DISTILLATIVE SEPARATION OF METHANE AND CARBON DIOXIDE

Abstract: Improvement in a Ryan/Holmes separation of methane from carbon dioxide wherein the upper portion of a distillation column is operated at temperatures above the triple point of carbon dioxide, i.e., -70<o>F, while still effectuating a separation of methane from carbon dioxide. This is achieved by increasing the amount of non-polar liquid agent added to the condenser of the column to an amount sufficient to maintain the condenser and all portions of the column at such temperatures.

Description: DISTI LATIVE SEPARATION OF METHANE AND CARBON DIOXIDE Description Technical Field This invention is in the field of distillation. 5 Background Art • ; There are many situations in which it is desirable to separate methane from carbon dioxide. For example, gas streams obtained from natural gas wells often con¬ tain relatively high amounts of carbon dioxide which 0 lowers the heating value of the gas and are highly corro¬ sive. In such situations, carbon dioxide must be removed from the gas stream in order to. meet the carbon dioxide specification for saleable gas products. Additionally, carbon dioxide usually must be separated from gas rnix- tures caused by injecting carbon dioxide-containing gases into oil wells for enhanced oil recovery. Generally, the processes developed for separating methane and carbon dioxide can be classified into cer¬ tain broad categories. These include carbon dioxide adsorption by solids, carbon dioxide absorption by chemi¬ cal solvents, carbon dioxide absorption by physical solvents and distillative separations at relatively low temperatures. Distillative separations offer many advantages and are possible because the relative vola- tility of methane to carbon dioxide is reasonably high. However, the behavior of me ' thane/carbon dioxide systems has often prevented such distillative separations from becoming commercially practical for separations reguiring sub¬ stantially complete carbon dioxide separation from high-carbon dioxide content gases. This is because solid carbon dioxide coexists with a vapor and liquid mixture of methane and carbon dioxide at certain compositions, * temperatures and pressures encountered in distillative separations. At these conditions, carbon dioxide freezes out of solution and would potentially plug up a distilla¬ tion column as well as other equipment thereby making the process inoperative. On the other hand, at higher pressures, where carbon dioxide does not freeze out, methane-rich mixtures become supercritical fluids not - subject to further purification of methane by distilla¬ tion. Thus, raising the pressure in a column above that where carbon dioxide freeze out occurs is not usually a viable alternative to achieving further methane sepa¬ ration. In a copending application, Serial No. 94,226, filed August 14, 1979 in the names of ' Arthur S. Holmes and James M. Ryan, a process which has become known as the "Ryan/Holmes" process is described. The Ryan/Holmes process can be employed to separate a feed gas mixture containing methane and carbon dioxide in a distillation column into a methane overhead product substantially free of carbon dioxide and a carbon dioxide bottoms product substantially free of methane. Unlike many other prior distillative separations, the Ryan/Holmes process in¬ volves the operation of the distillation column at temperatures, compositions and pressures which produce a solids potential zone for carbon dioxide within the tower. The term "solids potential zone" is employed with the Ryan/Holmes process because, although condi¬ tions in the tower are such that carbon dioxide solids would normally occur, the Ryan/Holmes process prevents actual solids formation from occurring. This is achieved by introducing into the upper portion of the distillation column an agent for preventing acid gas solids. The agent can be an external additive, or in the alternative, can be one or more recycled components from the bottoms product taken from the distillation column. A more- detailed description of the use of the Ryan/Holmes process for separating methane from carbon dioxide, as well as the prior art cryogenic distillative separa¬ tions of methane and carbon dioxide, can be found in 5 Serial No. 94,226, the teachings of which are hereby _ incorporated by reference. In a typical separation of methane from carbon dioxide employing the Ryan/Holmes process, the tempera¬ ture levels in the overhead condenser of the distillation 0 column have heretofore run in the order of about -125°F. Such low temperatures are typically achieved by employing a cascaded ethylene-propane refrigeration system. Be¬ cause of the low temperatures at thj≥ overhead, and operat¬ ing column pressures which are typically 500 psia or higher, the distillation column and associated equipment was typically fabricated from stainless steel. Disclosure of the Invention- This invention concerns an improved low temperature method and apparatus for the distillative separation of methane and carbon dioxide. In particular, this invention relates to an improvement in a Ryan/Holmes process for separating methane from carbon dioxide. '• It has now been unexpectedly discovered by Appli¬ cant that a Ryan/Holmes process for separating methane and carbon dioxide can be carried out employing much warmer temperatures in the upper portion of the distilla¬ tion column than heretofore believed possible. In this improved distillative process, the upper portion of the distillation column in a Ryan/Holmes process is operated above the triple point of carbon dioxide, i.e., above about -70°F. As long as the temperature is maintained above the triple point of carbon dioxide, formation of carbon dioxide solids does not occur. In this improved distillative process, a feed stream containing methane and carbon dioxide is introduced into a distillation column. Prior to introduction, the feed stream may be cooled but preferably should not be cooled below the triple point of carbon dioxide to avoid solids formation. The distillation column is provided with sufficient heat at its bottom to produce a bottoms prod¬ uct enriched in carbon dioxide. Overhead, a stream en¬ riched in methane is withdrawn and at least a portion of the withdrawn overhead stream is condensed. A condensed portion of overhead stream serves as reflux to the tower so that the condensed portion must be sufficient to pro¬ vide a column overhead enriched in methane. In a manner superficially similar to a typical Ryan/Holmes process for separating methane from carbon dioxide, a non-polar agent miscible with methane is intro¬ duced into the condenser of the distillation column. However, in the improved separation described herein, the agent must be maintained at a temperature above -the triple point of carbon dioxide. There must also be sufficient quantity of agent introduced into the upper portion of the column to maintain the temperature at all locations in the upper portion of the column above the triple point of carbon dioxide. Typically, this means that much larger amounts of agent are introduced into the condenser than have heretofore been suggested for use in the Ryan/Holmes separation of methane from carbon dioxide. That portion of withdrawn overhead stream not e - ployed as reflux is withdrawn as overhead product en¬ riched in methane. In summary, it can be seen that in this improve¬ ment of a Ryan/Holmes distillative separation of methane from carbon dioxide, the column is operated much warmer than had heretofore been suggested. This is achieved by introducing a sufficient quantity of non-polar agent to maintain temperatures in the upper portion of the column above the triple point of carbon dioxide. Preferably, " -, the feed is also introduced into the column at a tem¬ perature above the triple point of carbon dioxide. Thus ' , the improved Ryan/Holmes process for separat¬ ing methane from carbon dioxide described herein offers advantages over the typical Ryan/Holmes separation pre¬ viously proposed. Among the significant advantages is the elimination of a requirement for a refrigeration system capable of chilling the upper portions of a dis¬ tillation column to temperatures significantly below the triple point of carbon dioxide. It has been found, for example, that a propane refrigeration system can be employed instead of the more complex and costly cas- caded ethylene/propane refrigeration systems typically previously employed. The use of warmer temperatures in the column also • means that the column and associated items can often be made from carbon steel rather than from stainless steel. It has also been found that higher operating pres¬ sures can be employed with this improved Ryan/Holmes process compared to previous Ryan/Holmes separations of methane from carbon dioxide. Further, the process can be readily adapted to pro- duce pipeline quality gas (<2% CO-) or LNG quality gas ( • <50 ppm CO-) and the process can handle low or high carbon dioxide content feeds. Of,? It is still yet an additional advantage that the dehydration requirement of the feed gas is not as severe as with the lower temperature Ryan/Holmes process. The water dew point can match the lowest refrigerant tem- perature (e.g., -70°F or -40°F or warmer). Thus, glycol dehydration can often be employed instead of molecular sieve bed systems. Also, the ability to control the column overhead temperature at different levels, independently of the CO- content, enables the designer to control the hydro¬ carbon dew point of the product methane stream. Features of the process shared with the lower tem¬ perature Ryan/Holmes process include: capability of reducing the H-S content of feed and total sulfur to below 1/4 grain/100 SCF and the capability for complete extraction of the ethane from the feed. Finally, carbonyl sulfide and mercaptans can be removed from feed gases in the course of removing carbon dioxide. Brief Description of the Drawing The Figure is a schematic flow diagram illustrating the improved Ryan/Holmes distillative process for sepa¬ rating methane from carbon dioxide described herein. Best Mode of Carrying Out the Invention This invention will now be described with more spe- cific detail with regard to the Figure. In the Figure, it can " be seen that dry feed gas 10, containing a mixture of methane and carbon dioxide, and usually other components such as nitrogen and higher alkanes, enters in inlet feed line 12. The feed gas is cooled in heat exchanger 14 which receives refrigera¬ tion from refrigeration source 16. Feed gas exiting from exchanger 14 should preferably have a temperature above the triple point of carbon dioxide since the col¬ umn is run at such temperatures. Thereafter, cooled feed is introduced into one or 5 more of the feed points in distillation column 18. Dis¬ tillation column 18 contains a number of vapor-liquid contact devices, such as trays or packing, with the exact number of contact stages depending upon the required operating conditions, of course. Overhead is withdrawn in overhead line 20 and passed to condenser 22. Methane- enriched product is withdrawn in line 24. Condenser 22 receives refrigeration from refrigera¬ tion source 26 sufficient to condense at least a portion of overhead to provide reflux in line 28 to tower 18. Since the upper portion of tower 18 is maintained above the triple point of carbon dioxide in this separation, refrigeration source 26 can be a propane refrigeration system rather than a cascaded ethylene/propane system often employed if temperatures of about -130° to -140°F were required. Other common refrigeration systems capable of condensing a portion of the overhead stream withdrawn in line 20, such as Freon®, ammonia, propylene , carbon dioxide, etc., might also be employed. The re¬ quirement is, of course, to maintain the temperature at a temperature no lower than the triple point of carbon dioxide, which is about -70°F. Preferably, the tempera¬ ture is maintained even higher, such as above about -40°F. Bottoms exits from column 18 through line 30 and part of the bottoms is recycled to column 18 via line 32 which passes through reboiler heat exchanger 34 supplied with heat energy from heat source 36. This provides vaporization heat to the bottom of column 18. - - ^EX The balance of the bottoms passes through line 38 to further separation equipment 40 for separating out other fractions, such as an ethane plus fraction sepa¬ rated and collected through line 42. A carbon dioxide fraction is extracted through line 44. It is sometimes possible to separate non-polar liquid agent from bottoms, such as natural gas liquids. (NGL) , which is shown as recycled agent. The recycled agent exits from the separation equipment 40 in line 46 and valve 48 regulates the flow of such recycled agent through heat exchanger 50 cooled by refrigeration source 52, back to condenser 22. Refrigeration source 52 need only be sufficient to cool the agent to a point above the triple point of carbon dioxide. Recycled, cooled agent exiting from heat exchanger 50 flows in line 53 into condenser 22. It may also be added to column 18 at additional points, if desired. In another alternative embodiment, a non-polar agent can be externally added. For example, agent can be added externally via line 54 into heat exchanger 50, in which case the flow is controlled by valve 56. Typical agents which can be employed include ethane, propane, butane, pentane and mixtures thereof. In general, non-polar materials which are miscible with methane, such as C--C,- alkanes, are preferred agents be¬ cause they are typically present in feed gases, are easy to separate and recycle, and seem to have a very beneficial effect on raising the operating temperature in the upper portions of the distillation column. Cer- tain natural gas liquids (NGL) contain such alkanes and can often be separated from the bottoms product in conventional separation equipment. Thus, these NGL or components thereof can be conveniently recycled. It is also clear that agents need not be pure materials and may comprise, mixtures of components. The amount of non-polar agent added will depend 5 upon factors such as the composition of the feed, operating pressure, throughput of the column, desired purity of overhead methane, etc. In general, larger -• amounts of agent are employed than had heretofore been suggested for use in Ryan/Holmes separations of methane 0 from carbon dioxide. More specifically, it has been found that an amount of non-polar agent of more than one mole per mole of methane in the feed stream can be em¬ ployed, and more preferably from abo t 2 to about 10 moles per mole of methane in the feed. Since the column is operated under conditions which do not approach conditions under which carbon dioxide would freeze, a very wide range of carbon dioxide-content feed gases can be employed. Feeds can contain virtually any amount of carbon dioxide and the only limitation on use of this process to reduce the carbon dioxide is one of economic practicality. It is, of course, a particularly advantageous process for feeds containing high amounts (e.g.,_>50%) of carbon dioxide. On the other hand, the process can be employed in the production of pipeline quality gas (i.e., <Z 2-3% CO-) and even LNG quality gas (i.e., <:50 ppm CO_) . The pressure in the distillation column is maintained below the critical pressure' of any mixture therein so that a distillative separation can be performed. How- ever, the addition of large amounts of non-polar agent typically raises the critical pressure of the system, which means that a relatively wide range of pressures are suitable. For example, it has been typical with a -fuREX, Ryan/Holmes separation of methane from carbon dioxide to employ pressures in the range of above 660-700 psig, but operating the column at warmer temperatures as de¬ scribed herein often means that pressures of well over 1000 psig can be employed. In order to further describe this invention, a number of computer simulations will now be described. .. These were run using a plate-to-plate column calculation program to simulate conditions within the distillation column for certain given or desired operating conditions. SM The program employed was the PROCESS Simulation Pro¬ gram from Simulation Sciences, Inc., Fullerton, Cali¬ fornia, version 1080. Vapor-liquid-.equilibria and thermodynamic data for methane/carbon dioxide systems were calculated based upon the Peng-Robinson equation of state. Product specifications were established as 0.5% methane in the bottoms product, 2% carbon dioxide in the overhead, and less than 3.8 ppm H-S (1/4 grain/ 100 SCF) in the overhead. The feed and additive employed are presented below in Table I: - JRE _OMPI Table I Composition, Mole Percent Component Feed Gas Agent Hydrogen Sulfide 0.12 0 Nitrogen 0.07 v 0 Carbon Dioxide 87.09 0 Methane 5.03 0 Ethane 2.61 0 Propane 2.27 0.5 Isobutane 0.39 2.90 Normal Butane 1.13 16.39 Isopentane 0.38 ' 14.95 Normal Pentane 0.48 22.44 Normal Hexane 0.32 28.21 Normal Heptane 0.11 14.61 100.00 100.00 This NGL mix employed as non-polar agent miscible with methane was separated out from the bottoms product of the demethanizer column in subsequent columns. The results of the computer simulations are pre¬ sented in Table II. -ξ J3.E_^ OI ΈI Table II Column Pressure , psia 500 500 500 500 Feed Rate , Ib.moles/hr 7996 7996 7996 - 7996 Additive Rate , Ib .moles/hhrr 750 900 1250 1400 Feed & Additive Temp , °F -35 -35 -35 -35 Ratio Additive/Methane in Feed, moles /mole 1.9 2.5 3.2 .3.53 Number of Theoretical Traayyss 17 17 17 17 Feed Tray 11 11 11 11 Overhead Product Temperature,°F -83.3 -70.0 -44.9 -36.5 Condenser Duty,mmBtu/hr 3.08 -___. 2.78 2.03 1.68 Rate, lb.moles/hr 367.4 366.9 365.9 365.5 Composition, mole % H 2 S 1.2 ppm 1.7 ppm 2.8 ppm 3.3 ppm 1.52 1.52 1.53 1.53 N 2 co 2 2.00 2.00 2.00 2.00 CH 4 96.35 96.28 96.05 95.95 C 2 H 6 16 ppm 21 ppm 33 ppm 38 ppm C 3 Hg 0.02 0.03 0.05 0.05 iC 4 H 10 0.02 0.03- 0.06 0.07 nC 4 H 10 0.07 0.11 0.23 0.28 iC 5 H 12 0.01 0.02 0.04 0.05 nC 5 H 12 0.01 0.02 0.04 0.05 nC 5 H 14 20 ppm 34 ppm 84 ppm 0.01 nC 6 H 16 6 ppm 10 ppm 28 ppm 39 ppm Bottoms Product Temper ture, °F 37.5 38.3 40.1 40.8 Reboiler Duty, mmBtu/hr 19.63 20.13 21.11 21.48 Methane Content, Mole Percent 0.5 0.5 0.5 0.5 In the first column of Table I, it can be seen that 750 moles per hour of agent was insufficient to maintain the upper portion of the tower above the triple point of carbon dioxide. Note, the overhead temperature 5 of -83°F. Hence, a solids potential zone formed and had an approach to freezing of approximately 50°F. This is, then, an example of a typical Ryan/Holmes process for separating methane from carbon dioxide with the column ' -- being run at colder temperatures. Subsequent runs, where the amount of agent was increased to 900 mph or more of agent, brought the tem¬ perature in the overhead portion of the column up to the triple point or warmer. The increase in temperature is due to increased amounts of butane in he condenser. Thus, the " increased amounts of agent raise the column temperature to the range where carbon dioxide solids formation is not a concern. Surprisingly, very effective separations of methane from carbon dioxide can be achieved at these warmer temperatures with the use of relatively large amounts of agent compared to amounts previously employed in Ryan/Holmes separations. The improved. Ryan/Holmes process can also be used to reduce the CO- content of a methane-rich stream to an adequate level for further lower temperature process- ing, such as the liquefaction of natural gas. To illus¬ trate this, the results of computer simulations are pre¬ sented in Tables III and IV illustrating-how the CO content of the methane is reduced to 50 ppm, while the condenser temperature is controlled above the CO- triple point. Note also the H-S content of the methane stream is below 3.8 ppm and the ethane extraction from the feed is 100%. ' ' Table III Composition, Mole Percent Feed Gas Agent H 2 S 0 .40 0 .0015 N 2 0 .25 0 co 2 59 .29 0 CH„ 17. .19 0 8, .88 0 C 2 H 6 7, .47 0. .9985 C 3 H 8 1. .21 20. ,00 iC 4 H 10 3, .31--- 40. ,00 nC 4 H 10 0-. .86 15. 00 iC 5 H 12 nC 5 H 12 0, ,91 15. 00 nC 6 H 14 0. 21 7. 00 0. 02 2. 00 nC 7 H 16 100. 00 100.00 Table IV Column Pressure, psia 500 500 Feed Rate, lb. moles/hr 1211 1211 Additive Rate, lb. moles/hr 650 900 Feed and Additive Temp, °F -35 -35 Ratio Additive/Methane in Feed, moles/mole 3.1 4.3 Number of Theoretical Trays 17 17 Overhead Product Temperature, °F -73.5 -61.4 Condenser Duty, mmBtu/hr l_v.80 1.94 Rate, lb. moles/hr 196.9 197.2 Composition, Mole % H H 2 -S 1.6 ppm 2.1 ppm 1.52 1.52 '!2 co 2 50 ppm 50 ppm CH 4 98.09 97.94 C 2 H 6 0 0 C 3 H 8 0.02 0.03 iC 4 H 10 0.15 0.21 nC 4 H 10 0.17 0.25 iC 5 H 12 0.02 0.03 nC 5 H 12 0.01 0.02 nC 6 H 14 13 ppm 21 ppm nC 7 H 16 1 ppm 1 ppm Bottoms Product Temperature, °F 69.8 83.7 Reboiler Duty 6.76 8.57 Methane Content, lb. moles/hr 15 15 Industrial Applicability This invention is .useful in the distillative separation of methane from carbon dioxide. Equivalents Those skilled in the art will also recognize, or be able to determine using no more than routine experi^ mentation, equivalents to the specific embodiments de¬ scribed herein.

Claims: Claims 1. A method of distillatively separating a feed stream containing methane and carbon dioxide into-an overhead product enriched in methane and a bottoms product enriched in carbon dioxide, comprising: introducing said feed stream into a distillation column; providing sufficient heat to the bottom of said distillation column to provide a bottoms product enriched in carbon dioxide with respect to the feed and based upon a binary of methane and carbon dioxide; withdrawing an overhead stream from the top of said column; condensing at least a portion of said overhead stream for reflux in an overhead condenser at a temperature above the triple point of carbon dioxide and directing said condensed portion of overhead back to said column as reflux, said condensed portion being sufficient to provide a column overhead enriched in methane; introducing a non-polar agent miscible with methane into the condenser of said distillation column in a quantity sufficient to maintain the temperature in the condenser and at all locations within the distillation column above the triple point of carbon dioxide; withdrawing that portion of overhead not employed as reflux as overhead product enriched in methane; and, withdrawing bottoms enriched in carbon dioxide. A method of Claim 1 wherein said non-polar agent is introduced into the condenser of said distillation column in an amount of from about 2 to about 10 moles of agent per mole of methane in the feed stream. A method of Claim 2 wherei "said non-polar agent is a liquid. A method of Claim 3 wherein said agent comprises natural gas liquids. A method of Claim 3 wherein said agent comprises ethane, propane, butane, pentane or mixtures thereof. A method of Claim 3 wherein said agent comprises butane. A method of Claims 1, 3, 4, 5 or 6 wherein said agent is separated from the bottoms product from said distillation column and recycled to said column. A method of Claim 1 wherein the temperature in said condenser is maintained above about -40°F. 9. A method of Claim 7 wherein the temperature in said condenser is maintained above about -40°F. 10. A method of Claim 3 wherein said feed stream contains more than 50 mole percent carbon dioxide. 11. A method of Claim 3 wherein said feed stream is cooled prior to introduction to the distillation column to a temperature no lower than the triple point of carbon dioxide. 12. A method of Claim 3 wherein said distillation column is operated at a pressure above 1000 psig. 13. A method of Claim 3 wherein said overhead stream contains less than 2 mole percent carbon dioxide. 14. . A method of Claim 3 wherein said overhead stream contains less than 50 ppm carbon dioxide. 15. A method of Claim 3 wherein said feed stream is dehydrated employing glycol dehydration. 16. In a distillative separation wherein a feed stream containing methane and carbon dioxide is introduced into a distillation column and separated therein into an overhead product enriched in methane and a bottoms product OMPI enriched in carbon dioxide with respect to methane and carbon dioxide in said feed stream including withdrawing an overhead stream, condensing at least a portion thereof in a condenser, and directing said condensed portion back to the upper portion of said distillation column as reflux and wherein a non-polar liquid agent miscible with methane is also introduced into the condenser of said distillation column: The improvement wherein the tem¬ perature is maintained in said condenser and at all points in said column above about -70°F by providing a sufficient quantity of said agent in said condenser. 17. An improvement of Claim 16 wherein said agent comprises natural gas liquids. 18. An improvement of Claim 16 wherein said agent comprises ethane, propane, butane, petane or mixtures thereof. 19. A method of Claim 16 wherein said agent comprises butane. 20. A method of Claims 16, 17, 18, or 19 wherein said agent is introduced into the condenser of said column in an amount of from about 2 to about 10 moles per mole of methane in said feed stream. 21. An improvement of Claim 20 wherein said agent is separated from bottoms product from said distillation column and recycled back to the upper portion of said column. 22. In a method of separating, in a distillation column having a condenser to provide reflux to said column, methane from a feed stream comprising methane and carbon dioxide which method comprises: introducing the feed stream into a distillation column; introducing an agent into the condenser of said column, which agent is miscible with the methane and in an amount sufficient to permit the distil¬ lative separation of methane from the carbon dioxide; withdrawing a methane-enriched overhead stream; and, withdrawing a carbon dioxide enriched bottom stream which contains the agent. The improvement which comprises: maintaining, by the addition of sufficient quantity of the said agent, the- upper portion of the distillation column above the triple point of the carbon dioxide. 23. A method of distillatively separating a feed gas containing methane and carbon dioxide, comprising: EA OMPI a. drying said feed gas; b. cooling said dried feed gas to a temperature no lower than the triple point of carbon dioxide; c. introducing said dried, cooled feed gas into a distillation column; d. withdrawing a bottoms stream from said distillation column; e. heating a portion of said withdrawn bottoms stream and returning said heated portion to said distillation column to provide sufficient heat to provide a bottoms product enriched in carbon dioxide with respect to the feed and based upon a binary of methane and carbon dioxide; f. withdrawing an overhead stream from the top of said column, said overhead stream being enriched in methane; g. passing said overhead stream enriched in methane to an overhead condenser sup¬ plied with a source of refrigeration sufficient to condense a portion of said overhead stream, said condensed portion being returned to said column as reflux; h. passing the balance of withdrawn bottoms product to separation equipment for separating out a carbon dioxide frac¬ tion, an ethane-plus fraction, and agent for recycling to said distillation column; L. passing said agent for recyling through a cooler provided with refrigeration sufficient to cool said recycled agent to a temperature no lower than the triple point of carbon dioxide; j. introducing said cooled, recycled agent into the overhead condenser in suffi¬ cient quantity to maintain the tempera¬ ture in the condenser and at all loca¬ tions within the distillation column above the triple point of carbon diox- ide; and, k. withdrawing that portion of overhead not employed as reflux as overhead product enriched in methane.

Inventors: O'BRIEN JOHN VINCENT, O'BRIEN, JOHN, VINCENT
Applicants: KOCH PROCESS SYSTEMS INC, KOCH PROCESS SYSTEMS, INC.
Application year: 1982
Main classification: F25J3
IPC codes: C01B31, C07C1, C07C7, C07C9, C07C67, F25J3