USRE23463E - Process of producing oxygen - Google Patents

Process of producing oxygen Download PDF

Info

Publication number
USRE23463E
USRE23463E US23463DE USRE23463E US RE23463 E USRE23463 E US RE23463E US 23463D E US23463D E US 23463DE US RE23463 E USRE23463 E US RE23463E
Authority
US
United States
Prior art keywords
nitrogen
air
rectification
temperature
heat exchange
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Expired
Application number
Publication date
Application granted granted Critical
Publication of USRE23463E publication Critical patent/USRE23463E/en
Expired legal-status Critical Current

Links

Images

Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air

Definitions

  • This invention relate to the production of oxygen by the liquefaction and rectification of air, and more particularly to the operation of the usual two-stage rectification column and associated heat exchangers.
  • Oxygen is commonly produced by partial liquefaction of air and rectification at low temperatures; preferably rectification is conducted in two stages at different pressures.
  • the refrigeration necessary for liquefaction is supplied to the air after it has been compressed and water-cooled to approximately room temperature, by indirect heat exchange with the eifluent products of rectification.
  • an additional amount of refrigeration must be supplied to compensate for cold losses resulting from the difference in enthalpy between the incoming air and the out- 80111: products of rectification and for heat leaks into the system.
  • Methods of supplying this refrigeration heretofore used involve compressing at least a portion of the incoming air to pressures as high as 3000 pounds and expanding with or without the performance of work to produce a temperature drop; or compressing all the incoming air to about 600 pounds and after the air has been partially cooled by the products of rectification expanding a portion of the air. These methods are wasteful from the standpoint of compressor energy and require a great deal of equipment in the form of extra compressors, intercoolers and expanders.
  • heat exchangers cold accumulators or regenerators (hereinafter referred to as heat exchangers) of large cold absorbing capacity through which the warm in- Matter enclosed in heavy brackets I: 1 appears in the original patent but forms no part of this reissue specification; matter printed in italics indicates the additions made by reissue.
  • the air stream fiowing from the first exchanger to the second is refrigerated, the amount of cold thus introduced into the process being adequate to compensate for cold losses resulting from the difference in enthalpy between the air introduced into and the products of rectification withdrawn from the process and for heat leaks into the system.
  • the temperature conditions in the first exchanger are such that substantially all moisture present in the air is removed therefrom in the form of frost.
  • the temperature conditions in the second exchanger are such as to effect substantially complete removal of carbon dioxide from the air in its passage therethrough.
  • a temperature diiference in the range of about 5 to about 10 F., preferably about 6 to about 8 F.
  • This temperature difference is the difference between the temperature of the air and the weighted average temperature of the products of rectification, all temperatures being taken at the colder end of the second exchanger.
  • the weighted average temperature 01' the products or rectification is calculated by multiplying the temperature of the oxygen product stream by the volume percentage of the stream based on the combined volume of the products of rectification and adding thereto the corresponding figure obtained by multiplying the temperature of the nitrogen product stream by its volume percentage.
  • the rectification system is operated to produce two streams 01 substantially pure oxygen and pure nitrogen, the weighted average temperature of the two streams would be approximately the sum of 20% of the oxygen stream temperature and 80% of the nitrogen stream temperature.
  • the fiow of air and nitrogen through their respective paths in the two exchangers is reversed so that upon reversal the air flows through the paths in the two exchangers through which during the preceding step the nitrogen had passed and the nitrogen flows through the paths in the two exchangers through which had previously passed the air.
  • the nitrogen removes, by sublimation, the carbon dioxide deposited during the preceding step in the second exchanger and the frost deposited during the preceding step in the first exchanger;
  • This invention is in the nature of an improvement on the invention disclosed and claimed in the aforesaid copendirig application. It is an object of this invention to effect removal of incondensibles, such as hydrogen, helium and neon, from the rectification system without reduction in the yield of oxygen recovered in the process. A further object is to increase the efiiciency of the operation of the rectification system. Other objects and advantages of this invention will be apparent from the following detailed description.
  • a stream of air is passed through a path in two zones in series, each of the zones containing at least three paths in heat exchange relation with each other and streams of oxygen and nitrogen rectification products are passed through the other two paths in these zones in heat exchange relation with the air passing therethrough.
  • One of the streams is cooled in its flow between the first and second zones to a temperature sufilcient to supply to the system the necessary cold to compensate for cold losses resulting from the difierence in enthalpy between the incoming air and the outgoing products of rectification and for heat leaks into the system.
  • the temperature difierence between the temperature of the air leaving and the temperature of the rectification products entering the second zone is maintained within the range 01' from about 5 to about 10 F. and the exit temperature of the air leaving: this zone is such as'to eflect substantially complete removal.
  • a minor portion of the nitrogen withdrawn from the high-pressure stage of the rectification system is passed through the second zone where the nitrogen is heated by the air stream flowing to the high-pressure stage of the rectification system.
  • the heated nitrogen is then mixed with the remainder of the nitrogen withdrawn from the high-pressure stage of the rectification system thereby increasing the temperature of the nitrogen, preferably not more than 20 F., and the mixed nitrogen stream thus introduced into the expander at a temperature such that no liquid nitrogen is formed within the expander with consequent improvement in the efilciency of the operation of the expander.
  • the equipment shown for the practice of the process involves a pair of heat exchangers having an ethylene refrigeration system for refrigerating the air and the present description will be confined to the present illustrated embodiment of the. invention. It will be understood, however, that the process may be carried out in other equipment, for example, each of the two exchangers in series may be replaced by two or more smaller exchangers placed in series and/or parallel, if desired, although this is objectionable from the standpoint of increasing construction costs, or the number of heat exchange paths in each exchanger may be increased over the 3-path construction shown in the drawing, or other refrigeration systems may be employed in lieu of the ethylene system. Hence, the scope of the invention is not confined to the embodiment herein described.
  • I0 indicates a heat exchanger which may be of any wellknown type.
  • it consists of a single shell in which are provided three paths, namely, interior path ll through which fiows in one and the same direction throughout the operation of the exchanger the oxygen product. 01' rectification.
  • Paths l2 and I3 are provided within the shell of the exchanger through which periodically fiow air and the nitrogen product of rectification in heat exchange relation with each other and with the oxygen.
  • the heat exchanger has in each of the paths suitable fins of heat-conducting material. e. g., copper, promoting rapid 'and efiicient heat exchange between the gaseous media flowing therethrough.
  • suitable fins of heat-conducting material e. g., copper
  • Valve I4 is disposed in the pipe line system consisting of air inlet pipe l3 leading into valve I4, and pipe lines l1 and I3 leading from the valve to coolin paths l2 and I3, respectively.
  • At the base of the heat exchanger l lines l3 and 23 are positioned leading from paths l2 and I3, respectively, to the valve l3.
  • is provided in the form of a shell having therein paths 22, 23 and 24 provided with fins to promote heat exchange as in the case of the exchanger l3.
  • Path 24 is the path through which the oxygen product of rectiflcation flows from the rectification system hereinafter described to a pipe line 25 which communicates with path ll of heat exchanger In.
  • communicate with pipe lines 23 and 21, respectively, which are communicably connected with a compound valve 23 which may be of the same type as valves I4 and I5.
  • At the upper portions paths 22 and 23 communicate respectively with lines 23 and 30 which in turn communicate with a compound reversing valve 3
  • may be placed in vertical, horizontal or any other desired position. Likewise, when these exchangers are arranged vertically, the colder end may be above or below the warmer end.
  • a refrigeration system 32 of any well-known construction for supplying a refrigerating medium, such as ethylene or carbon tetrafluoride is provided for cooling either the nitrogen flowing from heat exchanger 2
  • This refrigerating system operates to cause the flow of the refrigerating medium in indirect heat exchange relation with the nitrogen or air to be cooled, the rate of flow and term perature of the various media being so controlled that enough cold is introduced by refrigeration, at this point in the process, to compensate for cold losses resulting from the difference in enthalpy between the incoming air and the outgoing products of rectification and for heat leaks into the system.
  • the air leaving the heat exchanger I3 is refrigerated to cause a drop of about 5 to about F. in its temperature; this has been found adequate for the purposes above stated. Refrigeration of the air is accomplished by causing it to flow through pipe line 33 which passes through the refrigerator 32 in indirect heat exchange with the refrigerant and communicably connects valves l5 and 23. Line 3 is the nitrogen line between the two heat exchangers III and 2
  • the desired amount of refrigeration may be introduced into the system by expanding a portion of the air, say about 7% of the total air introduced into the system.
  • the cold expanded air thus produced may be introduced into the nitrogen stream entering the heat exchanger l3 thereby supplying the necessary cold to compensate for cold losses resulting from the difference in enthalpy between the incoming air and the outgoing. products of rectification and for heat leaks into the system.
  • This latter method has the disadvantage that it involves a loss of approximately 7% of the oxygen content of the air introduced into the system.
  • it has the advantage that it eliminates the necessity for using a refrigeration system for cooling either the nitrogen or air, which system is more cumbersome and expensive in construction and operation than an expander of the type suitable for expanding a relatively small amount of air at a relatively low pressure, e. g., -85 pounds gauge.
  • may be periodically reversed, say every three minutes, so that during an initial period of operation air flows through heat exchange path
  • the rectification system comprises a two-stage rectification column 31, the lower section 33 of which is operated at a pressure of about 12 pounds gauge and the upper section 33 of which is operated at a pressure of from about 4 pounds to about 10 pounds gauge, preferably at about 5 pounds gauge.
  • This column as is customary is provided with rectification plates of the bubblecap or other desired type.
  • the lower section 33 of the column 31 communicates with a condenser 43 and has a liquid collecting shelf 4
  • Pipe line 42 leads from this shelf 4
  • Condenser 43 acts as a reboiler for the upper section 33 of the column 31.
  • a pipe line 43 for the flow of crude oxygen passes to a non-reversing heat exchanger 41 which communicates with pipe line 43 having a pressure reducing valve 43 therein with the low pressure section 33 at an intermediate point indicated by 7 the reference character ll.
  • Line It leads fro the top of the condenser 40 and has a regulating valve 52 therein.
  • This line communicates with an expander "which discharges by way of line 53a into line 54 hereinafter described.
  • a branch line It having a regulating valve II and leading to a path 60 disposed in heat exchanger 2! in indirect heat exchange relation with the oxygen. nitrogen and air passing through the other three paths in this exchanger 2
  • leads from path 80 backto line 3
  • a minor portion of the total nitrogen introduced into the process passes through line and, preferably, 01' the portion thus withdrawn a minor portion, say about passes through line 58, path 60 and line 8
  • the portion of nitrogen passing through path 60 is warmed up by indirect heat exchange, and by mixing with the remainder of the nitrogen, the stream entering expander 53 is at a temperature suflicient to avoid condensation or formation of liquid nitrogen in the expander.
  • the nitrogen stream refrigerated as a result of the expansion flows from the expander 53 to a line 53a which meets line 54 conveying the nitrogen stream leaving the top oi low-pressure section 39.
  • the mixture then flows through heat exchanger 43 in indirect heat exchange relation with the nitrogen passing through this exchanger and thereafter flowing through reducing valve 44 into the top of low-pressure section 39.
  • the mixed nitrogen stream flows through line 55 changer 41 where it flows in indirect heat exchange relation with the crude oxygen flowing therethrough to low-pressure section 39.
  • the mixed nitrogen stream passes through line 55 into and through heat exchanger where it passes in indirect heat exchange relation with air flowing into and from this exchanger by way of line 34.
  • the heat exchangers 35, 43 and 41 and the twostage fractionating column 31 may be of any conventional type. Two separate fractionating columns, suitably interconnected may be used in place of the two-stage column 31 shown. It will into and through heat ex- I be understood that the equipment throughout is heat insulated to minimize loss of cold.
  • Air under pressure of about pounds gauge and temperature of about 100 F. is supplied through line it, valve I4 and line H to heat exchanger i0, flowing through path l2 in which it is cooled to a temperature of 134.5 F.
  • the air then flows in indirect heat exchange relation with ethylene in the refrigeration system 22 and is cooled thereby to a temperature of -142 F., then passes through path 22 of the heat exchanger 2
  • Substantially all moisture is removed in the form of frost in path l2 of heat exchanger l0 and all carbon dioxide is removed in solidified form in path 22 of heat exchanger 2
  • the air then flows through the heat exchanger 35 in heat exchange relation with nitrogen enters high-pressure column 33 at a temperature of -278 F. and a pressure of 72 pounds.
  • Nitrogen at a temperatune of about 286.5 F. and a pressure of 72 pounds in amount equal to 12.5% by volume of the total nitrogen introduced into the process is withdrawn through line 5
  • 10% passes through line 58 and path 60, its temperature being increased to 146 F.
  • the remaining 90% of the nitrogen flows through valve 52 in line 5i and is mixed with the other 10% nitrogen, the temperature of the mixture being about -2'77 pander 53 is at a pressure of 5 pounds and a temperature of 315 F.
  • the expanded nitrogen flows through line 53a and becomes mixed with nitrogen at a temperature of 315.5 F. and a pressure of 5 pounds flowing through line 54.
  • the resultant nitrogen stream passes through exchanger 43 in indirect heat exchange relation with nitrogen employed as reflux in column 39, its temperature being thereby increased to 306" F. while the temperature of nitrogen flowing through line 42 (pressure of 72 pounds) and exchanger 43 is reduced to -300 F.
  • This nitrogen by expansion through valve 44- has its pressure reduced to 5 pounds and its temperature to -315.5
  • the nitrogen product of rectification then flows through heat exchanger 41 where its temperature is increased to 293 F.
  • the crude oxygen stream flowing through exchanger 41 is thereby cooled from a temperature of 280 F. to a temperautre of -289 F.
  • the nitrogen then flows through exchanger 35 in heat exchange F.
  • the nitrogen stream temperature being thereby increased to -2'79 F. at which temperature it enters the heat exchanger 2
  • the nitrogen and the oxygen streams have a weighted average temperature of nearly --282 F. while at this point the air is at a temperature of 2'75 F. A temperature difference of about 1 F. is therefore maintained. It will be noted that at the point where the air enters and the oxygen and nitrogen leave the heat exchanger 2
  • the nitrogen fiows through heat exchanger H! where it is heated to 90 F.
  • the nitrogen at this temperature and a pressure slightly above atmospheric, say 1 pound gauge, may be vented to the atmosphere thereby venting the lncondensibles, such as hydrogen, helium and neon, removed from the high-pressure stage of the rectification system.
  • the desired oxygen product is withdrawn through line 51 at a temperature of --292.5 F. and pressure or 5 pounds, flows through heat exchanger 2
  • the oxygen leaves exchanger III at a pressure of 1 pound.
  • the purging is carried out so as to increase vthe efllciency of the rectification system in that the nitrogen stream containing the incondensibles is expanded and the refrigeration thus produced employed to cool the refiux oxygen and nitrogen introduced into the low-pressure stage and the air introduced into the high-pressure stage.
  • this invention provides a process for producing oxygen of high purity without the use of chemical agents, which process may be operated continuously over a long period of time without shut-downs for the purpose of removing solid carbon dioxide or frost, which process is economical to operate, particularly in that the refrigeration which must be supplied to compensate for cold losses resulting from the difference in enthalpy between incoming air and the outgoing products of rectification and for heat leaks into the system is supplied at a point in the process where the temperatures are relatively high so that it can be supplied efllciently and economically, and which process effects continuous purging from the high-pressure stage of the rectification system of the incondensible constituent
  • a process for producing oxyygen by the liquefaction and rectification of air which comprises passing a stream of air through a path in two zones in series, each of said zones containing at least three paths in heat exchange relation with each other, passing respectively streams of oxygen and nitrogen products of rectification through two other paths in said zones in heat exchange relation with the air passing therethrough, cooling at least one or said streams during its fiow between the first zone and the second zone, withdrawing the air from the second zone at a temperature such that substantially all carbon dioxide in said air has been removed from the air in its passage through its path in said second zone, maintaining the temperature difference between the temperature of the air leaving and the weighted average temperature of the nitrogen and oxygen entering said second zone so that it falls within the range of from about 5 to about 10 F., passing the air from said second zone to the high-pressure stage of a two-stage rectification system in indirect heat exchange relation with a rectification product from the low-pressure stage of said system, withdrawing a minor portion of the nitrogen from the high-pressure stage, expanding the nitrogen thus
  • a process for producing oxygen by the liquefaction and rectification of air which comprises passing a stream of air at about '70 pounds to about pounds gauge and a temperature of about 70 to about F. through a path in two zones in series, each of said zones containing with each other, passing respectively streams of A process and for heat leaks into the system, withdrawing the air from the second zone at a temperature such that substantially all carbon dioxide in said air has been removed from the air in its passage through its path in said second zone, maintaining the temperature diflerence between the temperature of the air leaving and the weighted average temperature of the nitrogen and oxygen entering said second zone so that it falls within the range of from about to about F., passing the air from said second zone to the high-pressure stage of a two-stage rectification system in indirect heat exchange relation with a rectification product from the low-pressure stage of said system, withdrawing a minor portion of the nitrogen containing incondensible gases from the high-pressure stage, expanding the nitrogen thus withdrawn to cool the same, passing the expanded nitrogen in heat exchange relation
  • a process for producing oxygen by the liquefaction and rectification of air which comprises passing a stream 01' air at about 70 pounds to about 85 pounds gauge and a temperature of about 70 to about 110 F. through a path in two zones in series, each of said zones containing three paths in heat exchange relation with each other, passing respectively streams of oxygen and nitrogen products of rectification through the two other paths in said zones in heat exchange relation with the air passing therethrough, cooling at least one of said streams during its flow from one zone to the other, the amount of cold thus introduced into the process being adequate to compensate for cold losses resulting from the difference in enthalpy between the air introduced into and the products of rectification withdrawn from the process and for heat leaks into the system, withdrawing the air from the second zone at a temperature such that substantially all carbon dioxide in said air has been removed from the air in its passage through its path in said second zone, maintaining the temperature difierence between the temperature 01 the air leaving and the weighted average temperature of the nitrogen and oxygen entering said second zone so that it falls within the range of from about 5
  • a process for producing oxygen by the lique faction and rectification or air which comprises passing air at about to about pounds gauge and a temperature of about 70 to about F. through a path in a zone containing three paths in heat exchange relation with each other, flowing oxygen and nitrogen products of rectification respectively through the other two paths in said zone in heat exchange relation with the air, the air thus being cooled to a temperature sufficient- 1y low to deposit out as frost substantially all the moisturein the air, refrigerating the air leaving the first zone to lower its temperature about 5 to 10 F., then further cooling the air by flowing it through a path in a second zone containing three paths, flowing oxygen and nitrogen prodnets of rectification respectively through the other two paths in said second zone in heat exchange relation with the air thereby cooling the air to a temperature sufliciently low to deposit out substantially all the carbon dioxide in the air, the differential between the temperature of the air and the weighted average temperature of the oxygen and nitrogen at the colder end of said second zone being within the range of about 5 to about 10 F.,
  • a process for producing oxygen by the liquefaction and rectification of air which comprises passing a stream of air at about '70 pounds to about 85 pounds gauge and a temperature of about 70 to about 110 F. through a path in two zones in series, each of said zones containing three paths in heat exchan e relation with each other, passing respectively streams of oxygen and nitrogen products of rectification through the two other paths in said zones in heat exchange relation with the air passing therethrough.
  • a process for producing oxygen by the liquefaction and rectification of air which comprises passing a stream of rectification product through a path in a heat exchange zone, passing a stream of air through another path in said heat exchange zone to recover the cold content of the rectification product stream, thereby cooling the air to a temperature close to its condensation point at the pressure prevailing in said heat exchange zone and eflecting substantially complete removal of carbondioxide from the air in its passage through said heat exchange zone, passing the air from said heat exchange zone to the highpressure stage of a two-stage rectification system, withdrawing from said high-pressure stage a gaseous stream rich in nitrogen, warming the gaseous stream thus withdrawn to a temperature such that upon expansion to produce refrigeration said gaseous stream is'not liquefied by passing at least a portion of said gaseous stream through still another path in at least the colder end of said heat exchange zone in heat exchange relation with the streams of air and rectification product passing through said heat exchange zone, expanding the thus warmed gaseous stream to produce refrigeration without
  • a process for producing oxygen by the liquefaction and rectification of air which comprises passing a stream of nitrogen rectification product through a path in a heat exchange zone. passing a stream of air through another path. in said heat exchange zone to recover the cold content of the nitrogen rectification product stream, thereby cooling the air to a temperature close to its condensation point at the pressure prevailing in said heatexchange zone and eflecting substantially complete removal of carbon dioxide from the air in its passage through saidflheat exchange zone.
  • a process for producing oxygen by the liquefaction and rectiflcation of air which comprises passing a stream of air through a path in a heat exchange zone containing four paths in heat exchange relation with each other, passing respectively streams of oxygen and nitrogen products of rectiflcation through two of the other paths in said heat exchange zone in heat exchange relation with the air passing therethrough, withdrawing the air from said heat exchange zone at a temperature such that substantially all carbon dioxide in the air has been removed from the air in its passage through said heat exchange zone, passing the air from said heat exchange zone to the high-pressure stage of a two-stage rectiflcation system, withdrawing a portion of the nitrogen product from said highpressure stage and'warming said portion to a temperature such that upon expansion to produce refrigeration said portion is not liquefied by passing at least a part of said portion through still another of said four paths in at least the colder end of said heat exchange zone in heat exchange relation with the streams of air and oxygen and nitrogen rectification products passing through said heat exchange zone, expanding the thus warmed portion to produce refrigeration without liquefaction of
  • a process for producing oxygen by the liquefaction and rectiflcation of air which comprises passing a stream of air through a path in two heat exchange zones in series, each of said zones containing three paths in heat exchange relation with each other, passing respectively streams of oxygen and nitrogen products of rectiflcation through the two other paths in said zones countercurrent to the air passing therethrough, thereby cooling the air leaving the second zone to a temperature sufncient to remove substantially all carbon dioxide therefrom, the carbon dioxide thus removed being deposited in said second zone, passing the air from said second zone to the highpressure stage of a two-stage rectification system, withdrawing from said high-pressure stage nitrogen containing incondensible gases, warming the nitrogen thus withdrawn to a temperature such that upon expansion to produce refrigeration said nitrogen is not liquefied by passing at least a portion of said nitrogen through a fourth path in said second zone in heat exchange relation with the streams of air and oxygen and nitrogen rectiflcation products passing through said second zone, expanding the thus warmed nitrogen to produce refrigeration without liquefaction of said nitrogen, passing the

Description

Feb. 26, 1952 F. J. JENNY ETAL PROCESS OF PRODUCING OXYGEN Original Filed Dec. 5, 1945 INVENTO RS 0 Y m M v n WM m C T m A 0 d w a Md T We at. 26, 1952 Re; 23,463
PROCESS OF PRODUCING OXYGEN Frank J. Jenny, New York, N. Y., and Edward G. Scheibel, Montclair, N. 1., assignors to Hydrocarbon Research, Inc., New York, N. Y.
Original No. 2,552,558, dated May 15, 1951, Serial No. 632,859, December 5, 1945. Application for reissue August 3, 1951, Serial No. 240,256
13 Claims.
This invention relate to the production of oxygen by the liquefaction and rectification of air, and more particularly to the operation of the usual two-stage rectification column and associated heat exchangers.
All temperatures herein given are in degrees F. and pressures are in pounds per square inch gauge.
Oxygen is commonly produced by partial liquefaction of air and rectification at low temperatures; preferably rectification is conducted in two stages at different pressures. The refrigeration necessary for liquefaction is supplied to the air after it has been compressed and water-cooled to approximately room temperature, by indirect heat exchange with the eifluent products of rectification. However, an additional amount of refrigeration must be supplied to compensate for cold losses resulting from the difference in enthalpy between the incoming air and the out- 80111: products of rectification and for heat leaks into the system. Methods of supplying this refrigeration heretofore used, involve compressing at least a portion of the incoming air to pressures as high as 3000 pounds and expanding with or without the performance of work to produce a temperature drop; or compressing all the incoming air to about 600 pounds and after the air has been partially cooled by the products of rectification expanding a portion of the air. These methods are wasteful from the standpoint of compressor energy and require a great deal of equipment in the form of extra compressors, intercoolers and expanders.
For economical operation it is essential to recover the cold content of the outgoing products of rectification. This is usually accomplished by passing these products in heat transfer relationship with the incoming air. In older systems in order to avoid deposition of frost and solid car'- bon dioxide in the tubular countercurrent heat exchangers through which the air is passed in indirect heat exchange relation with the outgoing products of rectification, the air is treated in driers and caustic scrubbers to remove water and carbon dioxide prior to admittance of the air into the heat exchangers. Even with this treatment the exchangers had to be thawed out regularly to remove the frost (which term is used in a generic sense to include both snow and ice) which caused stopping up of the apparatus.
More recently it has been suggested to use cold accumulators or regenerators (hereinafter referred to as heat exchangers) of large cold absorbing capacity through which the warm in- Matter enclosed in heavy brackets I: 1 appears in the original patent but forms no part of this reissue specification; matter printed in italics indicates the additions made by reissue.
coming air and the cold products of rectification are alternately passed with periodically reversed operation so that streams of warm air are flowed through the same packing filled spaces that the cold separated oxygen and nitrogen traversed during the previous step in the process, the high boiling impurities deposited in these spaces during the passage of air therethrough being removed by sublimation during the subsequent flow in a reverse direction of the products of rectification. The use of these reversing heat exchangers in a process in which the air is compressed to relatively high pressure results in more costly operation from the standpoint of horsepower requirements because upon every reversal, which may take place every three minutes, the volume of compressed air in the heat exchangers is lost and must be again replaced.
In copending application Serial No. 632,858 filed December 5, 1945, now U. S. Patent No. 2,552,557, there is disclosed and claimed a process for producing oxygen by liquefaction and rectification of air involving the fiow of air at about to about pounds at a temperature of about 70 to about F. through the heat exchange paths of two or more reversing heat exchangers in series, each exchanger containing two other paths through which are passed respectively streams of oxygen and nitrogen products of rectification in heat exchange relation with the air passing therethrough. The air stream fiowing from the first exchanger to the second is refrigerated, the amount of cold thus introduced into the process being adequate to compensate for cold losses resulting from the difference in enthalpy between the air introduced into and the products of rectification withdrawn from the process and for heat leaks into the system. The temperature conditions in the first exchanger are such that substantially all moisture present in the air is removed therefrom in the form of frost. The temperature conditions in the second exchanger are such as to effect substantially complete removal of carbon dioxide from the air in its passage therethrough.
At the colder end of the second exchanger where the oxygen and nitrogen products of rectification enter and air leaves the exchanger, thereis maintained between these products of rectification and the countercurrent stream of air a temperature diiference in the range of about 5 to about 10 F., preferably about 6 to about 8 F. This temperature difference is the difference between the temperature of the air and the weighted average temperature of the products of rectification, all temperatures being taken at the colder end of the second exchanger. For. the
purposes 01' this-invention, the weighted average temperature 01' the products or rectification is calculated by multiplying the temperature of the oxygen product stream by the volume percentage of the stream based on the combined volume of the products of rectification and adding thereto the corresponding figure obtained by multiplying the temperature of the nitrogen product stream by its volume percentage. Thus, for example, it the rectification system is operated to produce two streams 01 substantially pure oxygen and pure nitrogen, the weighted average temperature of the two streams would be approximately the sum of 20% of the oxygen stream temperature and 80% of the nitrogen stream temperature. Periodically the fiow of air and nitrogen through their respective paths in the two exchangers is reversed so that upon reversal the air flows through the paths in the two exchangers through which during the preceding step the nitrogen had passed and the nitrogen flows through the paths in the two exchangers through which had previously passed the air. The nitrogen removes, by sublimation, the carbon dioxide deposited during the preceding step in the second exchanger and the frost deposited during the preceding step in the first exchanger;
Operating in this manner complete purging of carbon dioxide is attained upon each reversal or flow. Likewise complete purging of frost is obtained so that the equipment may be operated continuously.
This invention is in the nature of an improvement on the invention disclosed and claimed in the aforesaid copendirig application. It is an object of this invention to effect removal of incondensibles, such as hydrogen, helium and neon, from the rectification system without reduction in the yield of oxygen recovered in the process. A further object is to increase the efiiciency of the operation of the rectification system. Other objects and advantages of this invention will be apparent from the following detailed description.
In accordance with this invention a stream of air is passed through a path in two zones in series, each of the zones containing at least three paths in heat exchange relation with each other and streams of oxygen and nitrogen rectification products are passed through the other two paths in these zones in heat exchange relation with the air passing therethrough. One of the streams is cooled in its flow between the first and second zones to a temperature sufilcient to supply to the system the necessary cold to compensate for cold losses resulting from the difierence in enthalpy between the incoming air and the outgoing products of rectification and for heat leaks into the system. The temperature difierence between the temperature of the air leaving and the temperature of the rectification products entering the second zone is maintained within the range 01' from about 5 to about 10 F. and the exit temperature of the air leaving: this zone is such as'to eflect substantially complete removal.
of carbon dioxide from the air in its passage through its path in this zone. From this second zone the air is passed to the high-pressure stage of a two-stage rectification system in indirect heat exchange relation with rectification products from the low-pressure stage of the system.
A minor portion of the nitrogen introduced into the process and containing incondensible gases is withdrawn from the high-pressure stage, ex-
panded to cool the same and the cold thus produced imparted to the rectification products entering the low-pressure stage and preferably also to the air entering the high-pressure stage. Periodically the flow of air and nitrogen is reversed through their respective paths in the two zones, the air upon reversal flowing through the paths through which had previously flowed the nitrogen and the nitrogen flowing through the paths through which had previously flowed the air, whereby upon each reversal the nitrogen substantially completely removes the carbon dioxide deposited in the second zone during the preceding step of the process.
In the preferred embodiment of the invention. a minor portion of the nitrogen withdrawn from the high-pressure stage of the rectification system is passed through the second zone where the nitrogen is heated by the air stream flowing to the high-pressure stage of the rectification system. The heated nitrogen is then mixed with the remainder of the nitrogen withdrawn from the high-pressure stage of the rectification system thereby increasing the temperature of the nitrogen, preferably not more than 20 F., and the mixed nitrogen stream thus introduced into the expander at a temperature such that no liquid nitrogen is formed within the expander with consequent improvement in the efilciency of the operation of the expander.
In the preferred embodiment illustrated in the drawing, the single figure of which illustrates diagrammatically a preferred layout of apparatus for practicing the. process of this invention, the equipment shown for the practice of the process involves a pair of heat exchangers having an ethylene refrigeration system for refrigerating the air and the present description will be confined to the present illustrated embodiment of the. invention. It will be understood, however, that the process may be carried out in other equipment, for example, each of the two exchangers in series may be replaced by two or more smaller exchangers placed in series and/or parallel, if desired, although this is objectionable from the standpoint of increasing construction costs, or the number of heat exchange paths in each exchanger may be increased over the 3-path construction shown in the drawing, or other refrigeration systems may be employed in lieu of the ethylene system. Hence, the scope of the invention is not confined to the embodiment herein described.
In the drawing reference character I0 indicates a heat exchanger which may be of any wellknown type. In the embodiment shown in the drawings it consists of a single shell in which are provided three paths, namely, interior path ll through which fiows in one and the same direction throughout the operation of the exchanger the oxygen product. 01' rectification. Paths l2 and I3 are provided within the shell of the exchanger through which periodically fiow air and the nitrogen product of rectification in heat exchange relation with each other and with the oxygen. The heat exchanger has in each of the paths suitable fins of heat-conducting material. e. g., copper, promoting rapid 'and efiicient heat exchange between the gaseous media flowing therethrough. As the construction of the heat exchanger per se does not form part of this invention and as it may be of any well-known type. it is believed further description thereof is unnecessary.
The fiow of the air and nitrogen through their respective paths is periodically reversed so that during one step of the process air flows through path l2 and nitrogen through path I3, and upon reversal, during the succeeding step air flows through path l3 and nitrogen through path |2.
Reversal of flow is accomplished by suitably positioning the compound reversing valves l4 .and I! which may be of any well-known type. Valve I4 is disposed in the pipe line system consisting of air inlet pipe l3 leading into valve I4, and pipe lines l1 and I3 leading from the valve to coolin paths l2 and I3, respectively. At the base of the heat exchanger l lines l3 and 23 are positioned leading from paths l2 and I3, respectively, to the valve l3.
A second heat exchanger 2| is provided in the form of a shell having therein paths 22, 23 and 24 provided with fins to promote heat exchange as in the case of the exchanger l3. Path 24 is the path through which the oxygen product of rectiflcation flows from the rectification system hereinafter described to a pipe line 25 which communicates with path ll of heat exchanger In. The base portions of paths 22 and 23 of heat exchanger 2| communicate with pipe lines 23 and 21, respectively, which are communicably connected with a compound valve 23 which may be of the same type as valves I4 and I5. At the upper portions paths 22 and 23 communicate respectively with lines 23 and 30 which in turn communicate with a compound reversing valve 3| which may be of the same type as the other reversing valves.
Reversing exchangers l0 and 2| may be placed in vertical, horizontal or any other desired position. Likewise, when these exchangers are arranged vertically, the colder end may be above or below the warmer end.
A refrigeration system 32 of any well-known construction for supplying a refrigerating medium, such as ethylene or carbon tetrafluoride is provided for cooling either the nitrogen flowing from heat exchanger 2| to heat exchanger l3, or the air flowing from heat exchanger I3 to heat exchanger 2|. This refrigerating system operates to cause the flow of the refrigerating medium in indirect heat exchange relation with the nitrogen or air to be cooled, the rate of flow and term perature of the various media being so controlled that enough cold is introduced by refrigeration, at this point in the process, to compensate for cold losses resulting from the difference in enthalpy between the incoming air and the outgoing products of rectification and for heat leaks into the system. In the preferred embodiment of the invention the air leaving the heat exchanger I3 is refrigerated to cause a drop of about 5 to about F. in its temperature; this has been found adequate for the purposes above stated. Refrigeration of the air is accomplished by causing it to flow through pipe line 33 which passes through the refrigerator 32 in indirect heat exchange with the refrigerant and communicably connects valves l5 and 23. Line 3 is the nitrogen line between the two heat exchangers III and 2|.
Instead of refrigerating the nitrogen flowing from heat exchanger 2| to heat exchanger l3 thereby introducing the cold supplied by the refrigerating medium into the exchanger III, or instead of refrigerating the air flowing from heat exchanger ID to heat exchanger 2|, the desired amount of refrigeration may be introduced into the system by expanding a portion of the air, say about 7% of the total air introduced into the system. The cold expanded air thus produced may be introduced into the nitrogen stream entering the heat exchanger l3 thereby supplying the necessary cold to compensate for cold losses resulting from the difference in enthalpy between the incoming air and the outgoing. products of rectification and for heat leaks into the system. This latter method has the disadvantage that it involves a loss of approximately 7% of the oxygen content of the air introduced into the system. On the other hand it has the advantage that it eliminates the necessity for using a refrigeration system for cooling either the nitrogen or air, which system is more cumbersome and expensive in construction and operation than an expander of the type suitable for expanding a relatively small amount of air at a relatively low pressure, e. g., -85 pounds gauge.
With the arrangement of valves and piping shown flow of nitrogen and air through heat exchangers I3 and 2| may be periodically reversed, say every three minutes, so that during an initial period of operation air flows through heat exchange path |2, through line l3, valve l5, refrigeration system 32 by way of line 33, valve 23, line 23, cooling path 22 in heat exchanger 2 pipe line 23, valve 3| and thence to line 34 leading through the non-reversing heat exchanger 35 to the rectiflcation system hereinafter described. At the same time, nitrogen flows through pipe line 36 leading from the non-rever ing heat exchanger 35 into valve 3|, line 33, through path 23 in heat exchanger 2|, through line 21, valve 23, line 3, valve l3, pipe line 20, path I3 in heat exchanger l0, leaving this path through pipe line l3 and passing through valve H to the atmosphere or other suitable disposal point. Upon reversal (as shown by dotted arrows and valve settings), the air flows through valve |4, line l3, path I3, pipe line 23, valve l5, refrigeration system 32 .by way of line 33, valve 23, pipe line 21, and thence through the cooling path 23, leaving this cooling path through pipe line 30 and passing through valve 3| and pipe line 34 into the non-reversing exchanger 35. At the same time, the nitrogen flows from heat exchanger 35 through pipe line 36 into valve 3|, thence through pipe line 23, path 22 in heat exchanger 2|, pipe line 23, valve 23, line 3, valve l3, line H into path l2, thence through line H into valve I4 and thence to the atmosphere or other suitable disposal point.
The rectification system comprises a two-stage rectification column 31, the lower section 33 of which is operated at a pressure of about 12 pounds gauge and the upper section 33 of which is operated at a pressure of from about 4 pounds to about 10 pounds gauge, preferably at about 5 pounds gauge. This column as is customary is provided with rectification plates of the bubblecap or other desired type. The lower section 33 of the column 31 communicates with a condenser 43 and has a liquid collecting shelf 4| disposed immediately below the condenser 43 for collectin; liquid nitrogen. Pipe line 42 leads from this shelf 4| to a non-reversing heat exchanger 43 which in turn communicates through a pressure reducing valve 44 with the top portion of the upper section 33 as indicated by the reference character 43. Condenser 43 acts as a reboiler for the upper section 33 of the column 31.
From the base portion of the lower section 33 a pipe line 43 for the flow of crude oxygen (containing approximately 40% oxygen) passes to a non-reversing heat exchanger 41 which communicates with pipe line 43 having a pressure reducing valve 43 therein with the low pressure section 33 at an intermediate point indicated by 7 the reference character ll. Line It leads fro the top of the condenser 40 and has a regulating valve 52 therein. This line communicates with an expander "which discharges by way of line 53a into line 54 hereinafter described. Preterably. there is also provided a. branch line It having a regulating valve II and leading to a path 60 disposed in heat exchanger 2! in indirect heat exchange relation with the oxygen. nitrogen and air passing through the other three paths in this exchanger 2|. A line 6| leads from path 80 backto line 3|. Regulating valves 52 and 53 disposed in lines 3| and 58, respectively, regulate the portions of the nitrogen stream flowing from the condenser 40 which are passed directly to expander 53 and .indirectly through path of exchanger 2|.
By the arrangement of lines hereinabove described a minor portion of the total nitrogen introduced into the process passes through line and, preferably, 01' the portion thus withdrawn a minor portion, say about passes through line 58, path 60 and line 8| entering line 5| where it mixes with the remainder of the nitrogen withdrawn from the condenser 40. The portion of nitrogen passing through path 60 is warmed up by indirect heat exchange, and by mixing with the remainder of the nitrogen, the stream entering expander 53 is at a temperature suflicient to avoid condensation or formation of liquid nitrogen in the expander. In a preferred embodiment of the invention from about 1% to about by volume of the total nitrogen introduced into the process and containing incondensibles, such as hydrogen, helium and neon, is passed through line ill and of this quantity about 10% by volume passes through heating path 60 and 90% by volume continues through line II.
The nitrogen stream refrigerated as a result of the expansion flows from the expander 53 to a line 53a which meets line 54 conveying the nitrogen stream leaving the top oi low-pressure section 39. The mixture then flows through heat exchanger 43 in indirect heat exchange relation with the nitrogen passing through this exchanger and thereafter flowing through reducing valve 44 into the top of low-pressure section 39. From heat exchanger 43 the mixed nitrogen stream flows through line 55 changer 41 where it flows in indirect heat exchange relation with the crude oxygen flowing therethrough to low-pressure section 39. From the heat exchanger 4-! the mixed nitrogen stream passes through line 55 into and through heat exchanger where it passes in indirect heat exchange relation with air flowing into and from this exchanger by way of line 34. From the heat exchanger 35 the nitrogen stream flows through line 36 into a compound valve 3|, thence through path 22 or 23, as the case may be, of heat exchanger 2|, through valves 28 and I5 connected by line 9, then through path l2 or I! of heat exchanger l0 and finally through compound valve l4 to the atmosphere; the flow through path l2 or I3 of heat exchanger l0 depending upon the setting of valves l4 and I5 and the flow through path 22 or 23 of heat exchanger 2| depending upon the setting of valves 23 and 3i as hereinabove described in connection with the operation of these reversing heat exchangers.
The heat exchangers 35, 43 and 41 and the twostage fractionating column 31 may be of any conventional type. Two separate fractionating columns, suitably interconnected may be used in place of the two-stage column 31 shown. It will into and through heat ex- I be understood that the equipment throughout is heat insulated to minimize loss of cold.
One example of the operation of the process of this invention is described below. It will be understood this example is given for purposes of exemplification only and the invention is not limited thereto.
Air under pressure of about pounds gauge and temperature of about 100 F. is supplied through line it, valve I4 and line H to heat exchanger i0, flowing through path l2 in which it is cooled to a temperature of 134.5 F. The air then flows in indirect heat exchange relation with ethylene in the refrigeration system 22 and is cooled thereby to a temperature of -142 F., then passes through path 22 of the heat exchanger 2| leaving this path at a temperature of 275 F. which is close to the condensation point of the air at the pressure prevailing in heat ea:- changer 21. Substantially all moisture is removed in the form of frost in path l2 of heat exchanger l0 and all carbon dioxide is removed in solidified form in path 22 of heat exchanger 2|. The air then flows through the heat exchanger 35 in heat exchange relation with nitrogen enters high-pressure column 33 at a temperature of -278 F. and a pressure of 72 pounds.
C'rude oxygen at a temperature of 280 F. and a pressure of 72 pounds leaves the base of column 38, flows through heat exchanger 41 where its temperature is reduced to 289 F. and upon flow through the pressure reducing valve 49 is flashed, entering low-pressure column 39 at a temperature of 310 to -315 F. and a pressure of 5 pounds. Pure oxygen is withdrawn through line 51 at a temperature of 292.5 F. and a pressure of 5 pounds and flows through path 24, its temperature being increased to 146" F., the oxygen at this temperature entering path H of heat exchanger I0 and being withdrawn from this path at a temperature of F. and at a pressure of 1 pound.
Nitrogen at a temperatune of about 286.5 F. and a pressure of 72 pounds in amount equal to 12.5% by volume of the total nitrogen introduced into the process is withdrawn through line 5|. Of the nitrogen flowing through line SI, 10% passes through line 58 and path 60, its temperature being increased to 146 F. The remaining 90% of the nitrogen flows through valve 52 in line 5i and is mixed with the other 10% nitrogen, the temperature of the mixture being about -2'77 pander 53 is at a pressure of 5 pounds and a temperature of 315 F. The expanded nitrogen flows through line 53a and becomes mixed with nitrogen at a temperature of 315.5 F. and a pressure of 5 pounds flowing through line 54. The resultant nitrogen stream passes through exchanger 43 in indirect heat exchange relation with nitrogen employed as reflux in column 39, its temperature being thereby increased to 306" F. while the temperature of nitrogen flowing through line 42 (pressure of 72 pounds) and exchanger 43 is reduced to -300 F. This nitrogen by expansion through valve 44- has its pressure reduced to 5 pounds and its temperature to -315.5
F. The nitrogen product of rectification then flows through heat exchanger 41 where its temperature is increased to 293 F. The crude oxygen stream flowing through exchanger 41 is thereby cooled from a temperature of 280 F. to a temperautre of -289 F. The nitrogen then flows through exchanger 35 in heat exchange F. The nitrogen stream leaving the ex- 'tively, of heat exchangers i and 2|.
relation with the air, the nitrogen stream temperature being thereby increased to -2'79 F. at which temperature it enters the heat exchanger 2|. iiows therethrough and is thereby heated to -'146" F. At the colder end of the heat exchanger 2|, the nitrogen and the oxygen streams have a weighted average temperature of nearly --282 F. while at this point the air is at a temperature of 2'75 F. A temperature difference of about 1 F. is therefore maintained. It will be noted that at the point where the air enters and the oxygen and nitrogen leave the heat exchanger 2| the difference in temperature is approximately 4 F., the air being at a temperature of --l42" F.-
and the oxygen and nitrogen at 146 F.
From heat exchanger 2| the nitrogen fiows through heat exchanger H! where it is heated to 90 F. The nitrogen at this temperature and a pressure slightly above atmospheric, say 1 pound gauge, may be vented to the atmosphere thereby venting the lncondensibles, such as hydrogen, helium and neon, removed from the high-pressure stage of the rectification system.
The desired oxygen product is withdrawn through line 51 at a temperature of --292.5 F. and pressure or 5 pounds, flows through heat exchanger 2| where its temperature is increased to 146 F. and then through heat exchanger I! where its temperature is increased to 90 F. The oxygen leaves exchanger III at a pressure of 1 pound.
Upon reversal (as shown by dotted arrows and valve settings), which may take place every three minutes, the air flows through paths II' and 23, respectively, of heat exchangers l0 and 2i and nitrogen flows through paths l2 and 22, respec- The fiow is otherwise substantially the same and the temperature and pressure conditions remain the same. The nitrogen in its flow through path 22 of heat exchanger 2| removes by sublimation the carbon dioxide deposited in this path by the air during the preceding step, Likewise, the nitrogen in its flow through path |2 of heat exchanger "I removes from this path the frost deposited therein from the air during the preceding step. Thus in the continued operation upon each reversal the nitrogen effects removal of the carbon dioxide and frost deposited in the paths through which the air had passed during the preceding step of the process.
Operating in accordance with this invention it I oxygen and at the same time efiect continuous purging from the high-pressure stage of the rectification system of the incondensibieconstituents, such as hydrogen, helium and neon. Further, the purging is carried out so as to increase vthe efllciency of the rectification system in that the nitrogen stream containing the incondensibles is expanded and the refrigeration thus produced employed to cool the refiux oxygen and nitrogen introduced into the low-pressure stage and the air introduced into the high-pressure stage.
The expressions reversing the fiow of air and nitrogen and "reversal are used herein in the sense commonly employed in this art, namely, to mean the switching of the flow of two streams, for example, the air and the nitrogen streams, so that upon each "reversal" the air flows through the path through which had previously'fiowed the nitrogen, and the nitrogen fiows through the It will be noted this invention provides a process for producing oxygen of high purity without the use of chemical agents, which process may be operated continuously over a long period of time without shut-downs for the purpose of removing solid carbon dioxide or frost, which process is economical to operate, particularly in that the refrigeration which must be supplied to compensate for cold losses resulting from the difference in enthalpy between incoming air and the outgoing products of rectification and for heat leaks into the system is supplied at a point in the process where the temperatures are relatively high so that it can be supplied efllciently and economically, and which process effects continuous purging from the high-pressure stage of the rectification system of the incondensible constituents, such as hydrogen, helium and neon,
so as to increase the efficiency of the rectification system.
Since certain changes may be made in carrying out the above process without departing from the scope oi the invention, it is intended that all matter contained in the above description shall be interpreted as illustrative and not in a limiting sense.
What is claimed is:
1. A process for producing oxyygen by the liquefaction and rectification of air, which comprises passing a stream of air through a path in two zones in series, each of said zones containing at least three paths in heat exchange relation with each other, passing respectively streams of oxygen and nitrogen products of rectification through two other paths in said zones in heat exchange relation with the air passing therethrough, cooling at least one or said streams during its fiow between the first zone and the second zone, withdrawing the air from the second zone at a temperature such that substantially all carbon dioxide in said air has been removed from the air in its passage through its path in said second zone, maintaining the temperature difference between the temperature of the air leaving and the weighted average temperature of the nitrogen and oxygen entering said second zone so that it falls within the range of from about 5 to about 10 F., passing the air from said second zone to the high-pressure stage of a two-stage rectification system in indirect heat exchange relation with a rectification product from the low-pressure stage of said system, withdrawing a minor portion of the nitrogen from the high-pressure stage, expanding the nitrogen thus withdrawn to cool the same, imparting the cold thus produced to the rectification products entering the lowpressure stage, periodically reversing the flow of air and nitrogen through their respective paths in said zones, the air upon reversalflowing through the paths through which had previously fiowed the nitrogen and the nitrogen flowing through the paths through which had previously flowed the air, whereby upon each reversal the nitrogen substantially completely removes the carbon dioxide deposited in said second zone during the preceding step of the process.
2. A process for producing oxygen by the liquefaction and rectification of air, which comprises passing a stream of air at about '70 pounds to about pounds gauge and a temperature of about 70 to about F. through a path in two zones in series, each of said zones containing with each other, passing respectively streams of A process and for heat leaks into the system, withdrawing the air from the second zone at a temperature such that substantially all carbon dioxide in said air has been removed from the air in its passage through its path in said second zone, maintaining the temperature diflerence between the temperature of the air leaving and the weighted average temperature of the nitrogen and oxygen entering said second zone so that it falls within the range of from about to about F., passing the air from said second zone to the high-pressure stage of a two-stage rectification system in indirect heat exchange relation with a rectification product from the low-pressure stage of said system, withdrawing a minor portion of the nitrogen containing incondensible gases from the high-pressure stage, expanding the nitrogen thus withdrawn to cool the same, passing the expanded nitrogen in heat exchange relation with nitrogen and oxygen sup- .plied as reflux to the low-pressure stage and with air supplied to the high-pressure stage, and periodically reversing the flow of air and nitrogen through their respective paths in said zones, the air upon reversal flowing through the paths in the two zones through which had previously flowed the nitrogen and the nitrogen flowing through the paths through which had previously flowed the air, whereby upon each reversal the nitrogen substantially completely removes the carbon dioxide deposited in the second zneduring the preceding step of the process.
3. A process for producing oxygen by the liquefaction and rectification of air, which comprises passing a stream 01' air at about 70 pounds to about 85 pounds gauge and a temperature of about 70 to about 110 F. through a path in two zones in series, each of said zones containing three paths in heat exchange relation with each other, passing respectively streams of oxygen and nitrogen products of rectification through the two other paths in said zones in heat exchange relation with the air passing therethrough, cooling at least one of said streams during its flow from one zone to the other, the amount of cold thus introduced into the process being adequate to compensate for cold losses resulting from the difference in enthalpy between the air introduced into and the products of rectification withdrawn from the process and for heat leaks into the system, withdrawing the air from the second zone at a temperature such that substantially all carbon dioxide in said air has been removed from the air in its passage through its path in said second zone, maintaining the temperature difierence between the temperature 01 the air leaving and the weighted average temperature of the nitrogen and oxygen entering said second zone so that it falls within the range of from about 5 to about 10 F., passing the air from said zones to the high-pressure stage of a two-stage rectification system in indirect heat exchange relation with a rectification product from the low-pressure stage of said system, with- 12 drawing from the high-pressure stage about 1% to 15% of the total nitrogen introduced into the process, said nitrogen containing incondensible gases, heating approximately 10% or the nitrogen thus withdrawn, mixin the heated nitrogen with the remaining 90% of the nitrogen thus withdrawn thereby yielding a nitrogen stream having a temperature sufliciently high to avoid the formation of liquid nitrogen in the expander, expanding said nitrogen stream, passing the expanded nitrogen in heat exchange relation with oxygen and nitrogen supplied as reflux to the low-pressure stage and with the air supplied to the high-pressure stage, and periodically reversing the flow 01' air and nitrogen through their respective paths in said two zones, the air upon reversal fiowing through the paths in the two zones through which had previously flowed the nitrogen andthe nitrogen flowing through the paths in the said two zones through which had previously flowed the air, whereby upon each reversal the nitrogen substantially completely removes the carbon dioxide deposited in the second zone during the preceding step of the process.
4. A process for producing oxygen by the lique faction and rectification or air, which comprises passing air at about to about pounds gauge and a temperature of about 70 to about F. through a path in a zone containing three paths in heat exchange relation with each other, flowing oxygen and nitrogen products of rectification respectively through the other two paths in said zone in heat exchange relation with the air, the air thus being cooled to a temperature sufficient- 1y low to deposit out as frost substantially all the moisturein the air, refrigerating the air leaving the first zone to lower its temperature about 5 to 10 F., then further cooling the air by flowing it through a path in a second zone containing three paths, flowing oxygen and nitrogen prodnets of rectification respectively through the other two paths in said second zone in heat exchange relation with the air thereby cooling the air to a temperature sufliciently low to deposit out substantially all the carbon dioxide in the air, the differential between the temperature of the air and the weighted average temperature of the oxygen and nitrogen at the colder end of said second zone being within the range of about 5 to about 10 F., passing the air from said zones to the high-pressure stage of a two-stage rectification system in indirect heat exchange relation with a rectification product from the low-pressure stage of said system, withdrawing from 1% to 15% ot the total nitrogen introduced into the process from the high-pressure stage of the system, said nitrogen containing incondensible gases, expanding the stream of nitrogen thus withdrawn, mixing the expanded nitrogen with a stream of nitrogen withdrawn from the low-pressure stage and passing the resultant nitrogen in heat exchange relation with nitrogen and oxygen fed to the low-pressure stage and air fed to the high-pressure stage, and periodically reversing the flow of air and nitrogen through their respective paths in the said two zones, the air upon reversal flowing through the paths in the two zones through which had previously flowed the nitrogen and the nitrogen flowing through the paths in the said two zones through which had previously flowed the air, whereby upon each reversal the nitrogen substantially completely removes the carbon dioxide deposited in the se on m t on zone and the frost deand zone to a temperature sufiicient to remove substantially all carbon dioxide therefrom, the carbon dioxide thus removed being deposited in said second zone, cooling at least one of said streams during its flow from one zone to the other, the amount of cold thus introduced into the process being adequate to compensate for cold losses resulting from the difference in enthalpy between the air introduced into and the products of rectification withdrawn from the process and for heat leaks into the system, passing the air from said second zone to the high-pressure stage of a two-stage rectification system, withdrawing from said high-pressure stage nitrogen containing incondensible gases, heating by indirect heat exchange with the air passing through said second zone the nitrogen thus withdrawn to a temperature sufliciently high to avoid the formation of liquid nitrogen upon expansion of said nitrogen, expanding said nitrogen, passing the expanded nitrogen in heat exchange relation with oxygen and nitrogen supplied as reflux to the low-pressure stage of said rectification system, and periodically reversing the flow or air and nitrogen though their respective paths in said two zones, the air upon reversal flowing through the paths in the two zones through which had previously flowed the nitrogen and the nitrogen flowing through the paths in the said two zones through which had previously flowed the air, whereby upon each reversal the nitrogen substantially completely removes the carbon dioxide deposited in the second zone during the preceding step of the process.
6. A process for producing oxygen by the liquefaction and rectification of air, which comprises passing a stream of air at about '70 pounds to about 85 pounds gauge and a temperature of about 70 to about 110 F. through a path in two zones in series, each of said zones containing three paths in heat exchan e relation with each other, passing respectively streams of oxygen and nitrogen products of rectification through the two other paths in said zones in heat exchange relation with the air passing therethrough. thereby cooling the air leaving said second zone to a temperature sufllcient to remove substantially all carbon dioxide therefrom, the carbon dioxide thus removed being deposited in said second zone, cooling at least one of said streams during its flow from one zone to the other, the amount of cold thus introduced into the process being adequate to compensate for cold losses result-' ing from the difference in enthalpy between the air introduced into and the products of rectification withdrawn from the process and for heat leaks into the system, passing the air from said second zone to the high-pressure stage of a twostage rectification system in indirect heat exchange relation with a rectification product from the low-pressure stage of said system, withdrawing from the high-pressure stage from about 1% to about 15% of the total nitrogen introduced into the process, said nitrogen containing incondensible gases, heating a minor portion of the nitrogen thus withdrawn by indirect heat exchange withall o! the air passing to the highpressure stage of the rectification system, mixing the heated nitrogen with the remainder of the nitrogen thus withdrawn, thereby producing a nitrogen stream having a temperature sutflciently high to avoid the formation of liquid nitrogen upon expansion, expanding said nitrogen stream, passing the expanded nitrogen in heat exchange relation with oxygen and nitrogen supplied as reflux to the low-pressure stage and with the air supplied to the high-pressure stage, and periodically reversing the flow of air and nitrogen through their respective paths in said two zones, the air upon reversal flowing through the paths in the two zones through which had previously flowed the nitrogen and the nitrogen flowing through the paths in the said two zones through which had previously flowed the air, whereby upon each reversal the nitrogen substantially completely removes the carbon dioxide deposited in the second zone during thepreceding step or the process.
7. A process for producing oxygen by the liquefaction and rectification of air, which comprises passing a stream of rectification product through a path in a heat exchange zone, passing a stream of air through another path in said heat exchange zone to recover the cold content of the rectification product stream, thereby cooling the air to a temperature close to its condensation point at the pressure prevailing in said heat exchange zone and eflecting substantially complete removal of carbondioxide from the air in its passage through said heat exchange zone, passing the air from said heat exchange zone to the highpressure stage of a two-stage rectification system, withdrawing from said high-pressure stage a gaseous stream rich in nitrogen, warming the gaseous stream thus withdrawn to a temperature such that upon expansion to produce refrigeration said gaseous stream is'not liquefied by passing at least a portion of said gaseous stream through still another path in at least the colder end of said heat exchange zone in heat exchange relation with the streams of air and rectification product passing through said heat exchange zone, expanding the thus warmed gaseous stream to produce refrigeration without liquefaction of said. gaseous stream, maintaining the temperature difference between the temperature of the air leaving and the temperature of the rectification product entering said heat exchange zone so that it falls within the range of from about 5 to about 10 F., and periodically reversing the flow of air and rectification product through their respective paths in said heat exchange zone. the air upon reversal flowing through the path through which had previously flowed the rectification product and the rectification product flowing through the path through which had previously flowed the air, whereby upon each reversal the rectification product substantially completely removes the carbon dioxide deposited in said heat exchange zone during the preceding step of the process.
8. A process for producing oxygen by the liquefaction and rectification of air, which comprises passing a stream of nitrogen rectification product through a path in a heat exchange zone. passing a stream of air through another path. in said heat exchange zone to recover the cold content of the nitrogen rectification product stream, thereby cooling the air to a temperature close to its condensation point at the pressure prevailing in said heatexchange zone and eflecting substantially complete removal of carbon dioxide from the air in its passage through saidflheat exchange zone. passing the air from said heat exchange zone to the high-pressure stage of a two-stage rectification system, withdrawing from said high-pressure stage a gaseous stream rich in nitrogen, warming thegaseous stream thus withdrawn to a temperature such that upon expansion to produce refrigeration said gaseous stream is not liquefled by passing at least a portion of said gaseous stream through still another path in at least the colder end of said heat exchange zone in heat exchange relation with the streams of air and nitrogen rectiflcation product passing through said heat exchange zone, expanding the thus warmed gaseous stream to produce refrigeration without liquefaction of said gaseous stream, passing the expanded gaseous stream in heat exchange relation with oxygen and nitrogen streams supplied as reflux to the lowpressure stage of said rectiflcation system, maintaining the temperature difierence between the temperature of the air leaving and the temperature of the nitrogen rectification product entering said heat exchange zone so that it falls within the range of from about to about F., and periodically reversing the flow of air and nitrogen rectiflcation product through their respective paths in said heat exchange zone, the'air upon reversal flowing through the'path through which had previously flowed the nitrogen rectification product and the nitrogen rectificationproduct flowing through the path through which had previously flowed the air, whereby upon each reversal the nitrogen rectification product substantially completely removes the carbon dioxide deposited in said heat exchange zone during the preceding step of the process. I
9. A process for producing oxygen by the liquefaction and rectiflcation of air, which comprises passing a stream of air through a path in a heat exchange zone containing four paths in heat exchange relation with each other, passing respectively streams of oxygen and nitrogen products of rectiflcation through two of the other paths in said heat exchange zone in heat exchange relation with the air passing therethrough, withdrawing the air from said heat exchange zone at a temperature such that substantially all carbon dioxide in the air has been removed from the air in its passage through said heat exchange zone, passing the air from said heat exchange zone to the high-pressure stage of a two-stage rectiflcation system, withdrawing a portion of the nitrogen product from said highpressure stage and'warming said portion to a temperature such that upon expansion to produce refrigeration said portion is not liquefied by passing at least a part of said portion through still another of said four paths in at least the colder end of said heat exchange zone in heat exchange relation with the streams of air and oxygen and nitrogen rectification products passing through said heat exchange zone, expanding the thus warmed portion to produce refrigeration without liquefaction of said portion, maintaining the temperature difference between the temperature of the air leaving and the weighted average temperature of the oxygen and nitrogen rectiflcation products entering said heat exchange zone so that it falls within the range of from about 5 to about 10 F., and periodically reversing the flow of air and nitrogen rectiflcation product through their 16 respective paths in said heat exchange zone, the air upon reversal flowing through the path through which had previously flowed the nitrogen rectiflcation product and the nitrogen rectification product flowing through the path through which had previously flowed the air, whereby upon each reversal -the nitrogen rectiflcation product substantially completely removes the carbon dioxide deposited in said heat exchange zone during the preceding step of the process.
10. The process of claim 9 wherein the air is withdrawn from said heat exchange zone at a temperature of the order of 275 F.
11. A process for producing oxygen by the liquefaction and rectiflcation of air, which comprises passing a stream of air through a path in two heat exchange zones in series, each of said zones containing three paths in heat exchange relation with each other, passing respectively streams of oxygen and nitrogen products of rectiflcation through the two other paths in said zones countercurrent to the air passing therethrough, thereby cooling the air leaving the second zone to a temperature sufncient to remove substantially all carbon dioxide therefrom, the carbon dioxide thus removed being deposited in said second zone, passing the air from said second zone to the highpressure stage of a two-stage rectification system, withdrawing from said high-pressure stage nitrogen containing incondensible gases, warming the nitrogen thus withdrawn to a temperature such that upon expansion to produce refrigeration said nitrogen is not liquefied by passing at least a portion of said nitrogen through a fourth path in said second zone in heat exchange relation with the streams of air and oxygen and nitrogen rectiflcation products passing through said second zone, expanding the thus warmed nitrogen to produce refrigeration without liquefaction of said nitrogen, passing the expanded nitrogen in heat exchange relation with oxygen and nitrogen streams supplied as reflux to the low-pressure stage of said rectiflcation system, maintaining the temperature diflerence between the temperature of the air leaving and the weighted average temperature of the oxygen and nitrogen rectiflcation products entering said second zone so that it falls within the range of from about 5 to about 10 F., and periodically reversing the flow of air and nitrogen rectiflcation product through their respective paths in said zones, the air upon reversal flowing through the path in said zones through which had previously flowed the nitrogen rectiflcation product and the nitrogen rectification product flowing through the path in .said zones through which had previously flowed the air, whereby upon each reversal the'nitrogen rectiflcation product substantially completely removes the carbon dioxide deposited in said second zone during the preceding step of the process.
12. The process of claim 11 wherein the expanded nitrogen after passing in heat exchange relation with oIyyen and nitrogen streams supplied as reflux to the low-pressure stage of said rectiflcation system passes in heat exchange relation with the air passing from said second zone to the high-pressure stage of said rectification system.
13. A process for producing oxygen by the liquefaction and rectiflcation of air, which comsaid heat exchange zone to recover the cold content of the nitrogen rectiflcation product stream,
1 7 thereby cooling the air to a temperature close to its condensation point at the pressure prevailing in said heat exchange zone and eflecting substantially complete removal of carbon dioxide from the air in its passage through said heat exchange zone, passing the air from said heat exchange zone to the high-pressure stage of a two-stage rectification system, withdrawing from said highpressure stage a gaseous stream rich in nitrogen, warming the gaseous stream thus withdrawn to a temperature such that upon expansion to prodw ce refrigeration said gaseous stream is not liquefied by passing at least a portion of said gaseous stream through still another path in at least the colder end of said heat exchange zone in heat exchange relation with the'streams of air and nitrogen rectification product passing through said heat exchange zone, expanding the thus warmed gaseous stream to produce refrigeration without liquefaction of said gaseous stream, and periodically reversing the flow of air and nitrogen rectification product through their respective paths in said heat exchange zone, the air upon reversal flowing through the path through which had previously flowed the nitrogen rectification product and the nitrogen rectification product flowing through the path through which had previously flowed the air, whereby upon each reversal the nitrogen rectification product substantially completely removes the carbon dioxide deposited in said heat exchange zone during the preceding step of the process.
FRANK J. JENNY.
EDWARD G. SCHEIBEL REFERENCES CITED The following references are of record in the file of this patent or the original patent:
UNITED STATES PATENTS
US23463D Process of producing oxygen Expired USRE23463E (en)

Publications (1)

Publication Number Publication Date
USRE23463E true USRE23463E (en) 1952-02-26

Family

ID=2090800

Family Applications (1)

Application Number Title Priority Date Filing Date
US23463D Expired USRE23463E (en) Process of producing oxygen

Country Status (1)

Country Link
US (1) USRE23463E (en)

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2836040A (en) * 1954-08-19 1958-05-27 Air Prod Inc Method for the fractionation of air
US2964914A (en) * 1955-05-12 1960-12-20 British Oxygen Co Ltd Separation of air
US3535886A (en) * 1967-07-05 1970-10-27 Mc Donnell Douglas Corp Production of high purity nitrogen from air by distillation with depressurized,work expanded and cooled oxygen-rich bottoms used in indirect heat exchange for the distillation

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2836040A (en) * 1954-08-19 1958-05-27 Air Prod Inc Method for the fractionation of air
US2964914A (en) * 1955-05-12 1960-12-20 British Oxygen Co Ltd Separation of air
US3535886A (en) * 1967-07-05 1970-10-27 Mc Donnell Douglas Corp Production of high purity nitrogen from air by distillation with depressurized,work expanded and cooled oxygen-rich bottoms used in indirect heat exchange for the distillation

Similar Documents

Publication Publication Date Title
US2504051A (en) Process for producing oxygen by liquefaction of air in which a portion of the air is expanded to supply refrigeration without loss of oxygen content of the air
US2579498A (en) Process for producing oxygen
US2513306A (en) Process for producing oxygen by the liquefaction and rectification of air
US2534478A (en) Gas purifying method and apparatus
US3608323A (en) Natural gas liquefaction process
US3143406A (en) System for conducting heat exchange operations in a gas separation apparatus incorporating periodically reversible regenerators
US1989190A (en) Apparatus for separating low boiling gas mixtures
US2586811A (en) Process for producing oxygen
US2673456A (en) Separation of low boiling gas mixtures
US2648205A (en) Rectification of mixed gases
US2509034A (en) Method and apparatus for liquefying gaseous fluids
US2537046A (en) Process for producing oxygen by the liquefaction and rectification of air
US2433604A (en) Separation of the constituents of gaseous mixtures
US2582068A (en) Method and apparatus for separating gases
US2214790A (en) Process and apparatus for separating gases
US4308043A (en) Production of oxygen by air separation
US3210947A (en) Process for purifying gaseous streams by rectification
US2552560A (en) Process of producing oxygen
US3107992A (en) Low temperature gas decomposition plant
US2556850A (en) Oxygen separation
USRE23463E (en) Process of producing oxygen
US2643527A (en) Precooling air in oxygen production
US3721098A (en) Cooling by mixing gaseous streams
US2709348A (en) Process of and apparatus for separating gas mixtures
US3257814A (en) Process for the manufacture of oxygen-enriched air