, it is necessary to store large quantities of natural gas for the purpose of peak shaving to provide the large supply of gas needed during intervals of high demand. It has become a commos practice, since the volume of vapor to be stored would be impracticable, to liquefy the gas near the ultimate area of consumption and subsequently to vaporize and distribute it through the local gas distribution system for ultimate consumption.
The liquefied gas is generally stored in large doublewalled insulated tanks at a low temperature which gives a vapor pressure only slightly above atmospheric pres- :sure. An internal vapor pressure of 15 p.s.i.a. with the storage temperature of the liquefied gas being about 25'8 F. is quite common and representative of the storage conditions.
The natural gas is normally liquified by a cascade refrigeration system followed by isenthalpec expansion, or flashing, into the storage tank. A disadvantage of this system is that large volumes of vapor must be handled by expensive equipment using considerable horsepower.
In the filling of a storage tank, the gas in the pipeline may be about 315 p.s.i.a. and in the consumer distribution header at about 90 p.s.i.a. During normal filling of the storage'tank the ratio of gas being stored to gas being distributed as vapor from the tank is about 1 to 1. However, the calorific value of the vapor or distributed gas must be maintained above a specified minimum to meet standards required for the gas.
Maintaining the calorific value of the gas involved in the liquefied vapor flashed to storage temperature is a serious problem since contaminating gases such as nitrogen and carbon dioxide are present in the natural gas in volumes determined by equilibrium conditions. For example, a flow-of natural gas carrying 2% nitrogen when compressed to 1000 p.s.i.a., cooled to 206 F., liquefied and flashed to a storage temperature of 258 F., would "ice release vapor carrying about 30% nitrogen. If the resulting vapor is then sent into a distribution system, the calorific value of the distributed gas would be lower, unless suitable steps are taken to correct the calorific content, than the gas fed directly from the pipeline to the distribution system.
Because of the heat-leak problem involved in storage of liquefied gases at low temperatures in insulated storage tanks, it is necessary in controlling the pressure to remove the vapor from the tank and either distribute it into the consumer distribution system or to liquefy it and feed it back into the storage tank. Such storage tanks are buiit and designed to withstand pressures only slightly above atmospheric pressure and therefore, it is necessary carefully to control the pressure in the tank. It would be prohibitively expensive to erect a large size storage tank which can withstand pressure significantly higher than atmospheric pressure and for this reason the liquefied gas is stored at just slightly above atmospheric pressure but at very low temperatures.
There are provided according to the subject invention, novel processes and apparatus which employ the liquefied product for controlling the vapor pressure in the storage tank as well as processes and apparatus which use the liquified product as a means for lowering the temperature of gas to be stored as a liquid in the tank.
More particularly, there is provided by this invention a mehtod of controlling the pressure in an insulated storage tank holding liquefied methane, such as in the form of natural gas, at close to but slightly above atmospheric pressure, which comprises withdrawing vapor from the tank, increasing the pressure of the withdrawn vapor, feeding the vapor at increased pressure into the tube side of a vessel cooled on the shell side by liquefied methane withdrawn from the tank, liquefying the vapor in the tube side of the vessel, feeding said liquefied methane into the tank and feeding the methane from the shell side of the vessel to a transfer pipe either for use in refrigerating additional supplies of gas to be stored or for distribution to the consumer system.
In another aspect of the subject invention the liquefied natural gas in the storage tank is used for further cooling methane, or natural gas, already brought to a liquid condition but which has a temperature which exerts a pressure substantially above atmospheric pressure, to a. temperature considerably lower so that upon flashing into the storage tank, a substantial portionof the gas will be cooled to storage temperature at approximately atmospheric pressure. In this method, incoming natural gas is subjected to the refrigerating action of a cascade system to convert it into a liquid at a temperature which exerts a pressure substantially above atmospheric pressure, after which the so liquefied gas is further cooled by passing it through the tube side of a vessel which is cooled on the shell side by liquefied natural gas withdrawn from the storage tank holding the same at close to, but slightly above, atmospheric pressure, removing the liquefied gas from the tube side of the vessel at a much lower temperature than at which it entered and then flashing the so cooled liquefied gas into the storage tank to further cool it to storage temperature. By storage temperature is meant that temperature which gives a vapor pressure close to but slightly above atmospheric pressure.
The invention will now be described in conjunction with the attached drawing inwhich:
The figure is. a fiow sheet showing schematically a system of receiving natural gas from a pipeline, its liquefaction and storage in a main storage tank, vaporization of the liquefied gas and distribution to a consumer header.
Natural gas is received from a pipeline at apressure of about 315 p.s.i.a. and is sent through line 10'to compressor 11 where it is raised toabout 1000 p.s.i.a. and
through heat exchanger 13where it is cooled, such as to about 22 F. The cooling in heat exchanger 13 is effected-by the natural gas removed from the main storage tankand used in the liquefaction process as will be more fully described subsequently. The eooled'natural gas from heat exchanger 13 is conveyed by pipe 9 into the tube side of the evaporator-condenser 14. A closedloop propane refrigerating cycle is used to cool the natural gas on the tube side of the evaporator 14 to a temperature of about 35 F. In tne propane cycle, propane vapor from vessel 14 is compressed by compressor 70, condensed by cooling water, the condensate collected in receiver 15 and returned to vessel 14 after passing through the heat exchanger 16.
After the natural gas has been cooled such as to about 35 F. in vessel 14, it is conveyed by pipe 17 through heat exchanger 65 which is cooled by natural gas removed from the main storage tank. After leaving the heat exchanger 65, the natural gas is lowered to a temperature of about 48 F.- The natural gas is then cooled further by conveying it by pipe 18 through the tube side of evaporator-condenser 1? which is cooled on the shell side by means of ethylene.
In the ethylene cycle, ethylene vapor from vessel 1% is compressed by compressor 72, condensed by propane in vessel 14, the ethylene condensate collected in receiver 20. and returned through heat exchanger 21 to vessel 19.
The natural gas as it leaves vessel 19 has been cooled such as down to about 130 F. It is then conveyed by pipe 22 through heat exchanger 23 where itis further cooled by'natural gas removed from the main storage tank. After leaving the heat exchanger 23, the gas is conveyed by pipe 24 through the tube side of .the,
evaporatoncondenser vessel 25 from which it is conducted by pipe 26 into receiver 27.
Vapors are removed from receiver 27 by pipe 28 and fed to the engines (not shown) used in the system. The vapors removed are somewhat enriched in nitrogen but this is no problem since the engines can readily handle gas containing an appreciable increase in nitrogen. Removal of some of the nitrogen in this way serves to raise the calorific content of the natural gas that is stored in liquefied condition, subsequently vaporized and then distributed.
Liquefied gas is sent from receiver 27 through pipe 29 into the bottom of the main storage tank 30. There it is fiashedtofurther cool it to a temperature of about -25 8 F. and a pressure of 15 p.s.i.a.
Vapors formed during the final flash, as Well as vapors formed due to heat-leak between the'storage tank and its surroundings, plus vapor displaced by the fill, are removed by line 31 and by means of compressor 32'are increaesd to a pressure of about 25 p.s.i.a. The vapors are then conducted by pipe 33 through the tube side of evaporator-condenser vessel 34 where they are liquefied and then conveyed by pipe 35 into receiver 36. Pump 37 then conveys the liquefied gas from receiver 36 by pipe 38 into the bottom of the main storage tank 30.
Vessel 34 is cooled by withdrawing liquefied natural gas from the main storage tank 36 by means of pipe d and then sending it through pipe 51 to pump 52 where the leaves by pipe 55 which feeds to blower 56. Blower 56 sends the gas through heat exchanger and by means of pipe 57 it is conveyed through heat exchanger 13 and then by pipe 3% into the line 46) for distribution to a consumer header at a pressure of about 90 p.s.i.a.
Liquid natural gas is also removed from the main storage tank 30 and is conveyed by pipe 50 to pump 41 from Y throughheat exchanger 23' and exits from it at a temperature of about l40 F. through line 45. Line 45 conveys the still cool natural gas through heat exchanger 65 from which it is conveyed by pipe 46 through heat exchanger 13 from which it leaves by pipe 47 and is then conveyed to pipe 4%) for distribution.
When it is necessary to supply increased amounts of natural gas, the liquid product in the main storage tank 36 can be removed by pipe 50, conveyed to pump 48 and then to line 49 which feeds itto a main vaporizer station 60 which in turn sends it throughpipe 61 into pipe 40 .for distribution.
The concentration of nitrogen in the vapor space of storage tank 30 is considerably higher than in the natural gas received fromthe pipeline so the vapor mixture has a lower calorific content. If vapor was removed from the storage tank and either fed directly into the distribution line 40, or first used to cool natural gas being liquefied bypassing it through vessel 43 and/ or heat exchangers 23, 65 and '13 before feeding it to line 40, the calorific content would be lower than that of the gas received in the pipeline. This is because the partial pressure of nitrogen at the'storage conditions is much higher than the partial pressure of liquefied natural gas.
By withdrawing liquefied natural gas fromthe main storage tank and using it to cool the product being liquefied, as well as to liquefy vapor withdrawn from the tank to control the pressure therein, thescalorific content of the gas after vaporizing isnot less, and usually is more, than that ofthe natural gas originally'received from the pipeline.
Although vessels 34 and 43 showvaporization of the liquified gas therein, adequate cooling can alternatively be obtained by passing the gas through the shell side in liquid form. However, this would require a greater flow or" gas through the shell side andperhaps increased pressures on the tube sides of these vessels.
Among other advantages of the described process is the use of small liquid pumps for propelling the liquid natural gas. N'o low temperature expensive compressors are required to convey the gas to the distribution header. The invention thus permits delivering methane vapor at a high temperature by pumping liquefied methane from a storage tank at close to atmospheric pressure, passing the so withdrawn gas through heat'exchangers and Vaporizers which vaporize the outgoing gas while cooling a stream of methane incoming to the tank, while generating all of said high pressure by the'liquid pump, i.e., without the need of a high. pressure, low temperature operating blower.
The described process also uses less horsepower than the classical cascade system for liquifying natural gas. The process of this invention uses about 580 horsepower, while the classical cascade system would use about 825 horsepower, per one million standard cubic feetper day.
Various changes and modifications of the invention can be made and, to the extent that'such variations incorporate the spirit of this invention, they are intended to be included within the scope of the appended'claims;
What is claimed is: V i i 1. A method of liquefying natural gas and storing the same in an insulated storage tank 'at'close to-but slightly above atmospheric pressure, which comprises subjecting incoming natural gasto the refrigerating action of a cascade system to convert it into a liquid at a temperature which exertsa pressure substantially-above atmospheric pressure,- further cooling the liquefied gas bypassing it through the tube side of a first vessel cooled on theshell side of liquefied natural gas withdrawn from a storage tank holding the same at close to but slightly above atmospheric pressure, removing the liquefied gas from the tube side of the first vessel at a much lower temperature than at which it entered and flashing it into said storage tank for storage at a temperature at, which'the gas gives a vapor pressure close to but slightly above atmospheric pressure, withdrawing vapor from the tank when it reaches'a nominal level, increasing the pressure of the withdrawn vapor, feeding the vapor at increased pressure into the tube side of a second vessel cooled on the shell side by liquefied gas withdrawn from the tank, liquefying the vapor in the tube side of the second vessel, feeding said liquefied gas into the tank, and feeding the gas from the shell side of the second vessel to a transfer pipe.
2. The method of claim 1 in which the gas from the shell side of the first and second vessel is used to cool the gas being liquefied for storage in the tank during cooling by the cascade system to enhance its efficiency.
3. Apparatus for liquefying methane and storing the same for subsequent distribution as a vapor which comprises in combination a cascade means for receiving methane from a pipeline and cooling the same until liquefied with a pressure substantially above atmospheric pressure, a first vessel for receiving the said liquefied methane on the tube side for further cooling it, said first vessel being adapted to be cooled by liquefied methane removed by pipe means communicating with an insulated main storage tank and the steel side of the first vessel, pipe means communicating with the shell side of the first vessel for conveying methane therefrom to means for cooling methane liquefied by the cascade means and then to a vapor distribution line, pipe means for removing liquefied methane from the tube 'side of said first vessel and conveying it to the main storage tank for flash cooling therein, pipe means communicating with the main storage tank and with means for vaporizing liquefied gas withdrawn from the tank and distributing the vapor to distribution means, pipe means communicating with the vapor space in the tank and with pressure means for removing vapor from the tank and increasing the pressure thereof, pipe means communicating with the pressure means for conveying the vapor into the tube side of a second vessel for liquefaction therein, means for receiving, pumping and conveying liquefied methane from the tube side of the second vessel to the tank, pipe means communicating with the main storage tank and the shell side of the second vessel for withdrawing liquefied gas from the tank and conveying it into the shell side of the second vessel to cool the same, and pipe means communicating with the shell side of the second vessel for removing methane therefrom and conveying it to said distribution means.
References Cited by the Examiner UNITED STATES PATENTS 2,082,189 6/ 37 Twomey 62-54 2,582,148 1/52 Nelly 62-23 2,682,154 6/54 Wilkinson 6254 2,884,763 5/59 Faulk 6254 2,960,837 11/60 Swenson et a1 62-9 ROBERT A. OLEARY, Primary Examiner.
|Cited Patent||Filing date||Publication date||Applicant||Title|
|US2082189 *||May 9, 1934||Jun 1, 1937||Lee S Twomey||Method of liquefying and storing fuel gases|
|US2582148 *||May 15, 1947||Jan 8, 1952||Pritchard & Co J F||Method of recovering desirable liquefiable hydrocarbons|
|US2682154 *||Jun 21, 1949||Jun 29, 1954||Air Reduction||Storage of liquefied gases|
|US2884763 *||Nov 20, 1956||May 5, 1959||Cities Service Refining Corp||Storage of liquified gases|
|US2960837 *||Jul 16, 1958||Nov 22, 1960||Conch Int Methane Ltd||Liquefying natural gas with low pressure refrigerants|
|Citing Patent||Filing date||Publication date||Applicant||Title|
|US3271967 *||Feb 19, 1965||Sep 13, 1966||Phillips Petroleum Co||Fluid handling|
|US3273349 *||Feb 15, 1965||Sep 20, 1966||Air Reduction||Variable demand air rectification plant with recycle|
|US3303660 *||Sep 27, 1965||Feb 14, 1967||Berg Clyde H O||Process and apparatus for cryogenic storage|
|US3318104 *||Dec 13, 1965||May 9, 1967||Roszkowski Theodore R||Method and apparatus for storing low-boiling liquids|
|US3319434 *||Mar 14, 1966||May 16, 1967||Air Reduction||Low temperature refrigeration and gas storage|
|US3324670 *||Nov 3, 1965||Jun 13, 1967||Shell Oil Co||Method of transporting methane or natural gas|
|US3331214 *||Mar 22, 1965||Jul 18, 1967||Conch Int Methane Ltd||Method for liquefying and storing natural gas and controlling the b.t.u. content|
|US3440828 *||Feb 11, 1966||Apr 29, 1969||Air Prod & Chem||Liquefaction of natural gas employing cascade refrigeration|
|US3453836 *||Jul 24, 1967||Jul 8, 1969||Mcmullen John J||Liquefied petroleum gas tanker|
|US4249387 *||Jun 27, 1979||Feb 10, 1981||Phillips Petroleum Company||Refrigeration of liquefied petroleum gas storage with retention of light ends|
|US4675037 *||Feb 18, 1986||Jun 23, 1987||Air Products And Chemicals, Inc.||Apparatus and method for recovering liquefied natural gas vapor boiloff by reliquefying during startup or turndown|
|US4888955 *||Aug 23, 1988||Dec 26, 1989||Liquid Carbonic Corporation||Two phase CO2 storage tank|
|US5325894 *||Sep 7, 1993||Jul 5, 1994||Chicago Bridge & Iron Technical Services Company||Method and apparatus for fueling vehicles with liquefied natural gas|
|US5590535 *||Nov 13, 1995||Jan 7, 1997||Chicago Bridge & Iron Technical Services Company||Process and apparatus for conditioning cryogenic fuel to establish a selected equilibrium pressure|
|US5615561 *||Nov 8, 1994||Apr 1, 1997||Williams Field Services Company||LNG production in cryogenic natural gas processing plants|
|US5674053 *||Jun 17, 1996||Oct 7, 1997||Paul; Marius A.||High pressure compressor with controlled cooling during the compression phase|
|US5687776 *||Jul 1, 1994||Nov 18, 1997||Chicago Bridge & Iron Technical Services Company||Method and apparatus for fueling vehicles with liquefied cryogenic fuel|
|US5769610 *||Jan 27, 1995||Jun 23, 1998||Paul; Marius A.||High pressure compressor with internal, cooled compression|
|US5771946 *||Jun 17, 1996||Jun 30, 1998||Chicago Bridge & Iron Technical Services Company||Method and apparatus for fueling vehicles with liquefied cryogenic fuel|
|US7065974||Mar 31, 2004||Jun 27, 2006||Grenfell Conrad Q||Method and apparatus for pressurizing a gas|
|US8505312 *||Jun 17, 2004||Aug 13, 2013||Fluor Technologies Corporation||Liquid natural gas fractionation and regasification plant|
|US20040194499 *||Mar 31, 2004||Oct 7, 2004||Grenfell Conrad Q.||Method and apparatus for pressurizing a gas|
|US20060032239 *||Aug 12, 2004||Feb 16, 2006||Chicago Bridge & Iron Company||Boil-off gas removal system|
|WO2004088232A2 *||Apr 1, 2004||Oct 14, 2004||Conrad Q Grenfell||Method and apparatus for pressurizing a gas|
|U.S. Classification||62/48.2, 62/912, 62/50.2|
|International Classification||F25J3/06, F17C13/02, F25J1/00, F25J1/02|
|Cooperative Classification||F25J1/0085, F25J2235/60, F25J2205/02, F25J1/0045, F25J1/0025, F25J1/0087, F25J1/0221, F17C13/025, F25J2210/62, F25J2290/62, F25J1/0205, F25J2220/62, F25J1/0052, F25J1/0022, Y10S62/912|
|European Classification||F25J1/00C4V, F25J1/02F, F25J1/00A6B, F25J1/00A6, F25J1/00R6E, F25J1/00R6P, F25J1/00C2V, F25J1/02B4, F25J1/02, F17C13/02P|