Patent Publication Number: US-3874184-A

Title: Removing nitrogen from and subsequently liquefying natural gas stream

Description:
Harper et a1.  
 Apr. 1, 1975 1 REMOVING NITROGEN FROM AND SUBSEQUENTLY LIQUEFYING NATURAL GAS STREAM [75] Inventors: Ernest A. Harper; Martin R. Reber,  
  both of Bartlesville, Okla. [73] Assignee: Phillips Petroleum Company,  
 Bartlesville, Okla.  
 [22] Filed: May 24, 1973 [21] Appl. No.: 363,484  
 [52] US. Cl 62/28, 62/23, 62/9 [51] Int. Cl F25j 3/02 [58] Field of Search 62/23, 24, 27, 28, 29, 62/43, 40  
 [56] References Cited UNITED STATES PATENTS 2,557,171 6/1951 Bodle 62/23 2,677,945 5/1954 Miller 62/23 3,158,010 11/1964 Kuerston 62/29 3,160,489 12/1964 Brocoff 62/23 3,212,278 10/1965 Huddleston 62/23 3,274,787 9/1966 Grenier 62/23 3,323,316 6/1967 Harmens 62/28 3,407,614 10/1968 Poska 62/23 3,596,473 8/1971 Strcich et al 62/28 3,702,063 11/1972 Fizbach et a1. 62/23 3,763,658 10/1973 Gaumer ct a1. 62/40 Primary Examiner-A. Louis Monacell Assistant Examiner-Frank Se&#39;ver Attorney, Agent, or Firnz-Quigg &amp; Oberlin [57] ABSTRACT A natural gas containing substantial nitrogen is refrigerated to below minus 120F in usual propaneethylene refrigeration system using a cascade arrangement. Vapor and liquid thus obtained are separated and the liquid passed into the tubes of a refrigeration heat exchanger. The vapor and liquid, which has been further refrigerated, as a liquid, are recombined to ef-&#39; fect uniform distribution of the vapors into the further refrigerated liquid for a flow through the heat exchanger tubes. Thus, admixed liquid and vapor streams are further refrigerated by heat interchange with bottoms from a fractionation Zone into which the feed has been flashed, thus reboiling the fractionation zone bottoms. The nitrogen to be separated and some hydrocarbon, e.g., methane, are taken as overhead from the fractionation zone. Also, the overhead is used to refrigerate the liquid first obtained when refrigerating the feed after separation of vapors there from. Further, refrigeration of the recombined vapor and liquid is effected by flashing the natural gas containing fractionation zone bottoms in several stages, using liquid obtained upon a first flashing of said bottoms to refrigerate the recombined vapor and liquid streams described and using vapors from each flashing step practiced upon the fractionation zone bottoms to further refrigerate in order to the liquid first separated from the feed after separation of vapors therefrom and the incoming feed gas resulting in a fuel gas containing some nitrogen. The remainder of the several times flashed fractionation bottoms is now&#34;substantially at atmospheric pressure and constitutes liquefied natural gas substantially free from nitrogen which isthe product of the process. 1  
 A controls system designed to render the system essentially automatic and to keep it in balance operation is described.  
 4 Claims, 1 Drawing Figure SET J I V K1;- POINT FRC 36 I 2 1 I B-PRQPANE PRC l&#39;- A 1f 1 REFRIGERATION STAGES LIC J 2 N21 soMEcI-I 4 2s 2s 5 e FI AsHINc J 2 NE I I B 5/ t f 39 NI&#39;l&#39;ROGEN l I I l REMOVAL I I I &#39;2 2| I FRACT I I l l IONATOR 4 1 SEPARATOR l i FUEL GAS 1 l I 7 v 27 N2+CH4 Q I Ic I Ic y I 10 To&#39;B+I-I&#39; 5 33 H 23 T0&#39;B&#39;+&#39;H&#39; km 22 W l FLASHING LlC 5 ZONE TOPIPELINE i OROTHER I9 MEANS 20 REMOVING NITROGEN FROM AND SUBSEQUENTLY LIQUEFYING NATURAL GAS STREAM REMOVING NITROGEN FROM AND LIQUEFYING NATURAL GAS This invention relates to the production of liquefied natural gas substantially freed of nitrogen which is orginally contained. It also relates to a combination of steps wherewith to remove nitrogen from a natural gas containing same in substantial quantities.  
  In one of its concepts, the invention provides a process wherein a natural gas containing methane and nitrogen is fractionated in steps including refrigerating the natural gas to liquefy at least a substantial portion or all of the gas, separating the refrigerated gas into a liquid stream and a gas stream, refrigerating the separated liquid stream combining the refrigerated liquid stream and the separated gas stream, further refrigerating the combined streams, the natural gas being fed to the system at a suitable elevated pressure of the order of several hundred pounds per square inch, flashing the thus refrigerated stream into a fractionation zone, in said zone separating nitrogen as a vapor stream and a natural gas from which substantial nitrogen has been removed as a liquid stream and recovering from lastmentioned liquid stream a natural gas product substantially freed from nitrogen.  
  In a further, concept of the invention, it provides a process as described wherein the overhead from the fractionation zone is used to cool the first separated liquid stream.  
  In a further concept of the invention, there is provided a process as described wherein a portion of the liquid from the fractionation zone is heat interchanged with the feed to the fractionation zone before said feed is flashed thereinto and the thus warmed fractionation zone liquid returned to said fractionation zone to warm the bottom thereof.  
  In a still further concept of the invention, it provides steps in combination as described herein wherein bottoms from the fractionation zone are flashed to a lower pressure and separated into a vapor which can also be used to cool said first separated liquid and into a liquid which is used to refrigerate the combined liquid and vapor streams, the thus warmed and thus used liquid thereby being partially vaporized and passed as a cold vapor into heat interchange with said first obtained separated liquid stream.  
  In still another concept of the invention, the fractionation bottoms after flashing and separation into vapor and liquid which are used as described and some of which constitute a liquid still are now passed as said liquid through at least one pressure reduction step generating vapor and liquid at a reduced temperature which is useful as a refrigerant in the process and a remaining product which is liquefied natural gas substantially freed from nitrogen.  
  At a time of impending natural gas shortages some of which have been experienced already and which have resulted in layoffs and other undesirable situations, we have conceived a combination of steps as described herein which permit processing certain kinds of natural gases, particularly gases containing substantial quantities of nitrogen which must be removed from the said gases to accomplish anacceptable product.  
  It is an object of this invention to produce a purified liquefied natural gas. It is another object of this invention to provide a process with which to purify a natural gas. It is another object of the invention to provide a process for the removal of nitrogen from a natural gas containing the same in substantial quantity. It is a further object of the invention to remove nitrogen from a natural gas. It is a further object still to provide a combination of steps wherewith to process a natural gas to remove an undesired impurity therefrom in an economical and convenient manner.  
  Other aspects, concepts, objects and the several advantages of this invention are apparent from a study of this disclosure, the drawing and the appended claims.  
  According to the present invention, a combination of steps are provided for removing nitrogen from a natural gas containing the same wherein the natural gas is compressed to an elevated temperature of the order of several hundred pounds per square inch, is refrigerated, a vapor and a liquid stream are obtained following said refrigeration, a liquid stream is further refrigerated and then combined with the vapors for further refrigeration whereupon the thus refrigerated combined streams are flashed into a fractionation zone so operated as to obtain therefrom as overhead substantially all of the nitrogen and as bottoms therefrom a liquid stream substantially reduced in nitrogen which upon further flashing will yield a liquid residue which is a natural gas liquid substantially free from nitrogen and a fuel gas containing nitrogen and some methane.  
  Also according to the present invention, the liquid from the bottoms from the fractionation zone is heat interchanged with the feed coming into said fractionation zone and before it is flashed thereinto and thus to refrigerate the feed while warming a fractionation zone bottoms.liquid.  
  Also according to the invention, vapors obtained upon flashing the fractionation zone bottoms are used to refrigerate a first separated liquid-obtained upon refrigerating the incoming feed natural gas while liquid obtained upon flashing said fractionation zone bottoms is used to refrigerate the feed to the fractionation zone before it is flashed thereinto, yielding vapors which are also used to refrigerate said first separated liquid.  
  Other features and advantages of the combination of steps according to the invention are evident from the following description of the drawing which illustrates the now contemplated best mode for combining the steps of the invention and the operating conditions involved.  
  Referring now to the drawing, there is shown in diagrammatic form a flow plan according to the invention which provides the economy of equipment and operational costs which characterize the novel combination of steps or arrangement of the invention.  
  A nitrogen containing natural gas feed, as can be obtained in the gas fields in Algeria, enters by l at about 589 psia and atmospheric temperature and is cooled to about l27F at 547 psia passing through heat exchangers at 2 in which the entering fluid is heat exchanged with several stages of ethylene and propane refrigerants in the case of the design here described three of each in the order stated. Cascade arrangement,  
 .not shown, is employed. Such arrangements are well known and are omitted for sake of clarity of the drawing. The substantially condensed gas is passed by 3 into vapor separator A which is at about l27F and 547 psia. The overhead from A is largely nitrogen but does contain some hydrocarbon. A is maintained partly full of liquefied gas and on a level control 31 which is connected to operate valve 4 in pipe 5 which passes into and through heat exchanger zone B in which it is heat exchanged with streams later identified. According to the invention, a liquid from A is further cooled in B and then is combined with overhead stream 6 from A, the combined steams passing through 7 in heat exchanger zone G. The thus cooled vapors and liquid combined stream is passed by 8 through flash valve 9 into fractionator C from which overhead 25 is nitrogen and some methane at about l 73F. The bottoms from the fractionator at 355 psia are passed by 10 through flash zone 11 and to vapor separator D at about l 84F and at about 179 psia. Overhead from D is passed by 12 into B and therein is heat inter-changed with liquid feed passing through E in 5 and later with the feed stream in H.  
  Liquid in D is passed by 14 into heat interchange in G with the combined vapors and liquid from A in 7 and then back into the vapor space in D. D is maintained on the liquid level control 15 connected to liquid drawoff flash valve 16 in 17, the flashed liquid and vapors generated being passed to E. also a vapor-liquid separator at about 224F and at about 59 psia. The liquid from E which is maintained on liquid level control 18 is passed by 19 through release valve 20 into F from which the final liquefied natural gas product is passed at about atmospheric pressure to a pipeline or storage as desired by 21.  
  The vapors taken off from F at 22 and from E at 23 are heatinterchanged in B with the liquid in 5 and in H with the feed stream.  
  .The overhead 25 from fractionator C is passed through flow control valve 38 into B into heat interchange with the liquid portion of the feed in 5 and thence by 26 into heat interchange with the feed in H and is then taken from the system at 27 as fuel gas.  
  Residual gas flow from the top of separator A is controlled by valve 30 in pipe 6 also manipulated by level controller 31. In normal operation, valve 30 is wide open and valve 4 is opened and closed by controller 31 to maintain the liquid in tank A at a desired level. However, when valve 4 is wide open and the liquid level in tank A continues to rise, valve 30 is partially closed by controller 31 thereby increasing the pressure in tank A and forcing liquid out the bottom through pipe 5. Valve positions according to the output signal pressure from controller 31 are as follows:  
 Valve Position Controller Output Pressure, psig 4 3O 3 Closed Wide open +opening 9 Wide open Wide open 11 closing 15 Wide open Closed mixture among several passageways in a heat exchanger so as to insure equal amounts of liquid and vapor in each passageway are&#39;known.  
  The combination of such a&#39;system of control of vapor and liquid flows, according to the invention, permits an efficient utilization of the separated components of the stream in 3.  
  The natural gas in passageways 7 is additionally liquefied and subcooled in passing through exchanger G by indirect heat exchange with bottoms from fractionator C in two steps. In the first step cold bottoms from the fractionator are passed through exchanger G via pipe 33 countercurrently to the feedstream in passageways 7 thereby cooling said feedstream while warming and vaporizing part of the liquid in pipe 33. The now partially vaporized bottoms from fractionator C is returned to the fractionator via pipe 34. Thus fractionator G is reboiled by heat exchanging bottoms with feedstream in passageways 7.  
  Additional cooling of the stream in passageways 7 is obtained in a second step wherein bottoms from fractionator C are flashed by passage through valve 11 from 355 psia to 179 psia and l84F and then conducted via pipe 10 to flash drum D. Liquid circulates from drum D via pipe 14 through exchanger G by the the thermosiphon principle and flows back into drum D. The natural gas feedstream in passageways 7 is thereby cooled by countercurrent heat exchange with the cold liquid in pipe 14.  
  The cold feedstream exits exchanger G at 540 psia via pipe 8 and is flashed into the top of nitrogen removal fractionator C by passage through flash valve 9. By flashing from 540 psia to 355 psia, some of the liquid evaporates with a reduction in temperature to 1 73F in the top of fractionator C. Flash valve 9 is manipulated by pressure controller 35 in response to the pressure in pipe 8. The set point of controller 35 is manipulated by flow controller 36 in response to its primary set point and to a measurement of the rate of flow of gas entering the plant.  
  Fractionator C effects a separation between nitrogen and other low boiling impurities such as hydrogemhelium, etc. and methane and heavier hydrocarbons. The nitrogen product together with some methane exits the fractionator in the gaseous state at the top and passes via pipe 25 to exchanger B wherein it cools the feedstream in pipe 5. The nitrogen product then passes through exchanger I-l via pipe 26 wherein it cools a refrigerant stream and exits via pipe 27 as fuel gas. Flow rate of nitrogen product in pipe 25 is controlled by valve 38 which is manipulated by flow controller 39 in response to the measured flow in pipe 26. The set point of controller 39 is in turn manipulated by flow controller 36 in response to its applied set point and measurement of the flow rate of gas entering the plant.  
  Thus, according to the invention there has been provided a more efficient process for the liquefaction of natural gas, with an integrated&#39;nitrogen removal fractionator, wherein the natural gas is heat exchanged with the fractionator bottoms in two steps thereby reboiling the fractionator while cooling the natural gas feedstream. Refrigeration costs are substantially reduced as are equipment costs with our integrated liquefaction-nitrogen removal process. The following is an example given to illustrate the-invention. It is based partly on knowledge of the-art, including feed streams available and their-composition, engineering and related knowledge which have been incorporated together.  
 EXAMPLE Flow rate and composition of a typical nitrogencontaining natural gas entering the plant via pipe 1 is as follows:  
 Flow Rate Composition,  
 Component Mols/Day M01 /2 Helium 1742 0.2 Nitrogen 52951 6.3 Methane 745766 87.1 Ethane 46719 5.6 Propane 6214 0.7 lsobutane 462 0.05 n-Butane 429 0.04  
 Total 854384 100.00  
 Temp. 100 F.  
 Press. 589 psia Flow rate and composition of the gas as it exits exchanger 2 is, of course, the same as the feed gas to the plant but the gas has now been cooled to 127F at a pressure of 547 psia. The gas has now been partially liquefied and consists of 382,065 mols/day of vapor and 472,319 mols/day of liquid. This mixture of vapor and liquid is passed to phase separator A from which the vapor passes overhead via pipe 6 and the liquid passes from the bottom through pipe 5. The liquid is subcooled in exchanger B from l27F to about -l35F and it is then remixed with the gas in pipes 7 before passage of the mixture through exchanger G. The mixture still has the same composition and flow rate as in pipe I and now has a temperature of about 129F and a pressure of 544 psia. The gas-liquid mixture is equally distributed about among the several passageways in exchanger G using a device known in the art.  
  The gas-liquid mixture is completely liquefied in exchanger G and issues therefrom at a temperature of -176F and a pressure of 541 psia. This liquid is then passed via pipe 8 to nitrogen-removal fractionator C wherein a portion of the liquid feed flashes into vapor passing through valve 9 which reduces the pressure from 540 psia to 355 psia. Valve 9 is manipulated by PRC-35 in response to the pressure of the liquid passing to valve 9, i.e., the pressure in pipe 8. the set-point of PRC-35 is in turn manipulated by PRC-36 in response to the flow of feed gas entering the plant. The primary set point is applied to FRC-36. A flow rate of 855,000 moles per day, for example, is applied as set point to controller FRC-36. 1f the flow entering the plant as measured by flow element F-l decreases below 855,000 moles per day, PRC-36 manipulates the set point of PRC-35 in such a way that valve 9 must open, i.e., the set point of PRC-35 is decreased. PRC-35 thus opens valve 9 until the measured pressure in pipe 8 equals that applied as set point.  
  Fractionator C separates most of the nitrogen from the liquefied gas and rejects it as the overhead product. Compositions of overhead and bottoms are as follows:  
  Overhead, Bottoms. Component Mols/day Mols/day Helium 1.742 0 Nitrogen 52.831 Methane 91,325 654,441 Ethane 335 46,384 Propane 3 6,21 l lsobutane 0 462 n-Butanc 0 429 C 0 101 Temp.. F 173 l5l Press, psia 343 343 Bottoms product from the fractionator is passed via pipe 10 through pressure reduction valve 11 which reduces the pressure from about 360 psia to about 179 psia. This causes a portion of the liquid to flash and a reduction in temperature of from about 151F to about 1 85F. The resultant mixture of liquid and vapor is discharged into separator D from which vapor is discharged overhead. Liquid in separator D circulates by thermo-siphon action through pipe 14 and into exchanger G wherein it refrigerates the incoming feedstream. Stream 14 is thereby partially vaporized while stream 7 is totaly condensed and subcooled. Stream 14 amounts to 775,448 mols per day of liquid entering exchanger G and has the following composition:  
  Stream 14 is partially vaporized in passing through exchanger G and discharges back into tank D in the amount of 579,949 moles/day of liquid and 195,498 moles/day of vapor. Temperature is about l82.5F and pressure is about 179 psia.  
  Feedstream 7 was thus refrigerated by exchange with stream 14. Feedstream 7 is additionally cooled by heat exchange with recycle stream 33 taken from the bottom of fractionator C. The fractionator is reboiled by thermo-siphon circulation of liquid stream 33 through exchanger G and back into the fractionator via pipe 34. Stream 33 circulates at the rate of 1,014,470 moles per day and enters exchanger G at about l53F. Stream 34 exits the exchanger at a temperature of l5l.5F and consists of 723,860 moles per day of liquid and 290,610 moles per day of vapor.  
  Stream 17 is removed from the bottom of separator D at about F and about 179 psia, and comprises the bulk of the liquefied natural gas, now essentially free of nitrogen. It is reduced to atmospheric pressure. This is accomplished by letting the pressure down to atmospheric in two (or more) steps as shown by passage through valves 16 and 20. Flashed gases 22 and 23 are used to help cool the incoming feed gas and then recycled. The final LNG product in pipe 21 has the following flow rate:  
  Flow, Component Moles per Day Helium Nitrogen 3 l 7 Methane 669.700 Ethane 64,767 Propane 20,628 lsobutanc 3,666 n-Butane 5,484 C I29 Temp. F 257 Press, psia l Whie preferred operating conditions of temperature, pressure, compositions, etc. have been given for the practice of our invention, it should be understood that we may operate ouside the previously specified conditions at some decrease in operating efficiency depending on the extend of departure from the optimum conditions. The nitrogen content of the feed gas passed to the plant via pipe 1 may, for example, vary from about 1 mol percent to about 50 mol percent although it will usually be in the range of from about 2 mol percent to about 25 mol percent. The other components in the natural gas feedstock may also vary somewhat in concentration as no two natural gaes from different gas fields have percisely the same composition. Our invention lies in the separation of nitrogen from a natural gas and is relatively immune to, say the concentration of propane or butane in the feed gas.  
  Operating conditions for the nitrogen removal fractionator C will vary somewhat depending on the nitrogen content of the feed gas. Fractionator C will generally be operated at higher pressures and lower temperatures as the nitrogen content of the feed gas increases. For example, fractionator C may be operated in the range of from I00 to 1,000 psig, preferably in the range of from 200 to 500 psig. Fractionator C may be operated with a temperature in the top ranging from about l0OF to about 300F, preferably in the range of from about l50F to about 225F. Temperature at the bottom of fractionator C may range from about 50F to about &#34;250F, preferably from about l00F to about 200F.  
  Temperature of stream 8 passing to fractionator C will vary depending on its nitrogen content, said stream being lower in temperature as its nitrogen content increases. Temperature of stream 8 may range from about 50F to about 225F, preferably from about 100F to about 200F. To reduce the temperature of stream 8 to a lower level, it is necessary to flash stream 10 to a lower pressure in separator D in order to obtain a colder refrigerating stream 14 for use in cooling said stream 8 in exchanger G. Pressure in separator D may range from about 50 psia to about 300 psia. preferably from about 100 psia to about 200 psia. Temperature of stream 10 may vary from about 75F to about 300F, preferably from about lF to about 250F.  
  With the pressure in flash separator D ranging from 50 psia to about 300 psia, the pressure in flash separator E will range from atmospheric (separator F not needed) to about 200 psia, preferably from about atmospheric to about 250 psia. Pressure in separator F, if needed, will be atmospheric preferably but can be maintained at slightly elevated pressure of up to about 50 psig.  
  Reasonable variation and modification are possible within the scope of the foregoing disclosure, the drawing and the appended claims to the invention the essence of which is that there has been provided a process for the removal of an impurity, e.g., nitrogen, from a natural gas containing the same in substantial proportion which comprises compressing the gas, refrigerating the gas, separating the gas into a liquid and vapor component, refrigerating the liquid component, combining the gas and liquid component, further refrigerating the combined gas and liquid component and flashing the same into a fractionation zone wherefrom an overhead containing nitrogen is obtained and used as a heat exchange medium for further refrigerating said liquid component, bottoms from the fractionation zone are used at least in part to refrigerate the feed thereto thus to heat said portion of bottoms wherewith to reboil the fractionation zone and another portion of said bottoms are flashed in several stages to obtain vapor which can be used to further refrigerate said liquid component and a liquid which can be used and is used to further refrigerate the feed coming to the fractionation zone generating vapors which vapors can be used to further refrigerate said liquid component and a remaining portion of said fractionation zone bottoms which have been flashed or further processed to recover the natural gas substantially free from nitrogen.  
 We claim:  
  1. In a process for removing nitrogen as an impurity from natural gas comprising refrigerating said gas, generating a liquid portion and a vapor portion, separating the vapor and liquid portions from each other and further refrigerating the separated liquid portion in a first refrigeration zone, the improvement comprising the steps of l. combining the thus refrigerated liquid portion with said vapor portion and cooling the combined portion in a second refrigeration zone under conditions to substantially liquefy the combined portion,  
 2. reducting the pressure of said substantially liquefied mixture obtained in step (1) to flash the liquefied combined portion into a vapor portion and a liquid portion and introducing the flashed mixture into a fractionation zone,  
 3. subjecting said flashed mixture to temperature and pressure conditions in said fractionation zone sufficient to separate substantially all of the nitrogen as a vapor overhead stream and a bottoms liquid stream substantially free of nitrogen,  
 4. passing said vapor overhead stream obtained in step (3) in heat exchange relationship with said separated liquid portion in said first refrigeration zone to cool and refrigerate said liquid portion,  
 5. passing a portion of said bottoms liquid stream obtained in step (3) in heat exchange relationship with said combined portion in said second refrigeration zone and returning same to a lower portion of said fractionation zone as a source of reboiling heat,  
 6. reducing the pressure of the remainder of said bottoms liquid stream obtained in step (3) to flash same into a vapor portion and a liquid portion and introducing the flashed stream into a separation zone,  
 7. removing a liquid stream from said separation zone and passing a portion of said stream in heat exchange relationship with said combined portions in said second refrigeration zone and returning same to an upper portion of said separation zone as reflux and 8. removing a vapor stream from said separation zone and passing same in heat exchange relationship with said liquid portion in said first refrigeration zone.  
  2. A process according to claim 1 wherein the remaining portion of said liquid stream removed from said separation zone is further flashed to obtain nitrogen-containing gas therefrom and a final liquefied natural gas substantially free from nitrogen, and further wherein said vapor stream obtained from said separation zone upon use as a refrigerant in said first refrigeration zone is removed as a fuel gas containing nitrogen.  
  3. A process according to claim 1 wherein said fractionation zone is operated under conditions in which the upper portion of the fractionation zone is at a temperature in the range of 1 00 to300F and the bottom portion of the fractionation zone is at a temperature in the range of 50 to 250F, and the temperature of the combined vapor and liquid stream after refrigeration in said second refrigeration zone is at a temperature in the range of 50 to 225F.  
  4. A process according to claim 1 wherein the temperature of the liquid bottoms stream separated from said fractionation zone in step (3) is in the range of to -300F and the stream is flashed by reducing the pressure sufficiently to a pressure in the range of 50 to 300 psia to form a vapor portion and liquid portion. =l l= l