DE3319664A1 - Process and apparatus for purifying gas mixtures - Google Patents

Process and apparatus for purifying gas mixtures

Info

Publication number
DE3319664A1
DE3319664A1 DE19833319664 DE3319664A DE3319664A1 DE 3319664 A1 DE3319664 A1 DE 3319664A1 DE 19833319664 DE19833319664 DE 19833319664 DE 3319664 A DE3319664 A DE 3319664A DE 3319664 A1 DE3319664 A1 DE 3319664A1
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DE
Germany
Prior art keywords
gas
reactors
heat
adsorption
adsorption reactor
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.)
Withdrawn
Application number
DE19833319664
Other languages
German (de)
Inventor
Burkhard Dipl.-Chem.Dr. 4200 Oberhausen Harder
Karl Dipl.-Ing.Dr. 4300 Essen Knoblauch
Bernhard Dipl.-Ing. 4250 Bottrop Stricker
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Bergwerksverband GmbH
Original Assignee
Bergwerksverband GmbH
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Bergwerksverband GmbH filed Critical Bergwerksverband GmbH
Priority to DE19833319664 priority Critical patent/DE3319664A1/en
Priority to IN426/DEL/84A priority patent/IN161153B/en
Priority to AU28720/84A priority patent/AU2872084A/en
Priority to ZA844064A priority patent/ZA844064B/en
Priority to JP59109789A priority patent/JPS6041522A/en
Publication of DE3319664A1 publication Critical patent/DE3319664A1/en
Priority to JP1991077936U priority patent/JPH0499215U/ja
Withdrawn legal-status Critical Current

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Classifications

    • 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
    • B01D53/02—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 adsorption, e.g. preparative gas chromatography
    • B01D53/04—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 adsorption, e.g. preparative gas chromatography with stationary adsorbents
    • B01D53/0462—Temperature swing adsorption
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2256/00—Main component in the product gas stream after treatment
    • B01D2256/10—Nitrogen
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/40—Further details for adsorption processes and devices
    • B01D2259/402—Further details for adsorption processes and devices using two beds
    • 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
    • B01D53/02—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 adsorption, e.g. preparative gas chromatography
    • B01D53/04—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 adsorption, e.g. preparative gas chromatography with stationary adsorbents
    • B01D53/0407—Constructional details of adsorbing systems
    • B01D53/0438—Cooling or heating systems

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Separation Of Gases By Adsorption (AREA)

Abstract

In a process for purifying gas mixtures using the pressure swing adsorption method, in which the gas mixture flows through an adsorbent layer in an adsorption reactor with part of the gas components being adsorbed, and one or more gas components flow off at the end of the adsorbent layer and in which the crude gas stream is divided into a product gas stream and a residual gas stream, the adsorption reactor is heated/cooled by a heat exchange medium in the temperature range -20 to +40 DEG C. For this purpose, one of the gas streams is passed through a cavity between the adsorption reactor 1 and a heat shield 9. An apparatus for carrying out the process comprises reactors 1 having cooling coils 5 located in a thermal insulation layer 10, which cooling coils are connected to a machine 6 producing cold or heat, and further comprises the pipes 2-4 connecting the reactors. By means of the compressor 7, the gas mixture is passed through the heat exchanger 8 into the reactors 1, while residual gas exits via pipe 4 into a cavity 11 located between solar shield 9 and thermal insulation layer 10. <IMAGE>

Description

Die Erfindung betrifft ein Verfahren gemäß dem OberbegriffThe invention relates to a method according to the preamble

von Patentanspruch 1.of claim 1.

Es ist bekannt, Gasgemische zu reinigen oder zu trennen und sich dabei der zyklischen Druckwechseladsorptionstechnik an Adsorptionsmitteln zu bedienen. Diese Prozesse lassen sich wirtschaftlich in einem Temperaturbereich von etwa -20 bis +400C betreiben, weil in diesem Temperaturbereich das beste Verhältnis zwischen Adsorptionskapazität und Selektivität vorliegt.It is known to purify or separate gas mixtures and thereby to use the cyclic pressure swing adsorption technology on adsorbents. These processes can be carried out economically in a temperature range of around -20 operate up to + 400C because in this temperature range the best ratio between Adsorption capacity and selectivity is present.

Weicht die mittlere Arbeitstemperatur von dem genannten Temperaturbereich ab oder liegt sie in den Grenzzonen, so sind größere Adsorptionsmittelmengen erforderlich.Does the mean working temperature deviate from the stated temperature range or if it is in the border zones, larger amounts of adsorbent are required.

Demnach ist der Energiebedarf aller Anlagen, die nicht auf der optimalen Temperatur arbeiten, beträchtlich, was z. B.Accordingly, the energy requirements of all systems that are not at the optimum Temperature work, considerably, what z. B.

auch schon bei den teilweise hohen Temperaturunterschieden zwischen den Tag- und den Nachtstunden zum Tragen kommt, und erst recht im Falle von Gasreinigungen in extremen Klimazonen, wie etwa bei ca. 609C in tropischen und -80°C in arktischen Regionen.even with the sometimes high temperature differences between the day and night comes into play, and especially in the case of gas cleaning in extreme climates, such as around 609C in tropical and -80 ° C in arctic Regions.

Es ist bekannt, in extremen Klimasituationen betriebene Druckwechselanlagen thermisch zu isolieren. Dadurch wird jedoch nur ein Teilerfolg erzielt, da das zu adsorbierende Gas in der Regel auf Umgebungstemperatur sein wird, die aber erheblich außerhalb des Bereiches optimaler Temperatur liegt. Die Erfindung beruht in ihrer allgemeinen Form auf der Uberlegung, statt in erster Linie Isoliermaßnahmen zu ergreifen, den Adsorptionsreaktor mittels eines zusätzlichen Wärmetauschermediums zu kühlen oder zu erwärmen, da die hierfür erforderliche Energie weit unterhalb der ansonsten notwendigen Kompressionsenergie liegt. Verbessert wird dieses Verfahren selbstverständlich durch die Kombination mit einer Wärmeisolation und ganz besonders dann, wenn der mit einem Wärmeaustauscher umgebene Adsorptionsreaktor wärmeisoliert ist und von einem Wärmeschutzschild umgeben wird sowie der Zwischenraum vom Restgas und/oder Produktgasstrom durchspült wird, weil hierdurch die Wärme-oder Kälteenergie, die zur Vorwärmung/Vorkühlung in das Rohgas hineingesteckt wurde, zum Teil noch nachträglich genutzt werden kann.It is known to operate pressure swing systems in extreme climatic situations thermally isolate. However, this only achieves partial success, since that too Adsorbing gas will usually be at ambient temperature, but that will be significant is outside the range of optimal temperature. The invention resides in their general form on consideration, instead of primarily taking isolation measures, to cool the adsorption reactor by means of an additional heat exchange medium or to heat, since the energy required for this is far below that otherwise necessary compression energy. This process will of course be improved through the combination with thermal insulation and very special when the adsorption reactor surrounded by a heat exchanger is thermally insulated and is surrounded by a heat shield and the space in between is surrounded by residual gas and / or product gas flow is flushed through, because this causes the heating or cooling energy, which was inserted into the raw gas for preheating / precooling, partly still can be used subsequently.

Es ist demnach die Aufgabe der Erfindung, ein Verfahren und eine Vorrichtung bereitzustellen, die die vorerwähnten Nachteile vermeidet und sowohl die Adsorptionsmittelmengen als auch die Kompressionsenergie für das zu trennende Rohgasgemisch möglichst weitgehend vermindert.It is accordingly the object of the invention, a method and a device provide which avoids the aforementioned disadvantages and both the amounts of adsorbent and the compression energy for the raw gas mixture to be separated as much as possible reduced.

Die Aufgabe wird hinsichtlich eines Verfahrens der eingangs genannten Art durch die kennzeichnenden Merkmale von Patentanspruch 1 gelöst; weitere Ausführungen der Erfindung ergeben sich aus den Unteransprüchen 2 bis 3. Die Erfindung wird hinsichtlich einer Vorrichtung durch die kennzeichnenden Merkmale von Patentanspruch 3 gelöst.With regard to a method, the task is as mentioned at the beginning Kind solved by the characterizing features of claim 1; further explanation of the invention emerge from the dependent claims 2 to 3. The invention is with respect to a device solved by the characterizing features of claim 3.

Ausführunqsbeispiel Bei der Sicstoffezeugung aus Luft werden z. B. bei eint~r Arbeitstempc'rit:tir von 200C und einer erwünschten Stickstoffreinheit von 99,9 % bei 1,7 bar und 300 m3/h Produktgas ca. 10,5 m3 des Adsorptionsmittels benötigt; der Luftbedarf beträgt 1.200 m3/h. - Soll die gleiche Stickstoffproduktionsrate bei einer mittleren Arbeitstemperatur von 400c bei sonst gleichen Druckbedingungen erzielt werden, wird eine fast doppelt so große Menge (16,8 m3) des Adsorptionsmittels benötigt und der Luftbedarf beträgt nunmehr ca. 1.845 m3/h. Der Gesamtenergiebedarf für die PSA-Anlage bei einer Bettemperatur von 20 0C beträg 194 kW, demgegenüber bei einer Bettemperatur von 40 0C 310 kW. Für die Kühlung der Adsorptionsbehälter und der Eingangs luft auf 20 0C ist ein Energieverbrauch von 24 kW zu veranschlagen. Damit würde also ein Energiegewinn von ca. 100 kW erzielt, wenn die Gasreinigung nicht bei 40, sondern bei 200c durchgeführt würde.Exemplary embodiment In the production of Sicstoff from air z. B. at a working temperature of 200C and a desired nitrogen purity of 99.9% at 1.7 bar and 300 m3 / h product gas approx. 10.5 m3 of the adsorbent needed; the air requirement is 1,200 m3 / h. - Shall have the same rate of nitrogen production at an average working temperature of 400c under otherwise identical pressure conditions achieved will be almost twice as large (16.8 m3) of the adsorbent is required and the air requirement is now approx. 1,845 m3 / h. The total energy requirement for the PSA system at a bed temperature of 20 0C is 194 kW, on the other hand at a bed temperature of 40 0C 310 kW. For cooling the Adsorption tank and the inlet air to 20 0C is an energy consumption of 24 kW should be estimated. This would result in an energy gain of approx. 100 kW, if the gas cleaning were not carried out at 40 but at 200c.

Weiter Vorteile und Ausführungsformen der Erfindung werden in einem bevorzugten Ausführungsbeispiel anhand der beiliegenden Zeichnung näher erläutert. Die Figur zeigt schematisch eine Vorrichtung zur Reinigung von Gasgemischen (Rohgas) mittels der üblichen Druckwechseladsorptionstechnik. Diese Vorrichtung besteht aus der Druckwechselanlage, von der nur die beiden Reaktoren 1 und die verbindenen Rohrleitungen 2 - 4 angedeutet sind. Die Reaktoren sind von den in eine Wärmeisolationsschicht 10 eingebetteten Rohrschlangen 5 umgeben, die mit einer Kälte- bzw. alternativ einer Wärmeerzeugungsmaschine 6 verbunden sind. In tropischen Gebieten wird eine Kälte-, in arktischen Gebieten eine Wärmemaschine benötigt. Die Rohrschlange sowie die Wärmeisolationsschicht sind wärmeteschniscb auszulegen .Further advantages and embodiments of the invention are in one preferred exemplary embodiment explained in more detail with reference to the accompanying drawings. The figure shows schematically a device for cleaning gas mixtures (raw gas) by means of the usual pressure swing adsorption technology. This device consists of the pressure change system, of which only the two reactors 1 and the connecting pipelines 2-4 are indicated. The reactors are covered by a thermal insulation layer 10 embedded coils 5 surrounded with a cold or alternatively a Heat generating machine 6 are connected. In tropical areas, a cold, a heat engine is required in arctic regions. The pipe coil and the thermal insulation layer are to be interpreted as heat sinks.

Durch die Leitung 2 wird mittels des Kompressors 7 auf Betriebsdruck komprimierte Luft zunächst im Wärmeaustauscher 8 auf 150C gekühlt und zyklisch in einen der beiden Reaktoren geleitet. Der produzierte Stickstoff verläßt die Druckwechselanlage über Leitung 3, während das Restgas mit etwa 200C über die Leitung 4 in den zwischen dem Wärmeschutzschild 9 und der Wärmeisolationsschicht 10 der Reaktoren 1 gbiletcn Hohlraum 11 eintritt.Through the line 2 is by means of the compressor 7 to operating pressure compressed air is first cooled in the heat exchanger 8 to 150C and cyclically in passed one of the two reactors. The nitrogen produced leaves the pressure swing system via line 3, while the residual gas with about 200C via line 4 in the between the heat shield 9 and the heat insulation layer 10 of the reactors 1 gbiletcn Cavity 11 enters.

- L e e r s e i t e -- L e r s e i t e -

Claims (4)

Verfahren und Vorrichtung zur Reinigung von Gasgemischen Patentansprüche Verfahren zur Reinigung von Gasgemischen (Rohgas) mittels üblicher Druckwechseladsorptionstechnîk, bei dem eine Adsorptionsmittelschicht in einem Adsorptionsreaktor vom Rohgas unter Adsorption eines Teiles der Gaskomponenten durchströmt wird und eine oder mehrere Gaskomponenten am Ende der Adsorptionsmittelschicht abströmen und bei dem der Rohgasstrom in einen Produktgas- und einen Restgasstrom zerlegt wird, gekennzeichnet durch Temperieren des Adsorptionsreaktors mittels eines Wärmeaustauschmediums im Temperaturbereich von - 20 bis + 40 OC. Method and device for cleaning gas mixtures Patent claims Process for cleaning gas mixtures (raw gas) using the usual pressure swing adsorption technology, in which an adsorbent layer in an adsorption reactor from the raw gas under Adsorption of a part of the gas components is flowed through and one or more Gas components flow off at the end of the adsorbent layer and in which the raw gas flow is broken down into a product gas and a residual gas stream, characterized by temperature control of the adsorption reactor by means of a heat exchange medium in the temperature range from - 20 to + 40 OC. 2. Verfahren nach Anspruch i; dadurch gekennzeichnet, daß einer der Gasströme durch einen Hohlraum zwischen dem Adsorptionsreaktor und einem diesen umgebenden Wärmeschutzschild geleitet wird. 2. The method according to claim i; characterized in that one of the Gas flows through a cavity between the adsorption reactor and one of these surrounding heat shield is conducted. 3. Vorrichtung zur Durchführung des Verfahrens nach den Ansprüchen 1 und 2, gekennzeichnet durch Reaktoren (1) mit in einer Wärmeisolationsschicht (10) befindlichen Kühlschlange (5), die mit Rohrleitungen (2 - 4) verbunden sind und sich mit dem die Reaktoren (1) umgebenden Hohlraum (11) innerhalb eines Wärmeschutzschildes (9) befinden. 3. Device for performing the method according to the claims 1 and 2, characterized by reactors (1) with in a thermal insulation layer (10) located cooling coil (5), which are connected to pipes (2-4) and with the cavity (11) surrounding the reactors (1) within a heat shield (9) are located. 4. Vorrichtung nach Anspruch 3, gekennzeichnet durch außerhalb des Wärmeschutzschildes (9) angeordneten Kompressor (7), Wärmeaustauscher (8) und Kälte-/Wärmemaschine (6).4. Apparatus according to claim 3, characterized by outside the Heat shield (9) arranged compressor (7), heat exchanger (8) and cooling / heating machine (6).
DE19833319664 1983-05-31 1983-05-31 Process and apparatus for purifying gas mixtures Withdrawn DE3319664A1 (en)

Priority Applications (6)

Application Number Priority Date Filing Date Title
DE19833319664 DE3319664A1 (en) 1983-05-31 1983-05-31 Process and apparatus for purifying gas mixtures
IN426/DEL/84A IN161153B (en) 1983-05-31 1984-05-21
AU28720/84A AU2872084A (en) 1983-05-31 1984-05-25 Pressure change adsorption
ZA844064A ZA844064B (en) 1983-05-31 1984-05-29 Process and equipment for purifying gas mixtures
JP59109789A JPS6041522A (en) 1983-05-31 1984-05-31 Method and apparatus for purifying gaseous mixture
JP1991077936U JPH0499215U (en) 1983-05-31 1991-09-26

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
DE19833319664 DE3319664A1 (en) 1983-05-31 1983-05-31 Process and apparatus for purifying gas mixtures

Publications (1)

Publication Number Publication Date
DE3319664A1 true DE3319664A1 (en) 1984-12-06

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DE19833319664 Withdrawn DE3319664A1 (en) 1983-05-31 1983-05-31 Process and apparatus for purifying gas mixtures

Country Status (4)

Country Link
JP (2) JPS6041522A (en)
AU (1) AU2872084A (en)
DE (1) DE3319664A1 (en)
ZA (1) ZA844064B (en)

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0537597A1 (en) * 1991-10-07 1993-04-21 Praxair Technology, Inc. Low temperature pressure swing adsorption with refrigeration
EP0617995A1 (en) * 1993-03-30 1994-10-05 SODIBO S.p.A. Activated-carbon solvent treatment unit for dry-cleaning machines with increased absorption
EP0736319A1 (en) * 1994-02-02 1996-10-09 Praxair Technology, Inc. Pressure swing adsorption heat recovery
US7266949B2 (en) * 2002-01-18 2007-09-11 Thermagen Sa Insulation of a self-cooling beverage package
EP2415512A1 (en) * 2009-03-30 2012-02-08 Taiyo Nippon Sanso Corporation Pressure variation adsorption method for gas separation of gas and apparatus therefor

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4696681A (en) * 1986-10-01 1987-09-29 The Boc Group, Inc. PSA assembly

Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE2950731A1 (en) * 1979-12-17 1981-06-25 Michael 8000 München Zoche Removing nitrogen from argon in purification process - involves heating to reaction temp. before introducing into chamber contg. titanium sponge

Family Cites Families (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS5235173A (en) * 1975-09-13 1977-03-17 Kobe Steel Ltd Cooling method of adsorbent
JPS5745321A (en) * 1980-09-03 1982-03-15 Toshiba Corp Activated carbon adsorb

Patent Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE2950731A1 (en) * 1979-12-17 1981-06-25 Michael 8000 München Zoche Removing nitrogen from argon in purification process - involves heating to reaction temp. before introducing into chamber contg. titanium sponge

Cited By (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0537597A1 (en) * 1991-10-07 1993-04-21 Praxair Technology, Inc. Low temperature pressure swing adsorption with refrigeration
EP0617995A1 (en) * 1993-03-30 1994-10-05 SODIBO S.p.A. Activated-carbon solvent treatment unit for dry-cleaning machines with increased absorption
EP0736319A1 (en) * 1994-02-02 1996-10-09 Praxair Technology, Inc. Pressure swing adsorption heat recovery
US7266949B2 (en) * 2002-01-18 2007-09-11 Thermagen Sa Insulation of a self-cooling beverage package
EP2415512A1 (en) * 2009-03-30 2012-02-08 Taiyo Nippon Sanso Corporation Pressure variation adsorption method for gas separation of gas and apparatus therefor
CN102365122A (en) * 2009-03-30 2012-02-29 大阳日酸株式会社 Pressure variation adsorption method for gas separation of gas and apparatus therefor
EP2415512A4 (en) * 2009-03-30 2012-08-22 Taiyo Nippon Sanso Corp Pressure variation adsorption method for gas separation of gas and apparatus therefor
US8657922B2 (en) 2009-03-30 2014-02-25 Taiyo Nippon Sanso Corporation Pressure swing adsorption-type gas separation method and separation apparatus
CN102365122B (en) * 2009-03-30 2014-06-25 大阳日酸株式会社 Pressure variation adsorption method for gas separation of gas and apparatus therefor

Also Published As

Publication number Publication date
AU2872084A (en) 1984-12-06
ZA844064B (en) 1985-01-30
JPS6041522A (en) 1985-03-05
JPH0499215U (en) 1992-08-27

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