WO1988008749A1 - A method for controlled catalyst sulfidation - Google Patents

A method for controlled catalyst sulfidation Download PDF

Info

Publication number
WO1988008749A1
WO1988008749A1 PCT/SE1987/000235 SE8700235W WO8808749A1 WO 1988008749 A1 WO1988008749 A1 WO 1988008749A1 SE 8700235 W SE8700235 W SE 8700235W WO 8808749 A1 WO8808749 A1 WO 8808749A1
Authority
WO
WIPO (PCT)
Prior art keywords
catalyst
hydrogenation
nickel
catalyst sulfidation
catalysts
Prior art date
Application number
PCT/SE1987/000235
Other languages
French (fr)
Inventor
Gudmund Smedler
Robert KÖLBY
Original Assignee
Gudmund Smedler
Koelby Robert
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
Priority to SE8505403A priority Critical patent/SE450871B/en
Application filed by Gudmund Smedler, Koelby Robert filed Critical Gudmund Smedler
Priority to DE8787904353T priority patent/DE3778557D1/en
Priority to AT87904353T priority patent/ATE75163T1/en
Priority to JP87503946A priority patent/JPH02503395A/en
Priority to PCT/SE1987/000235 priority patent/WO1988008749A1/en
Priority to KR1019890700049A priority patent/KR950008198B1/en
Priority to EP87904353A priority patent/EP0367758B1/en
Publication of WO1988008749A1 publication Critical patent/WO1988008749A1/en
Priority to NO89890049A priority patent/NO890049L/en

Links

Classifications

    • CCHEMISTRY; METALLURGY
    • C11ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
    • C11CFATTY ACIDS FROM FATS, OILS OR WAXES; CANDLES; FATS, OILS OR FATTY ACIDS BY CHEMICAL MODIFICATION OF FATS, OILS, OR FATTY ACIDS OBTAINED THEREFROM
    • C11C3/00Fats, oils, or fatty acids by chemical modification of fats, oils, or fatty acids obtained therefrom
    • C11C3/12Fats, oils, or fatty acids by chemical modification of fats, oils, or fatty acids obtained therefrom by hydrogenation
    • C11C3/123Fats, oils, or fatty acids by chemical modification of fats, oils, or fatty acids obtained therefrom by hydrogenation using catalysts based principally on nickel or derivates
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01JCHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/70Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
    • B01J23/74Iron group metals
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01JCHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J27/00Catalysts comprising the elements or compounds of halogens, sulfur, selenium, tellurium, phosphorus or nitrogen; Catalysts comprising carbon compounds
    • B01J27/02Sulfur, selenium or tellurium; Compounds thereof
    • B01J27/04Sulfides
    • B01J27/047Sulfides with chromium, molybdenum, tungsten or polonium
    • B01J27/049Sulfides with chromium, molybdenum, tungsten or polonium with iron group metals or platinum group metals
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01JCHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J37/00Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
    • B01J37/20Sulfiding
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01JCHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J21/00Catalysts comprising the elements, oxides, or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium, or hafnium
    • B01J21/12Silica and alumina
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01JCHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/70Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
    • B01J23/74Iron group metals
    • B01J23/755Nickel

Definitions

  • Ni/Cu alloys have in some cases shown a remarkably higher selectivity than conventional nickel catalysts. A problem is , however, the surface enrichement of one of the components at elevated temperatures.
  • NiS, Ni 2 S and Ni 3 S 2 give a much higher selectivity in the hydrogenation of edible oils than nickel catalysts .
  • the present invention is concerned with a new and flexible method for an application specific optimal control of the degree of catalyst poisoning that could be directly used in the customers plant.
  • This method it is possible to tailor a catalyst that is optimal for the temporary feedstock and desired products, starting from a conventional nickel-catalyst.
  • TECHNIQUE The method is based on selective chemisorption, which in this case means that small amounts of H 2 S is added, through a certain number of pulses or at a low flow under a certain time, to a reactor where the main rection takes place.
  • H 2 S that is irreversibly adsorbed at moderate temperatures is hindered to adsorb everywhere on the catalyst surface, since a large fraction of the surface is covered by adsorbed reaction participants.
  • the method is making use of a mass transfer effect: At process conditions where the rate constants for hydrogenation as well as for H 2 S adsorption are very high, the observed rate will be entirely controlled by the external mass transfer rates of H 2 and H 2 S, respectively. The concentrations of these species at the catalyst surface (where the poisoning takes place) will then be yery much lower than the corresponding saturation concentrations, an effect that can be used for kinetic and thermodynamic control of the poisoning process.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Chemistry (AREA)
  • Materials Engineering (AREA)
  • General Chemical & Material Sciences (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Wood Science & Technology (AREA)
  • Catalysts (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

A Ni-containing catalyst is sulfidized by an addition of H2S to the liquid phase hydrogenation reactor during the hydrogenation of natural oils. The catalyst sulfidation will then occur simultaneously with the hydrogenation reaction.

Description

A Method for Controlled Catalyst Sulfidation.
Hydrogenation of carbon monoxide (Fischer-Tropsch-methanization and related processes) and of polyunsaturated organic compounds are old and well known examples of industrial large scale hydrogenation processes where the catalyst selectivity is of vital economic importance. If the yield of desired products could be maximized in the reactor, the waste of raw material resulting from the production of by-products of low value would be avoided. Furthermore (and perhaps more important) the energy consumption and capital costs of the separation equipment would be minimized. In the light of to-day's tendency on the energy market, energy craving unit operations such as distillation could be expected to carry an increasing fraction of the total costs of the process industry in the future. This tendency is also reflected in the intensified research activities in the fields of catalyst development and reactor design during the last 15 years.
The requirement of a high catalyst activity (high production capacity per unit of catalyst mass) is very often in conflict with the requirement of a high selectivity (high preference for certain desired reactions and low activity for other undesired reactions). Some typical examples of commercially important hydrogenation processes where the conflict between catalyst activity and selectivity is pronounced are
* partial hydrogenation of polyunsaturated natural triglycerides for production of fatty acids. Saturated triglycerides (stearin) are not preferable in this case.
* Partial hydrogenation of acetylene to ethene. Ethene is perhaps the most important of all petrochemical compounds, and is for instance the starting material in the manufacture of the plastics polyethene and PVC. The saturated hydrogenation product (ethane) could in itself only be used as a fuel. * Partial hydrogenation of 2-ethyl-hexenal to 2-ethyl-hexanal for the production of octanoic acid. The full-hydrogenated product (2-ethyl-hexanol) has quite different properties and is used for PVC-softeners. The development of selective catalysts has , in principal, been following the lines listed below
* Replacement of the active metal component. Palladium has, in contrast to nickel, appeared to be very selective in the hydrogenation of for example acetylene and unsaturated aldehydes. A change of the active component is often (as in this case ) associated with increased catalyst costs .
* Alloying of the active metal with another, less active, metal. Ni/Cu alloys have in some cases shown a remarkably higher selectivity than conventional nickel catalysts. A problem is , however, the surface enrichement of one of the components at elevated temperatures.
* Poisoning of the catalyst by means of a sulfur compound. Sulfur, that in general is causing severe problems through unwanted catalyst deactivation , can interact with metal catalysts and give rise to the formation of a new type of catalyst sites , with a substantially higher selectivity than the original ones . This technique must however be applied under rigorous control of the process conditions , as otherwise a total deactivation could take place. It is known since long ago that nickel/sulfur-catalysts
(NiS, Ni 2S and Ni3S2) give a much higher selectivity in the hydrogenation of edible oils than nickel catalysts .
In the past, elementary sulfur was added to the hydrogenation reactor in order to modify the nickel catalyst, but the results were in general hard to predict. Nowadays , Ni/S-catalysts are marketed and the results are more reproducible::
Higher selectivity and lower activity in comparison with ordinary nickel catalysts.
The problem for the process industry is that one is forced to choose one out of a limited number of catalysts that are sold on the market, at a cost that is drastically increasing when the requirements on the catalyst specifications increase.
The present invention is concerned with a new and flexible method for an application specific optimal control of the degree of catalyst poisoning that could be directly used in the customers plant. By this method, it is possible to tailor a catalyst that is optimal for the temporary feedstock and desired products, starting from a conventional nickel-catalyst. TECHNIQUE The method is based on selective chemisorption, which in this case means that small amounts of H2S is added, through a certain number of pulses or at a low flow under a certain time, to a reactor where the main rection takes place. H2S that is irreversibly adsorbed at moderate temperatures, is hindered to adsorb everywhere on the catalyst surface, since a large fraction of the surface is covered by adsorbed reaction participants. In addition, the method is making use of a mass transfer effect: At process conditions where the rate constants for hydrogenation as well as for H2S adsorption are very high, the observed rate will be entirely controlled by the external mass transfer rates of H2 and H2S, respectively. The concentrations of these species at the catalyst surface (where the poisoning takes place) will then be yery much lower than the corresponding saturation concentrations, an effect that can be used for kinetic and thermodynamic control of the poisoning process. EXPERIMENTAL METHOD
In a glass reactor provided with a turbine impeller was charged 400 ml of sunflower oil and 20 g of Ni-catalyst (82% Ni supported on an alumina-silica-carrier). The mixture was heated to 180°C under nitrogen atmosphere at a stirrer rate of 1200 r.p.m. before the hydrogenation was initiated. The hydrogen flow was 25 ml/s (1 atm, 25°C) during the poisoning process. By means of a gas dosing loop of known volume (5.43 ml) different amounts of H2S were introduced to a mixing flask, from where the main hydrogen flow was carrying the H2S into the hydrogenation reactor. The results from the different poisoning experiments were continuously monitored by means of an on-line flamephotomultiplicator detector that made possible a fast and easy determination of the H2S-uptake of the catalyst. The hydrogenation time was in all cases 70 minutes , no matter the amount of H2S added.
By the method just described, 8 different catalyst samples were prepared through the addition of 4, 8, 10, 15, 20, 25, 34, and 60 loops of H2S , respectively. From each one of these samples , 0.12 g of catalyst was withdrawn for activity and selectivity tests in a slurry reactor operating under kinetic conditions (eliminated mass transfer limitations) . The conditions in the slurry reactor were: PH2 = 5.0 atm, Temp.= 180°C . Hydrogen flow rate = 5 ml/s ( 1 atm. 25°C ) , catalyst loading = 0.12 g and stirrer rate 1800 r.p.m. As references , the unpoisoned nickel catalyst and a commercially available Ni/S-catalyst with the same Ni contents, were used.
The results , that are summarized in appendix 1 , show that the maximum concentration of mono-unsaturated fatty acid is practically independent of the degree of poisoning, while the trans/cis-ratio of the mono-unsaturated fatty acid is directly related to the degree of poisoning. Morever , the same table indicates that the activities of our Ni/S-catalysts are in all cases significantly higher than is the activity of the commercial Ni/S-catalyst, although the Ni-contents are the same.
To summarize, it is clearly demonstrated that our method provides an easy way to modify the conventional nickel catalyst in such a way that its selectivity is drastically increased while the activity is still much higher than that of the commercially available Ni/S-catalyst . In addition , it is also shown that the method makes it possible to poison a limited fraction of the catalyst surface, an aspect that makes the method flexible for varying operational conditions in the plant. Appendix 1.
Selectivity vs. sulphur treatment severity. Distribution of mono-unsaturated isomeres. Loops added cis trans 18:1 total
(H2S)
0 13.48 57.22 70.7
10 7.67 59.87 67.54 20 - 67.52 67.52 25 - 68.23 68.23 34 - 70.03 70.03 60 _ 71.49 71.49
Commercial - 71.93 71.93 NiS-catalyst
note 1. The composition is given in mole percentages. note 2. All hydrogenations performed at 5 bar 180°C.
Activity comparison of the samples above, expressed as initial rate of reaction.
Loops added robs/mol.mL -3 ·s-1
(H2S) (activity)
0 1.691
10 0.454
20 0.429 25 0.342
34 0.231
60 0.235
Commercial 0.103 NiS-catalyst

Claims

CLAIM
A method for controlled catalyst sulfidation, c h a r a cte r i z e d by:
Sulfiding of nickel-containing catalysts through the addition of H2S to a liquid phase hydrogenation reactor during hydrogenation of natural oils, thereby causing the catalyst sulfidation to occur simultaneously with the hydrogenation reaction.
PCT/SE1987/000235 1985-11-15 1987-05-13 A method for controlled catalyst sulfidation WO1988008749A1 (en)

Priority Applications (8)

Application Number Priority Date Filing Date Title
SE8505403A SE450871B (en) 1985-11-15 1985-11-15 Controlled partial sulphiding method for nickel catalyst
DE8787904353T DE3778557D1 (en) 1985-11-15 1987-05-13 METHOD FOR CONTROLLED SULFURATION OF THE CATALYST.
AT87904353T ATE75163T1 (en) 1985-11-15 1987-05-13 PROCESS FOR THE CONTROLLED SULFATION OF THE CATALYST.
JP87503946A JPH02503395A (en) 1985-11-15 1987-05-13 Controlled catalytic sulfidation method
PCT/SE1987/000235 WO1988008749A1 (en) 1985-11-15 1987-05-13 A method for controlled catalyst sulfidation
KR1019890700049A KR950008198B1 (en) 1987-05-13 1987-05-13 A method for controlled catalyst sulfidation
EP87904353A EP0367758B1 (en) 1985-11-15 1987-05-13 A method for controlled catalyst sulfidation
NO89890049A NO890049L (en) 1985-11-15 1989-01-06 PROCEDURE FOR CONTROLLED SULFIDATION OF CATALYST.

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
SE8505403A SE450871B (en) 1985-11-15 1985-11-15 Controlled partial sulphiding method for nickel catalyst
PCT/SE1987/000235 WO1988008749A1 (en) 1985-11-15 1987-05-13 A method for controlled catalyst sulfidation

Publications (1)

Publication Number Publication Date
WO1988008749A1 true WO1988008749A1 (en) 1988-11-17

Family

ID=26659145

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/SE1987/000235 WO1988008749A1 (en) 1985-11-15 1987-05-13 A method for controlled catalyst sulfidation

Country Status (7)

Country Link
EP (1) EP0367758B1 (en)
JP (1) JPH02503395A (en)
AT (1) ATE75163T1 (en)
DE (1) DE3778557D1 (en)
NO (1) NO890049L (en)
SE (1) SE450871B (en)
WO (1) WO1988008749A1 (en)

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0564317A1 (en) * 1992-04-01 1993-10-06 EUROPEENNE DE RETRAITEMENT DE CATALYSEURS (en abrégé EURECAT) Process for presulfurizing a catalyser for treating hydrocarbons
FR2755379A1 (en) * 1996-11-07 1998-05-07 Inst Francais Du Petrole A new method for the sulphuration of hydrotreatment catalysts containing a group VI and/or a group VIII metal(s)

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS63165344A (en) * 1986-12-26 1988-07-08 Chisso Corp Optically active-2-methylbytrates and utilized substance thereof

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB1000829A (en) * 1962-03-27 1965-08-11 California Research Corp In situ sulfiding of nickel- and/or cobalt-containing catalysts
DE2406024B2 (en) * 1973-02-16 1976-03-18 Universal Oil Products Co., Des Piaines, 111. (V.St.A.) CATALYST, METHOD FOR MANUFACTURING IT AND ITS USE
SE384453B (en) * 1972-01-20 1976-05-10 Unilever Nv PROCEDURE FOR THE PREPARATION OF A PARTIALLY SULFIDATED CARRIED METAL CATALYST
DE2824125B2 (en) * 1977-06-21 1979-07-19 Labofina S.A., Bruessel Process for the preparation of a sulfur-containing nickel catalyst
EP0064429B1 (en) * 1981-04-09 1985-06-19 Institut Français du Pétrole Process for the hydrotreatment of a hydrocarbon feed in the presence of a presulphurised catalyst

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB1000829A (en) * 1962-03-27 1965-08-11 California Research Corp In situ sulfiding of nickel- and/or cobalt-containing catalysts
SE384453B (en) * 1972-01-20 1976-05-10 Unilever Nv PROCEDURE FOR THE PREPARATION OF A PARTIALLY SULFIDATED CARRIED METAL CATALYST
DE2406024B2 (en) * 1973-02-16 1976-03-18 Universal Oil Products Co., Des Piaines, 111. (V.St.A.) CATALYST, METHOD FOR MANUFACTURING IT AND ITS USE
DE2824125B2 (en) * 1977-06-21 1979-07-19 Labofina S.A., Bruessel Process for the preparation of a sulfur-containing nickel catalyst
EP0064429B1 (en) * 1981-04-09 1985-06-19 Institut Français du Pétrole Process for the hydrotreatment of a hydrocarbon feed in the presence of a presulphurised catalyst

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0564317A1 (en) * 1992-04-01 1993-10-06 EUROPEENNE DE RETRAITEMENT DE CATALYSEURS (en abrégé EURECAT) Process for presulfurizing a catalyser for treating hydrocarbons
FR2689420A1 (en) * 1992-04-01 1993-10-08 Eurecat Europ Retrait Catalys Process for presulfiding hydrocarbon processing catalyst
US5397756A (en) * 1992-04-01 1995-03-14 Europeenne De Retraitement De Catalyseurs (Eurecat) Process for the presulphurization of hydrocarbon treatment catalysts
CN1040071C (en) * 1992-04-01 1998-10-07 欧洲催化剂加工公司 Process for the presulphurization of hydrocarbon treatment catalysts
FR2755379A1 (en) * 1996-11-07 1998-05-07 Inst Francais Du Petrole A new method for the sulphuration of hydrotreatment catalysts containing a group VI and/or a group VIII metal(s)

Also Published As

Publication number Publication date
SE8505403D0 (en) 1985-11-15
SE450871B (en) 1987-08-10
NO890049D0 (en) 1989-01-06
NO890049L (en) 1989-01-06
JPH02503395A (en) 1990-10-18
EP0367758A1 (en) 1990-05-16
DE3778557D1 (en) 1992-05-27
ATE75163T1 (en) 1992-05-15
SE8505403L (en) 1987-05-16
EP0367758B1 (en) 1992-04-22

Similar Documents

Publication Publication Date Title
US2511453A (en) Catalyst and process for carrying out hydrogenation reactions
EP0174836B1 (en) Solid strong acid catalyst
Parshall et al. Organometallic chemistry and catalysis in industry
JPS62184100A (en) Continuous hydrogenation of fat, fatty acid and fatty acid derivative
US2574445A (en) Catalytic desulfurization of kerosene and white spirits
EP0079132B1 (en) Process for the production of oxygenated hydrocarbons by the catalytic conversion of synthesis gas
US4251672A (en) Process for hydrogenating organic compounds with coprecipitated copper-nickel-silica catalysts
EP0367758B1 (en) A method for controlled catalyst sulfidation
US2143364A (en) Process for effecting catalytic reactions
US4153671A (en) Catalytic gas purification process
EP0777636A1 (en) Process for the production of cyclohexane
US3239454A (en) Selective multistage hydrogenation of hydrocarbons
US3691063A (en) Residual fuel oil hydrocracking process
EP0011906A1 (en) Process for selective hydrogenation of dienes in pyrolysis gasoline
KR950008198B1 (en) A method for controlled catalyst sulfidation
CN1016165B (en) Catalyzer rich in macropores for selectively hydrogenating olefinic hydrocarbon
KR910004885B1 (en) Process for the production of edible oils
US3851001A (en) Hydrogenation of aromatic hydrocarbons to the corresponding saturated hydrocarbon
US3769358A (en) Hydrogenation process start-up method
US3692864A (en) Hydrogenation process utilizing homogeneous metal catalysts
US3160579A (en) Hydrogenation process
JPS59105083A (en) Selective hydrogenation for diene in pyrolized gasoline
Lloyd et al. Hydrogenation catalysts
JP2003212800A (en) Method for producing decalin by hydrogenating naphthalene
US2709714A (en) Production of oxo alcohols

Legal Events

Date Code Title Description
AK Designated states

Kind code of ref document: A1

Designated state(s): AU BG BR DK FI HU JP KR NO RO US

AL Designated countries for regional patents

Kind code of ref document: A1

Designated state(s): AT BE CH DE FR GB IT LU NL

WWE Wipo information: entry into national phase

Ref document number: 1987904353

Country of ref document: EP

WWP Wipo information: published in national office

Ref document number: 1987904353

Country of ref document: EP

WWG Wipo information: grant in national office

Ref document number: 1987904353

Country of ref document: EP