EP0233169B1 - Verfahren zur Behandlung von Gasölen - Google Patents

Verfahren zur Behandlung von Gasölen Download PDF

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Publication number
EP0233169B1
EP0233169B1 EP87870016A EP87870016A EP0233169B1 EP 0233169 B1 EP0233169 B1 EP 0233169B1 EP 87870016 A EP87870016 A EP 87870016A EP 87870016 A EP87870016 A EP 87870016A EP 0233169 B1 EP0233169 B1 EP 0233169B1
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EP
European Patent Office
Prior art keywords
hydrocarbons
treatment
feed
amount
effluent
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 - Lifetime
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EP87870016A
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English (en)
French (fr)
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EP0233169A2 (de
EP0233169B2 (de
EP0233169A3 (en
Inventor
Jacques F. Grootjans
Pierre J. Bredael
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Total Research and Technology Feluy SA
Original Assignee
Fina Research SA
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Application filed by Fina Research SA filed Critical Fina Research SA
Publication of EP0233169A2 publication Critical patent/EP0233169A2/de
Publication of EP0233169A3 publication Critical patent/EP0233169A3/fr
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Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
    • C10G45/58—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins
    • C10G45/60—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins characterised by the catalyst used
    • C10G45/64—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins characterised by the catalyst used containing crystalline alumino-silicates, e.g. molecular sieves
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G65/00—Treatment of hydrocarbon oils by two or more hydrotreatment processes only
    • C10G65/02—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only
    • C10G65/12—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including cracking steps and other hydrotreatment steps
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/70—Catalyst aspects
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F02—COMBUSTION ENGINES; HOT-GAS OR COMBUSTION-PRODUCT ENGINE PLANTS
    • F02B—INTERNAL-COMBUSTION PISTON ENGINES; COMBUSTION ENGINES IN GENERAL
    • F02B3/00—Engines characterised by air compression and subsequent fuel addition
    • F02B3/06—Engines characterised by air compression and subsequent fuel addition with compression ignition

Definitions

  • the present invention relates to a process for treating diesel fuel charges in order to be able to extract more recoverable products therefrom than by the usual treatments.
  • the present invention relates to a particular combination of two treatments of diesel fuel charges in order to promote the production of diesel and petrol.
  • Heavy gas oils (vacuum distillation, VGO, or 370 to 540 C cut gas) were generally sent directly to the catalytic cracking unit in order to convert them into lighter, highly recoverable hydrocarbons; however, it is desirable to try to make the best possible use of all the constituents of gas oils, whether they come from atmospheric distillation or from vacuum distillation. We have also realized in recent years, that it was possible to treat gas oils before sending them to catalytic cracking so as to recover many more recoverable products than by catalytic cracking alone.
  • Gas oils can also be subjected to a process to remove waxy paraffinic hydrocarbons. This leads to lowering the cloud point of gas oils.
  • EP-A-0 070 125 describes a process for treating boiling hydrocarbons in the range of heavy gas oils, in the presence of a catalyst consisting of a mixture comprising generally modified silicalite and a hydrogenation catalyst deposited on a support . Significant pour point reduction results are obtained when the silicalite is modified by a catalytic metal of the palladium type.
  • the present invention relates to a process for the treatment of boiling hydrocarbons in the range of heavy gas oils so as to increase the recovery of light hydrocarbons.
  • the present invention also relates to a process for the treatment of heavy gas oils in two stages making it possible to increase the production of diesel oil and of petrol relative to the quantity generally recoverable by catalytic cracking of the same charge.
  • the present invention also relates to a process which makes it possible to treat hydrocarbons having a boiling point of between approximately 370 C and 540 C so as to obtain a significant quantity of variable light hydrocarbons.
  • the Applicant has unexpectedly found that by first subjecting the charge of boiling hydrocarbons in the range of heavy gas oils to a treatment to remove waxy paraffinic hydrocarbons, by passing over a polymorphic crystalline silica of the unmodified silicalite type. under suitable conditions, and by subjecting the resulting charge to a light hydrocracking, a production of light hydrocarbons, in particular diesels and gasolines, was obtained in quantities clearly improved compared to what could reasonably be expected.
  • the fillers used for the process of the invention are heavy gas oils, or vacuum distillation gas oils (VGO), comprising the fraction of hydrocarbons having a boiling point of 370 to 540 ° C. approximately. These charges can contain at most 25% of hydrocarbons having a boiling point below 370 C.
  • VGO vacuum distillation gas oils
  • the process of the invention is particularly suitable for heavy diesel fillers containing significant sulfur contents as high as 4% (by weight).
  • a preferred application of the invention lies in the treatment of fillers containing more than about 1% of sulfur.
  • an unmodified silicalite is used, that is to say a crystalline polymorphic silica which has no exchange capacity compared to zeolites and which has not been modified by a catalytic metal.
  • Aluminum can be present in these catalysts, but only in the form impurities from the starting materials and in particular from the source of silica used. The methods for obtaining these materials are given in US Patent 4,061,724 to Grose and Flanigen.
  • Silicalites are microporous materials prepared hydrothermally using a reaction mixture comprising tetrapropylammonium cations, alkali metal cations, water and a source of reactive silica.
  • an unmodified silicalite having pores of about 0.55 nm and in the form of crystallites of size less than 8 ⁇ m is used.
  • the step of removing waxy paraffinic hydrocarbons can be carried out in any device comprising a reaction zone containing the catalyst of the silicalite type.
  • the Applicant has surprisingly found that by subjecting the charge resulting from the first step directly to a light hydrocracking, a final charge containing light hydrocarbons was obtained in quantities significantly greater than those which could be obtained. hope.
  • the light hydrocracking reaction is carried out on a conventional light hydrocracking catalyst.
  • a conventional light hydrocracking catalyst By way of example, mention may be made of a Ni-Mo catalyst deposited on alumina and silica, prepared by incorporation of Ni and Mo in the form of oxide followed by drying and then by treatment with scanning of a mixture of hydrogen and H 2 S (1-2% vol.) first at 200-250 ° C then up to 320-350 ° C. It is also possible to partially replace this catalyst with a Co-Mo catalyst deposited on alumina, prepared in a similar manner.
  • these catalysts In their oxide form, these catalysts generally contain from 3 to 6% by weight of NiO or CoO, and from 10 to 20% by weight of MoOs; they have a specific surface generally between 150 and 300 m 2 / g and the pore volume is generally between 0.3 and 0.6 ml / g. These catalysts are commercially available in oxide form.
  • the reactions can be carried out in two reactors arranged in cascade and under temperature and pressure conditions which need not necessarily be identical, the Applicant has found that the two reactions could be carried out in the same reactor. proportion of the different catalysts plays a certain role in obtaining interesting results. Thus, the Applicant has found that 15 to 25% by volume of silicalite should be used, relative to the total catalyst and 85 to 75% by volume of light hydrocracking catalyst.
  • the catalysts can be arranged in one or more layers which can be surrounded by layers of inert materials.
  • the two stages of the process are carried out in the same reactor, and the various catalysts are thus arranged in several beds, the first bed encountered being constituted by a polymorphic crystalline silica of the type unmodified silicalite.
  • the charge is passed through the reaction zone containing the catalysts at a temperature between 350 and 450 ° C., and preferably between 380 and 420 ° C. under a pressure between atmospheric pressure and 80 bars, and preferably between 35 and 65 bars, and at an hourly liquid space velocity (LHSV) of between 0.1 and 20 I / I (calculated with respect to all the catalysts), preferably between 0.5 and 5 I / I.
  • LHSV hourly liquid space velocity
  • hydrogen is introduced into the reaction zone, in an amount such that the hydrogen / hydrocarbon volume ratio is between 50 and 5000 and preferably between 250 and 1000 (the volume of the hydrogen being measured in gaseous state and under standard conditions).
  • the hydrogen / hydrocarbon volume ratio is between 50 and 5000 and preferably between 250 and 1000 (the volume of the hydrogen being measured in gaseous state and under standard conditions).
  • the gas recovered at the outlet of the reactor is generally recycled.
  • part of the recycled gas is permanently drawn off and replaced by hydrogen.
  • the Applicant has also observed a synergistic effect by carrying out another embodiment of the process of the invention, in which the charge is subjected to a light hydrocracking before the removal of the waxy paraffinic hydrocarbons.
  • this effect is notably weaker than when light hydrocracking constitutes the second stage of the process, but the quality of the cut 250-370 C is better.
  • the latter catalyst was pretreated by subjecting it to drying at 130 ° C. followed by sulphurization at 54 bar while scanning an H 2 + H 2 S mixture (1.1% vol) first at 250 ° C until the partial pressure of H 2 S exceeds 0.03 bar at the outlet of the reactor, then gradually up to 320 ° C while maintaining a partial pressure of H 2 S greater than 0.03 exit bar.
  • the sulfurized Ni-Mo catalyst contained about 10% by weight of sulfur.
  • a 2.5 cm internal diameter reactor was filled with 20% by volume (i.e. 7 cm in height) of silicalite and 80% by volume (i.e. 28 cm in height) of Ni-Mo catalyst, all between two layers inert material (each 40 cm high).
  • a charge of hydrocarbons was passed into the reactor in normal mode, the charge successively passing through the silicalite, then the Ni-Mo.
  • the refinery hydrogen (called “pure” but containing about 85% hydrogen) was passed at a partial hydrogen pressure of at least 40 bars.
  • Example 1 The procedure described in Example 1 was repeated, replacing the Ni-Mo catalyst for half with a Co-Mo catalyst on alumina (commercially available under the name Ketjen 742) and for the other half with a catalyst. Ni-Mo on Al 2 O 3 / SiO 2 . The charge passed successively through the silicalite, the Co-Mo and then the Ni-Mo.
  • Example 2 The procedure described in Example 1 was repeated, reversing the catalysts, the charge passing through successively Ni-Mo then silicalite. The results are shown in Table 2.
  • the conversion due to the light hydrocracking step can be recalculated taking into account the conversion of example C1,
  • composition of some effluents and some properties of certain cuts are listed in Table 4, compared with the values of Example 1A.

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  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Crystallography & Structural Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Catalysts (AREA)

Claims (7)

1. Verfahren zur Behandlung von Beschickungen von siedenden Kohlenwasserstoffen aus der Reihe der schweren Gasöle zur Gewinnung leichter Kohlenwasserstoffe, das ein leichtes Hydrocracken und eine Entfernung paraffinischer wachsartiger Kohlenwasserstoffe umfaßt, dadurch gekennzeichnet, daß es besteht aus
(i) der Entfernung paraffinischer wachsartiger Kohlenwasserstoffe aus einer solchen Beschickung, indem man die Beschickung über ein kristallines polymorphes Siliciumdioxid vom Typ eines nicht modifizierten Silicalits unter solchen Bedingungen leitet, die zum Cracken der paraffinischen wachsartigen Kohlenwasserstoffe geeignet sind, dann
(ii) dem Unterwerfen der aus der ersten Stufe erhaltenen Beschickung einem leichten Hydrocracken und schließlich
(iii) dem Gewinnen der Beschickung, die eine erhebliche Menge leichter Kohlenwasserstoffe enthält, sowie dadurch, daß der nicht modifizierte Silicalit von 15 bis 25 Volumen-% des Katalysatorgesamtvolumens bildet.
2. Verfahren zur Behandlung von Beschickungen von siedenden Kohlenwasserstoffen aus der Reihe der schweren Gasöle zur Gewinnung leichter Kohlenwasserstoffe, das ein leichtes Hydrocracken und eine Entfernung paraffinischer wachsartiger Kohlenwasserstoffe umfaßt, dadurch gekennzeichnet, daß es besteht aus
(i) dem Unterwerfen einer solchen Beschickung einem leichten Hydrocracken, dann
(ii) dem Entfernen der paraffinischen wachsartigen Kohlenwasserstoffe aus der aus der ersten Stufe erhaltenen Beschickung, indem man diese über ein kristallines polymorphes Siliciumdioxid vom Typ eines nicht modifizierten Silicalits unter solchen Bedingungen leitet, die zum Cracken der paraffinischen wachsartigen Kohlenwasserstoffe geeignet sind, und dann
(iii) dem Gewinnen der Beschickung, die eine erhebliche Menge leichter Kohlenwasserstoffe enthält, sowie dadurch, daß der nicht modifizierte Silicalit von 15 bis 25 Volumen-% des Katalysatorgesamtvolumens bildet.
3. Verfahren nach einem der Ansprüche 1 oder 2, dadurch gekennzeichnet, daß die Beschickung wenigstens 75 % Kohlenwasserstoffe mit einem Siedepunkt von 370 bis 540 °C umfaßt.
4. Verfahren nach einem der Ansprüche 1 bis 3, dadurch gekennzeichnet, daß die Beschickung von 1 bis 4 % Schwefel enthält.
5. Verfahren nach einem der Ansprüche 1 bis 4, dadurch gekennzeichnet, daß man das Verfahren bei einer Temperatur von 350 bis 450° C, bei einem Druck von 1 bis 80 bar, bei einer LHSV von 0,1 bis 20 und in Gegenwart einer solchen Menge Wasserstoff, daß das Volumenverhältnis H2/HC von 50 bis 5000 beträgt, durchführt.
6. Verfahren nach einem der Ansprüche 1 bis 5, dadurch gekennzeichnet, daß man das Verfahren bei einer Temperatur von 380 bis 420 C, bei einem Druck von 35 bis 65 bar, bei einer LHSV von 0,5 bis 5 und in Gegenwart einer solchen Menge Wasserstoff, daß das Volumenverhältnis H2/HC von 250 bis 1000 beträgt, durchführt.
7. Verfahren nach einem der Ansprüche 1 bis 6, dadurch gekennzeichnet, daß man die Stufen (i) und (ii) als aufeinanderfolgendes Hindurchleiten durch zwei getrennte Katalysatorbetten in dem gleichen Reaktor durchführt.
EP87870016A 1986-02-03 1987-02-03 Verfahren zur Behandlung von Gasölen Expired - Lifetime EP0233169B2 (de)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
LU86288A LU86288A1 (fr) 1986-02-03 1986-02-03 Procede de traitement des gasoils
LU86288 1986-02-03

Publications (4)

Publication Number Publication Date
EP0233169A2 EP0233169A2 (de) 1987-08-19
EP0233169A3 EP0233169A3 (en) 1989-02-22
EP0233169B1 true EP0233169B1 (de) 1991-12-27
EP0233169B2 EP0233169B2 (de) 2001-08-29

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ID=19730635

Family Applications (1)

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EP87870016A Expired - Lifetime EP0233169B2 (de) 1986-02-03 1987-02-03 Verfahren zur Behandlung von Gasölen

Country Status (5)

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US (1) US4810356A (de)
EP (1) EP0233169B2 (de)
JP (1) JP2879793B2 (de)
DE (1) DE3775426D1 (de)
LU (1) LU86288A1 (de)

Families Citing this family (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5385663A (en) * 1992-06-18 1995-01-31 Uop Integrated hydrocracking-catalytic dewaxing process for the production of middle distillates
RU2128681C1 (ru) * 1993-10-08 1999-04-10 Акцо Нобель Н.В. Способ превращения парафинсодержащего углеводородного сырья
US5690810A (en) * 1994-11-14 1997-11-25 Texaco Inc. Single-step process to upgrade naphthas to an improved gasoline blending stock
US6068757A (en) * 1995-11-03 2000-05-30 Coastal Eagle Point Oil Company Hydrodewaxing process
EP0920911A1 (de) * 1997-12-05 1999-06-09 Fina Research S.A. Herstellung von Katalysatoren für die Olefinumsetzung
US6461497B1 (en) 1998-09-01 2002-10-08 Atlantic Richfield Company Reformulated reduced pollution diesel fuel
CA2292314C (en) * 1998-12-16 2007-02-06 China Petrochemical Corporation A process for producing diesel oils of superior quality and low solidifying point from fraction oils
EP1061117A1 (de) * 1999-06-16 2000-12-20 Fina Research S.A. Herstellung von Olefinen
US20030070965A1 (en) * 1999-11-01 2003-04-17 Shih Stuart S. Method for the production of very low sulfur diesel
US7955401B2 (en) * 2007-07-16 2011-06-07 Conocophillips Company Hydrotreating and catalytic dewaxing process for making diesel from oils and/or fats

Family Cites Families (25)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3700585A (en) * 1969-10-10 1972-10-24 Mobil Oil Corp Dewaxing of oils by shape selective cracking and hydrocracking over zeolites zsm-5 and zsm-8
US3654133A (en) 1970-06-23 1972-04-04 Universal Oil Prod Co Dewaxed lubricating oil production
US3894938A (en) † 1973-06-15 1975-07-15 Mobil Oil Corp Catalytic dewaxing of gas oils
US4061724A (en) * 1975-09-22 1977-12-06 Union Carbide Corporation Crystalline silica
US4229282A (en) * 1979-04-27 1980-10-21 Mobil Oil Corporation Catalytic dewaxing of hydrocarbon oils
US4419271A (en) * 1979-10-15 1983-12-06 Union Oil Company Of California Hydrocarbon conversion catalyst
US4309276A (en) † 1980-04-28 1982-01-05 Chevron Research Company Hydrocarbon conversion with low-sodium silicalite
US4292166A (en) * 1980-07-07 1981-09-29 Mobil Oil Corporation Catalytic process for manufacture of lubricating oils
US4428862A (en) * 1980-07-28 1984-01-31 Union Oil Company Of California Catalyst for simultaneous hydrotreating and hydrodewaxing of hydrocarbons
JPS5763134A (en) * 1980-07-28 1982-04-16 Union Oil Co Simultaneous hydrogenation dewaxing and hydrogenation treatment method for hydrocarbon and catalyst used for said method
US4347121A (en) * 1980-10-09 1982-08-31 Chevron Research Company Production of lubricating oils
US4325805A (en) * 1980-12-18 1982-04-20 Chevron Research Company Lubricating oil stabilization
US4361477A (en) * 1981-04-17 1982-11-30 Chevron Research Company Stabilizing and dewaxing lube oils
US4561967A (en) * 1981-04-23 1985-12-31 Chevron Research Company One-step stabilizing and dewaxing of lube oils
US4362653A (en) * 1981-04-27 1982-12-07 Uop Inc. Hydrocarbon conversion catalyst
US4428825A (en) * 1981-05-26 1984-01-31 Union Oil Company Of California Catalytic hydrodewaxing process with added ammonia in the production of lubricating oils
US4513090A (en) * 1981-07-09 1985-04-23 Exxon Research And Engineering Co. Crystalline silica zeolite-containing catalyst
US4443329A (en) * 1981-07-09 1984-04-17 Exxon Research And Engineering Co. Crystalline silica zeolite-containing catalyst and hydrocarbon hydroprocesses utilizing the same
US4394249A (en) * 1981-08-03 1983-07-19 Mobil Oil Corporation Catalytic dewaxing process
CA1203225A (en) * 1981-08-07 1986-04-15 Stephen M. Oleck Two-stage hydrocarbon dewaxing hydrotreating process
US4458024A (en) * 1982-02-08 1984-07-03 Mobil Oil Corporation Process for hydrotreating petroleum residua and catalyst therefor
US4490570A (en) * 1982-02-22 1984-12-25 Cosden Technology, Inc. Method for para selective alkylation employing silicalite catalysts
US4548705A (en) * 1982-03-09 1985-10-22 Union Oil Company Of California Hydrocracking with catalytically active amorphous silica and zeolites
US4599473A (en) * 1983-12-19 1986-07-08 Cosden Technology, Inc. Process for para selective alkylation of aromatic hydrocarbons
US4597854A (en) * 1985-07-17 1986-07-01 Mobil Oil Corporation Multi-bed hydrodewaxing process

Also Published As

Publication number Publication date
EP0233169A2 (de) 1987-08-19
US4810356A (en) 1989-03-07
JP2879793B2 (ja) 1999-04-05
EP0233169B2 (de) 2001-08-29
LU86288A1 (fr) 1987-09-10
JPS62246995A (ja) 1987-10-28
EP0233169A3 (en) 1989-02-22
DE3775426D1 (de) 1992-02-06

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