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Publication numberUS2958205 A
Publication typeGrant
Publication dateNov 1, 1960
Filing dateOct 22, 1958
Priority dateOct 22, 1958
Publication numberUS 2958205 A, US 2958205A, US-A-2958205, US2958205 A, US2958205A
InventorsBoyd Mcconkey George
Original AssigneeSun Oil Co
Export CitationBiBTeX, EndNote, RefMan
External Links: USPTO, USPTO Assignment, Espacenet
Transportation of normally gaseous fluids in pipe line system
US 2958205 A
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Description  (OCR text may contain errors)

TRANSPORTATION OF NORMALLY GASEOUS FLUIDS 1N PIPE 'LINE SYSTEM George Boyd Mc'Conkey, Wallingford, Pa., assgnor to Sun Oil Company, Philadelphia, Pa., a corporation of New Jersey Filed Oct. 22, 1958, Ser. No. 769,008

3 Claims. (Cl. 62-54) This invention relates to method and means for the transportation of normally gaseous iluids over long disstances and more particularly concerns a pipe line system for transporting a normally gaseous iluid wherein the transporting is effected with the iluid in liquid phase during a major portion of its travel and in mixed phase during the remainder. The invention, for example, is applicable to the transportation of n-atural gas across country.

Conventional systems for transporting a low boiling, normally gaseous iluid over long distances operate with the fluid in gaseous phase. Por instance, pipe line systems for natural gas conventionally have spaced apart pumping stations which pump the material in gas form. The present invention is distinguished from commonly used transportation systems in that the normally gaseous fluid is transported mainly in liquid phase. However, the invention is practiced in such a manner that the uid is purposely transported over a minor part of its distance o-f travel in mixed vapor and liquid phases. This effects substantial economies as compared to transporting the iluid entirely in liquid phase, as hereinafter more fully explained.

According to the invention a pipe line system is provided with spaced apart pumping stations and with means adjacent each station for liquefying that portion of the uid which has vaporized before arriving at the station. The temperature and pressure of the Huid are regulated at the rst station -in the system such that the fluid will be entirely in liquid phase when it enters and will remain in liquid phase for a major part of the distance to the next pumping station. As the iluid flows toward the nex-t station, its temperature progressively rises due to heat transfer from the pipe and frictional effects and its pressure progressively `decreases due to pressure drop through the line. The regulated temperature and pressure conditions for the entering lluid are such Ithat, after it has travelled a major portion of the distance toward the next station but substantially before it has arrived there, it will begin to vaporize in the pipe line. This vaporization proceeds as the iluid mixture flows toward the next pumping station, thereby causing the temperature to progressively decrease. The distance between pumping stations is such that, as the fluid arrives at the next pumping station, its temperature has dropped to approximately the original regulated temperature. At this point the mixture is passed to a separator where the gas phase is separated from the liquid, the gas is condensed, the condensate is admixed with the liquid, Yand the mixture is then pumped at regulated pressure toward the next station. Again, the mixture ows a major part of the distance between stations in liquid Iform `and then begins vaporizing, which causes the temperature to drop to approximately the original temperature as the mixture arrives at the next station. The same procedure is then repeated between each adjacent pair of pump stations.

The invention is more specifically described with refited States Patent O ICC erence to the 4accompanying drawing which schematically illustrates a pipe line system laccording to the present invention and which also illustrates the fluid temperature variation that occurs -along the line. For purpose of discussion the system will be considered as one adapted for the transportation of natural gas over long distances.

Referring to the drawing, the portion enclosed by dotted line 10 represents the initial liquefaction plant and pumping station for the natural gas which enters in vapor form through line 11 from a gas supply source. Station 10 has a liquefaction section which is illustrated schematically by compressor 12, condenser 13 and liquid collecting tank 14 and -a pumping section represented by pump 15. The liquefaction section serves for liquefying the feed and reducing the temperature of the liquid to the `desired low value, and pump 15 supplies the cold liquid to pipe line section 16a under the necessary pressure as shown in the drawing. The liquefaction section is a simplication of the equipment that would actually be required for reaching the low temperature that would be used in practice. For example, a cascade refrigeration system generally would be employed wherein the natural gas would be condensed by indirect heat exchange with evaporating ethylene, the vaporized ethylene would be recondensed similarly by means of ammonia or propane, and the ammonia Ior propane would be recondensed by water cooling. However, `any suitable manner of cooling the natural gas to the desired low temperature can be employed, and hence a detailed description of the liquefaction and reliquefaction stations is not required for proper understanding of the invention.

Following the initial pumping station the system includes a plurality of additional stations, represented in the drawing by the portions enclosed by dotted lines 17a and 17b which are connected by pipe line section 16b. While only two such stations are shown in the drawing, it will be understood that the system will include any required number of stations for transporting the material across country the desired distance. The stations are `approximately equally spaced apart at a distance which will depend largely upon the rate of heat build-up in the flowing uid resulting from heat transfer through the pipe 16 and from frictional effects in the line. Pipe 16 should be carefully insulated, as by means of a jacketing outer pipe with insulation or a vacuum or both provided in the annulus. With eilicient insulating means provided, the distance between adjacent pumping stations typically may be of the order of miles for a system designed for transporting 3200 gals/min. of liqueiied natural gas.

At each pumping station 17, means are provided for separating the uid into vapor and liquid portions, condensing the vapo-r portion, admixing the condensate with the liquid portion and then pumping the mixture at regulated pressure into the next section of the pipe line. Thus, station 17a is provided with vapor-liquid separator 18a and reliquefaction means again illustrated schematically by compressor 19a, condenser 20a and pump 21a, while stati-on 17b correspondingly has separator 18b, compressor 19b, condenser 2Gb and pump 2lb. This arrangement allows the fluid to be fed as a liquid into -all sections of line 16 `following the pumping stations at about the same temperature and pressure conditions as originally employed at station 10. Hence, between each adjacent pair of pumping stations, the fluid will flow about the same distance before vaporization begins to occur.

The upper portion of the drawing illustrates the variations in iluid temperature that occur along the sections of line 16. For example, assume that at station 10 the temperature of the liquefied feed has been regulated to 205 F. and that pump 15 supplies the cold liquid to line section 16a at a pressure of about 1100 p.s.i.g. The temperature level at this stage is indicated by point A in the upper part of fthe drawing. As the liquid ows through section 16a, heat build-up will cause the temperature to rise as indicated by line AB. At the same time the liquid pressure along the line progressively decreases. At point B pressure and temperature conditions are reached at which the liquid begins to vaporize. For example, B may occur at a distance which is 90% of that between stations and 17a, and the temperature and pressure at this point typically may be 158 F. and 304 p.s.i.g., respectively. This vaporization continues to occur as the liquid flows toward station 17a, thus causing the temperature to progressively decrease as indicated by line BA. The point A indicates that the temperature has again reached approximately the low value of 205 F., the pressure at this point being about 100 p.s.i.g, The shaded area under line BA indicates the zone in which vaporization occurs; and under the conditions assumed herein about 22% of the fluid would vaporize during its travel through this zone.

Upon reaching station 17a, the mixture is passed into separator 18a and the 22% portion of vapor is removed through compressor 19a and liquefied by means of condenser 20a. The condensate returns to the separator via line 22a where it mixeswith the 78% liquid portion of the uid. The mixture, which has a temperature of about 205 F., is pumped via pump 21a into line section 16b which it enters at a pressure of about 1100 p.s.i.g. During its passage toward station 17b, its temperature increases as indicated by line AB', reaching a maximum of about 158 F. at point B which is about l0 miles from the next pumping station. Again the material proceeds to vaporize, causing the temperature to drop back to 205 F. by the time it reaches pumping station 17b. The vapor is again separated and condensed, and the material is pumped into the next line section at a ternperature of about 205 F. and a pressure of about 1100 p.s.1.g.

Operation between succeeding pumping stations proceeds in the same manner as above described until the transported iluid has reached its final destination.

From the foregoing description it can be seen that the transporting operation conducted in accordance with the present invention involves substantially identical flow stages between adjacent pumping stations. In each stage the fluid enters the pipe line at about the same predetermined temperature and pressure conditions, which conditions are adapted to maintain the fluid in liquid form throughout a major portion, preferably 65-95%, of its distance of travel and then to cause continuous partial vaporization throughout the remainder of the distance. The distance of travel until vaporization begins is selected so that the cooling eiect in the vaporization zone will bring the temperature of the vapor-liquid mixture approximately down to the initial low tempertaure as the material reaches the next pumping station.

By operating in the foregoing manner, substantial economies are effected as compared to maintaining liquid phase ow over the entire section between pumping stations. When natural gas is transported entirely in liquid phase with pumping stations spaced so that the liquid approaches but does not reach its bubble point, a considerably lower fluid temperature (eg. 50 F. lower) is required or else the distance between pumping stations must be substantially shorter as compared to operating in accordance with the present invention. When a lower temperature is used, the heat transfer rate through the pipe line to the flowing material is materially greater and recooling costs are correspondingly increased. Decreasing the distance between pumping stations necessitates having more of them for a given distance of transportation and likewise increases the costs.

While the foregoing description has been directed largely to the transportation of natural gas, it is to be understood that the principles of the invention also are applicable 'to the transportation of other normally gaseous materials. For example, the transportation of materials such as oxygen, nitrogen, ethylene and acetylene over long distances can advantageously be carried out by employing the present invention.

I claim:

1. Method of transporting a normally gaseous fluid over long distances in a pipe line system having spaced apart pumping stations which comprises regulating the temperature and pressure of the iiuid at the first station such that the fluid enters the pipe line in liquid form at a temperature substantially below that at which vaporization would occur; pumping the fluid alone toward the next pumping station, whereby the temperature of the fluid within the pipe line progressively increases and the pressure progressively decreases; permitting fluid to begin vaporizing within the line after the fluid has travelled a predetermined major portion in the range of -95% of the distance to the next pumping station, whereby vaporization causes the temperature of the fluid to progressively decrease; passing fluid, when its temperature has decreased due to vaporization to approximately the aforesaid regulated temperature, into a separating zone and therein separating vapor from liquid; condensing the vapor; mixing the condensate with the separated liquid; pumping the mixture alone at a temperature and pressure approximately the same as said regulated temperature and pressure toward the next pumping station; and repeating the specified operation between each adjacent pair of pumping stations.

2. Method according to claim 1 wherein the normally gaseous fluid is natural gas.

3. Method according to claim 2 wherein said temperature and pressure at each pumping station approximate 205 F. and 1100 p.s.i.g., respectively, and vaporization occurs when the fluid has travelled about of the distance between stations.

References Cited in the le of this patent UNITED STATES PATENTS 1,762,423 Scharpenberg June 10, 1930 1,956,009 Dieschur Apr. 24, 1934 2,021,394 Wade Nov. 19, 1935 2,392,783 Stevens Jan. 8, 1946

Patent Citations
Cited PatentFiling datePublication dateApplicantTitle
US1762423 *Jan 24, 1927Jun 10, 1930Scharpenberg Henry AMethod of transporting petroleum products
US1956009 *Feb 15, 1932Apr 24, 1934M L R DiescherPipe line system for the transportation of natural gas
US2021394 *Mar 11, 1935Nov 19, 1935Henry N WadeApparatus for dispensing highly volatile liquids
US2392783 *Jun 14, 1944Jan 8, 1946B F Sturtevant CoGas compressor station
Referenced by
Citing PatentFiling datePublication dateApplicantTitle
US3256705 *Dec 27, 1963Jun 21, 1966Moses DimentbergApparatus for and method of gas transportation
US3362177 *Jun 30, 1966Jan 9, 1968Phillips Petroleum CoVapor pressure control in liquefied gas dispensing
US3508415 *Apr 23, 1968Apr 28, 1970Eduardo Ospina RacinesNatural gas transmission power cycle
US3802213 *Oct 25, 1972Apr 9, 1974Osaka Gas Co LtdA gas transmission system suitable over wide demand variation
US3990256 *Feb 26, 1973Nov 9, 1976Exxon Research And Engineering CompanyMethod of transporting gas
US4015437 *May 13, 1975Apr 5, 1977Messer Griesheim GmbhProcess for cooling cryocables using a hydrogen slush
US4024720 *Apr 4, 1975May 24, 1977Dimentberg MosesTransportation of liquids
US4336689 *Jul 10, 1981Jun 29, 1982Union Carbide CorporationProcess for delivering liquid cryogen
US4420950 *Apr 1, 1982Dec 20, 1983Energiagazdalkodasi IntezetPlant for utilization of low-potential waste heat of a gas-pipeline compressor station
US4554791 *Dec 30, 1983Nov 26, 1985Danfoss A/SApparatus for conveying liquids
US4559786 *Feb 8, 1984Dec 24, 1985Air Products And Chemicals, Inc.High pressure helium pump for liquid or supercritical gas
US4958653 *Jan 29, 1990Sep 25, 1990Atlantic Richfield CompanyDrag reduction method for gas pipelines
US5020561 *Aug 13, 1990Jun 4, 1991Atlantic Richfield CompanyUsing fatty acid amine having amine polar group and hydrocarbon non-polar group
US5372010 *Jul 8, 1993Dec 13, 1994Mannesmann AktiengesellschaftMethod and arrangement for the compression of gas
US5778917 *Jun 19, 1997Jul 14, 1998Yukon Pacific CorporationNatural gas compression heating process
US6141973 *Sep 15, 1998Nov 7, 2000Yukon Pacific CorporationApparatus and process for cooling gas flow in a pressurized pipeline
US6201163Jul 16, 1997Mar 13, 2001Jl Energy Transportation Inc.Adding to natural gas sufficient ethane or propane to form a mixture wherein at the pressure and temperature to be used for transporting, the product of z factor and molecular weight of mixture is lower than z factor of untreated gas
US6209350Oct 21, 1999Apr 3, 2001Exxonmobil Upstream Research CompanyRefrigeration process for liquefaction of natural gas
US6217626Jul 16, 1997Apr 17, 2001Jl Energy Transportation Inc.High pressure storage and transport of natural gas containing added C2 or C3, or ammonia, hydrogen fluoride or carbon monoxide
WO2000025060A1 *Oct 22, 1999May 4, 2000Exxonmobil Upstream Res CoRefrigeration process for liquefaction of natural gas
WO2006046875A1Oct 25, 2005May 4, 2006Sargas AsMethod and plant for transport of rich gas
Classifications
U.S. Classification62/48.2, 62/50.1, 48/190, 137/13
International ClassificationF17D1/00
Cooperative ClassificationF17D1/005, F16L2101/40
European ClassificationF17D1/00B