AU728970B2 - Catalytic removal of acetylene during separation of air - Google Patents

Catalytic removal of acetylene during separation of air Download PDF

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Publication number
AU728970B2
AU728970B2 AU50403/98A AU5040398A AU728970B2 AU 728970 B2 AU728970 B2 AU 728970B2 AU 50403/98 A AU50403/98 A AU 50403/98A AU 5040398 A AU5040398 A AU 5040398A AU 728970 B2 AU728970 B2 AU 728970B2
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Australia
Prior art keywords
air
acetylene
catalyst
accordance
heat exchanger
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Ceased
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AU50403/98A
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AU5040398A (en
Inventor
Peter Matthias Fritz
Peter Haussinger
Eberhard Lassmann
Matthias Meilinger
Wilhelm Rohde
Nicole Schodel
Ulrike Wenning
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Linde GmbH
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Linde GmbH
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/86—Catalytic processes
    • B01D53/8668—Removing organic compounds not provided for in B01D53/8603 - B01D53/8665
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/002—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by condensation
    • 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
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04163—Hot end purification of the feed air
    • 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
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
    • F25J3/04303—Lachmann expansion, i.e. expanded into oxygen producing or low pressure column
    • 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
    • F25J3/04406—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 using a dual pressure main column system
    • F25J3/04412—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 using a dual pressure main column system in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
    • 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
    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
    • F25J3/04854—Safety aspects of operation
    • 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
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/24—Processes or apparatus using other separation and/or other processing means using regenerators, cold accumulators or reversible heat exchangers
    • 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
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/82—Processes or apparatus using other separation and/or other processing means using a reactor with combustion or catalytic reaction
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
    • Y02C20/00—Capture or disposal of greenhouse gases
    • Y02C20/40—Capture or disposal of greenhouse gases of CO2

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • General Chemical & Material Sciences (AREA)
  • Analytical Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Environmental & Geological Engineering (AREA)
  • Health & Medical Sciences (AREA)
  • Biomedical Technology (AREA)
  • Separation By Low-Temperature Treatments (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Catalysts (AREA)
  • Exhaust Gas Treatment By Means Of Catalyst (AREA)

Description

AUSTRALIA
PATENTS ACT 1990 COMPLETE SPECIFICATION NAME OF APPLICANT(S): Linde Aktiengesellschaft ADDRESS FOR SERVICE: DAVIES COLLISON CAVE Patent Attorneys 1 Little Collins Street, Melbourne, 3000.
INVENTION TITLE: Catalytic removal of acetylene during separation of air The following statement is a full description of this invention, including the best method of performing it known to me/us:- The invention relates to a method for low temperature air separation, whereby the air is compressed, cooled in at least one switch-over heat exchanger and subsequently fractionated in at least one distillation column.
For the removal of water vapour and carbon dioxide from the air, air separation plants •are operated on the one hand by switch-over heat exchangers, regenerators or Revex, and on the other hand by molecular sieve adsorbers. In plants where the sum of the produced oxygen and nitrogen quantities is less than 50 of the air quantity charged, the use of switch-over heat exchangers has the advantage that the undesired components, water vapour and carbon dioxide, are removed from the heat exchanger .during each switch-over process between charged warm air and cold residue gas.
Such plants however have the great disadvantage that hydrocarbons, in particular acetylene, are removed from the air only incompletely and are able to concentrate in the liquid oxygen. If the acetylene concentration exceeds its solubility limit, it recrystallises and forms a highly flammable, explosive mixture. In view of its poor solubility in oxygen, the acetylene concentration should therefore not exceed 1 ppm.
In plants with switch-over heat exchangers, so-called gas phase adsorbers are used in combination with rotary adsorbers or pressure column adsorbers in combination with rotary adsorbers which, at low temperatures, largely adsorb acetylene. These adsorbers are arranged in pairs, as they have to be switched over for regeneration after a certain operating period.
The expenditure involved in the operation of such adsorbers is considerable, so that after the advent of the molecular sieves, the adsorbers were built into the "warm section" of the air separation plant, i.e. upstream of the heat exchangers. These molecular sieves do not only adsorb acetylene very effectively, but also water vapour and carbon dioxide. It is therefore no longer necessary to use switch-over heat exchangers for low-temperature liquids.
The adsorption efficiency of molecular sieves is strongly dependent on temperature.
For reasons of economy, they are therefore operated at temperatures between 5 0 C and 0 C, depending on the ambient temperature, so that, as a rule, precooling of the air which is leaving the compressor and which is to be fractionated is necessary. A disadvantage is also presented by the pressure loss at the molecular sieve, which increases the energy consumption of the plant, in particular, during the heating period .of the regeneration gas. Moreover, molecular sieves are considerably larger than the 0: "adsorbers of a plant with switch-over heat exchangers, resulting in higher investment costs.
The main source of danger in cryogenic air separation plants is acetylene and its poor solubility in oxygen. The other hydrocarbons, such as propane and ethylene, which even in molecular sieve adsorbers are only retained in a limited manner, as well as methane and ethane, which in molecular sieve adsorbers are hardly retained at all, possess good solubility in oxygen. A concentration of these hydrocarbons-beyond an admissible extent is usually avoided by extraction of a certain quantity of liquid from the main condenser, the main site of concentration, and its subsequent evaporation.
The article "safe design and operation of LOW TEMPERATURE AIR SEPARATION PLANTS", Chem. Eng. Prog. Vol. No. 52, 11, pp. 441-447 (1956), suggests that air separation plants located in regions where the air is severely contaminated with acetylene (10 to 30 ppm) remove the acetylene catalytically. To achieve this, the hot air, after the compressor, is passed through a special catalyst where the acetylene content is reduced to below 1 ppm. A greater reduction of the acetylene concentration to just a few ppb is however not possible. Moreover, the catalyst only works reliably at sufficiently high temperatures.
P:OPERL\Axd O03-98.doc.02/ 1/00 -4- Advantageously, the present invention provides a simple and economic method of the type mentioned at the outset, by which acetylene can be removed from the air to be fractionated and which avoids the disadvantages mentioned above.
According to the invention there is provided a process for low temperature air separation, whereby the air is compressed, cooled in at least one switch-over heat exchanger which is a reversing exchanger or Revex and subsequently fractionated in at least one distillation column, wherein acetylene prior to the entry of the air into the heat exchanger is catalytically oxidised at a temperature between 70 and 130 0 C, and that water and carbon dioxide are substantially removed from the air in the heat exchanger.
In accordance with the invention, the removal of acetylene is arranged upstream of the water and carbon dioxide removal. Prior to the entry of the air into the heat exchanger, i.e.
in the "warm section" of the air separation plant, acetylene is removed from the air, whilst 15 water and carbon dioxide are removed from the air in switch-over heat exchangers or Revex. In this process, the air, prior to its entry into the heat exchanger or heat exchangers, is neither heated nor cooled by additional apparatus; thus the process can be accomplished in a simple and cost-effective manner.
In low temperature air separation plants, the air is initially compressed in a multi-stage compressor, whereby the air is intercooled after each compression stage. In accordance with the invention, acetylene is removed from the air by catalytic oxidation. To accomplish this, the air is supplied to the catalyst for the acetylene removal at a temperature between 70 and 130 0 C, preferably between 80 and 1 10 0 C. Therefore, the catalyst can be positioned between the last compressor stage and the aftercooler of the compressor. The acetylene concentration after the catalytic oxidation is less than 1 ppb.
The air freed of acetylene is subsequently, via the aftercooler, supplied to the switch-over heat exchanger where water and carbon dioxide are separated.
Advantageously, a precious metal supported on a carrier is used as catalyst, as this allows the removal of acetylene from the air at a high rate of efficiency. The precious metals L platinum and palladium supported on a carrier such as A1 2 0 3 have proven to be particularly suited for this purpose.
Also the use of metal oxides, in particular MnO2, Hopcalit, Co304, Fe203 and NiO or the use of mixtures of metal oxides have proven to be advantageous as catalysts, as these allow, at the temperatures prevailing after the last compressor, an effective acetylene removal from the air to be fractionated.
The process in accordance with the invention has clear advantages compared with the state of the art. The removal of acetylene in the "warm section" of the air separation plant can be achieved in a manner technically simpler than in the "cold section".
The removal can be accomplished without additional heating and/or cooling of the air, which renders the use of additional heat exchangers, for instance, unnecessary. This results in obvious savings as far as investment costs and energy consumption are concerned. The removal of carbon dioxide and water from the air is performed in .switch-over heat exchangers. The catalyst provided for the acetylene removal can thus be of a comparatively small size. The invention is particularly suited to very large plants and for plants which recover oxygen only.
During compression of the air used, care must be taken that the air is not overheated due to the resultant compression heat, as otherwise the work required to perform the compression action will be increased out of proportion. For this reason, the compression is usually performed in several stages, with coolers interpositioned, which eliminate the compression heat. By selection of the temperature range according to the invention between 70 and 130 0 C, a preheating of the air prior to entry into the catalyst is rendered unnecessary, and the air compression can be performed at lower temperatures. In this manner, energy savings are achieved in comparison with traditional methods.
The invention is described by example of a preferred embodiment in the schematic drawing.
The only figure shows a low temperature air separation plant with Revex and a catalyst for the removal of acetylene in the "warm section" of the air separation plant.
The air to be fractionated is supplied via an air filter 1 to an air compressor 2. The air compressor 2 is equipped with several stages whereby, between the individual compression stages, intercooling of the air is provided. The air exiting from the compressor 2 prior to the subsequent aftercooling has a temperature of between and 110 0 C. The acetylene content is approx. 10 ppb, but can be as high as a few ppm.
Without any further heating, the air is supplied directly into a catalyst 3, where acetylene is oxidised catalytically. As catalytic material, Pd is applied on a A1203 carrier. After the catalytic conversion, the air contains less than 1 ppb of acetylene.
Thus a dangerous concentration of acetylene in the liquid oxygen is avoided, without 0: any further apparatus being required for the acetylene removal.
After the catalyst 3, the air freed of acetylene is cooled in the traditional aftercooler 4 of the compressor 2 and subsequently supplied to the Revex pair 5, 6. In these switchover heat exchangers 5, 6 the air is cooled down to the dew point, whereby carbon dioxide and water are removed from the air. The Revex 5, 6 are followed by a traditional distillation column with a pressure column 8, a main condenser 9 and a low pressure column 10 with which oxygen is recovered in the known manner. The entire low temperature section of the air separation plant is located in a coldbox mantel 11.
The reference to any prior art in this specification is not, and should not be taken as, an acknowledgment or any form of suggestion that the prior art forms part of the common general knowledge in Australia.

Claims (6)

1. Process for low temperature air separation, whereby the air is compressed, cooled in at least one switch-over heat exchanger which is a reversing exchanger or Revex and subsequently fractionated in at least one distillation column, wherein acetylene prior to the entry of the air into the heat exchanger is catalytically oxidised at a temperature between 70 and 130'C, and that water and carbon dioxide are substantially removed from the air in the heat exchanger.
2. Process in accordance with Claim 1, wherein the acetylene is catalytically oxidised at a temperature between 80 and 110C.
3. Process in accordance with Claim 1 or 2, wherein as a catalyst a precious metal oeo supported on a carrier is used.
4. Process in accordance with Claim 3, wherein as the catalyst Pd or Pt supported on a :carrier are used.
5. Process in accordance with any one of the Claims 1 to 4, wherein as the catalyst a S° 20 metal oxide or mixtures of metal oxides are used.
6. Process for low temperature air separation substantially as hereinbefore described with reference to the drawings. DATED THIS 2nd day of November, 2000 Linde Aktiengesellschaft by DAVIES COLLISON CAVE Patent Attorneys for the Applicants
AU50403/98A 1997-01-10 1998-01-09 Catalytic removal of acetylene during separation of air Ceased AU728970B2 (en)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE19700644A DE19700644A1 (en) 1997-01-10 1997-01-10 Removal of acetylene during air separation
DE19700644 1997-01-10

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AU5040398A AU5040398A (en) 1998-07-16
AU728970B2 true AU728970B2 (en) 2001-01-25

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EP (1) EP0852964A1 (en)
JP (1) JPH10202060A (en)
KR (1) KR19980070370A (en)
AR (1) AR011356A1 (en)
AU (1) AU728970B2 (en)
BR (1) BR9800276A (en)
CA (1) CA2226592A1 (en)
DE (1) DE19700644A1 (en)
NO (1) NO980101L (en)
TW (1) TW357255B (en)
ZA (1) ZA98156B (en)

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Publication number Priority date Publication date Assignee Title
TWI363655B (en) 2004-03-30 2012-05-11 Taiyo Nippon Sanso Corp Pre-processing refining device of air liquefying/separating apparatus, hydrocarbon absorption agent, and pre-processing method of air material
DE102006058082A1 (en) * 2006-12-07 2008-06-12 Beko Technologies Gmbh Cleaning system for gases
JP6580848B2 (en) * 2015-03-30 2019-09-25 積水化学工業株式会社 Gas purification method and apparatus, and valuable material generation method and apparatus
JP6841878B2 (en) * 2019-08-29 2021-03-10 積水化学工業株式会社 Gas purification method and equipment, and valuable resource generation method and equipment
CN113786830B (en) * 2021-08-24 2023-08-15 万华化学(四川)有限公司 Preparation method and application of catalyst for treating acetylene device carbon black water desorption alkyne-containing waste gas

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US295439A (en) * 1884-03-18 Mail-bag
US1836927A (en) * 1929-12-04 1931-12-15 Ig Farbenindustrie Ag Removal of acetylene from gases
GB1001294A (en) * 1952-06-02 1965-08-11 British Oxygen Co Ltd Purification of gas mixtures

Family Cites Families (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE2014655A1 (en) * 1969-05-23 1970-11-26 VEB Leuna-Werke Walter Ulbricht, χ 4220 Leuna Removal of acetylene impurities from air - by palladium catalysed hydrogenation
GB1471496A (en) * 1974-04-26 1977-04-27 Le Tek I Kholodilnoi Promy Process for low-temperature separation of air
DE3322473A1 (en) * 1983-06-22 1985-01-03 Linde Ag, 6200 Wiesbaden Method and device for avoiding enrichment of undesired components in a liquid medium
JPS61190277A (en) * 1985-02-16 1986-08-23 大同酸素株式会社 High-purity nitrogen and oxygen gas production unit

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US295439A (en) * 1884-03-18 Mail-bag
US1836927A (en) * 1929-12-04 1931-12-15 Ig Farbenindustrie Ag Removal of acetylene from gases
GB1001294A (en) * 1952-06-02 1965-08-11 British Oxygen Co Ltd Purification of gas mixtures

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CA2226592A1 (en) 1998-07-10
AR011356A1 (en) 2000-08-16
BR9800276A (en) 2001-03-20
NO980101L (en) 1998-07-13
DE19700644A1 (en) 1998-07-16
JPH10202060A (en) 1998-08-04
ZA98156B (en) 1998-07-09
AU5040398A (en) 1998-07-16
NO980101D0 (en) 1998-01-09
KR19980070370A (en) 1998-10-26
EP0852964A1 (en) 1998-07-15
TW357255B (en) 1999-05-01

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