AU682239B2 - Creation of Inventions and Patents with Artificial Intelligence

AU682239B2 – Process for the catalytic partial oxidation of hydrocarbons
– Google Patents

AU682239B2 – Process for the catalytic partial oxidation of hydrocarbons
– Google Patents
Process for the catalytic partial oxidation of hydrocarbons

Download PDF
Info

Publication number
AU682239B2

AU682239B2
AU13173/95A
AU1317395A
AU682239B2
AU 682239 B2
AU682239 B2
AU 682239B2
AU 13173/95 A
AU13173/95 A
AU 13173/95A
AU 1317395 A
AU1317395 A
AU 1317395A
AU 682239 B2
AU682239 B2
AU 682239B2
Authority
AU
Australia
Prior art keywords
process according
catalyst
range
feed
partial oxidation
Prior art date
1993-12-27
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.)

Ceased

Application number
AU13173/95A
Other versions

AU1317395A
(en

Inventor
Krijn Pieter De Jong
Ronald Jan Schoonebeek
Koert Alexander Vonkeman
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.)

Shell Internationale Research Maatschappij BV

Original Assignee
Shell Internationale Research Maatschappij BV
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.)
1993-12-27
Filing date
1994-12-22
Publication date
1997-09-25

1994-12-22
Application filed by Shell Internationale Research Maatschappij BV
filed
Critical
Shell Internationale Research Maatschappij BV

1995-07-17
Publication of AU1317395A
publication
Critical
patent/AU1317395A/en

1997-09-25
Application granted
granted
Critical

1997-09-25
Publication of AU682239B2
publication
Critical
patent/AU682239B2/en

2014-12-22
Anticipated expiration
legal-status
Critical

Status
Ceased
legal-status
Critical
Current

Links

Espacenet

Global Dossier

Discuss

Classifications

C—CHEMISTRY; METALLURGY

C01—INORGANIC CHEMISTRY

C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C

C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen

C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen

C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air

C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents

C01B3/38—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts

C01B3/40—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts characterised by the catalyst

C—CHEMISTRY; METALLURGY

C01—INORGANIC CHEMISTRY

C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C

C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen

C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen

C01B3/386—Catalytic partial combustion

C—CHEMISTRY; METALLURGY

C01—INORGANIC CHEMISTRY

C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C

C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas

C01B2203/10—Catalysts for performing the hydrogen forming reactions

C01B2203/1005—Arrangement or shape of catalyst

C01B2203/1011—Packed bed of catalytic structures, e.g. particles, packing elements

C—CHEMISTRY; METALLURGY

C01—INORGANIC CHEMISTRY

C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C

C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas

C01B2203/10—Catalysts for performing the hydrogen forming reactions

C01B2203/1005—Arrangement or shape of catalyst

C01B2203/1023—Catalysts in the form of a monolith or honeycomb

C—CHEMISTRY; METALLURGY

C01—INORGANIC CHEMISTRY

C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C

C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas

C01B2203/10—Catalysts for performing the hydrogen forming reactions

C01B2203/1005—Arrangement or shape of catalyst

C01B2203/1029—Catalysts in the form of a foam

C—CHEMISTRY; METALLURGY

C01—INORGANIC CHEMISTRY

C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C

C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas

C01B2203/10—Catalysts for performing the hydrogen forming reactions

C01B2203/1041—Composition of the catalyst

C01B2203/1047—Group VIII metal catalysts

C—CHEMISTRY; METALLURGY

C01—INORGANIC CHEMISTRY

C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C

C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas

C01B2203/10—Catalysts for performing the hydrogen forming reactions

C01B2203/1041—Composition of the catalyst

C01B2203/1047—Group VIII metal catalysts

C01B2203/1064—Platinum group metal catalysts

C—CHEMISTRY; METALLURGY

C01—INORGANIC CHEMISTRY

C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C

C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas

C01B2203/10—Catalysts for performing the hydrogen forming reactions

C01B2203/1041—Composition of the catalyst

C01B2203/1082—Composition of support materials

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

Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS

Y02P20/00—Technologies relating to chemical industry

Y02P20/50—Improvements relating to the production of bulk chemicals

Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts

Abstract

This invention concerns a process for the catalytic partial oxidation of a hydrocarbon feedstock. The process comprises contacting a feed mixture comprising the hydrocarbon feedstock and an oxygen-containing gas, which feed mixture also comprises nitrogen, with a catalyst capable of catalyzing the partial oxidation of the hydrocarbon feedstock, wherein the feed mixture also comprises a sulfur-containing compound. This process allows sulfur-containing hydrocarbon feedstocks to be processed without first undergoing a sulfur removal treatment. Accordingly, a process for the preparation of carbon monoxide and/or hydrogen from a hydrocarbon feedstock comprises subjecting the hydrocarbon feedstock in a first stage to a catalytic partial oxidation process as described above and subjecting at least a portion of the product of the first stage in a second stage to a desulfurization process.

Description

C~ q p -P C I WO 95/18062 PCT/EP94/04270 1 PROCESS FOR THE CATALYTIC PARTIAL OXIDATION OF HYDROCARBONS The present invention relates to a process for the catalytic partial oxidation of hydrocarbons, in particular to a process for the preparation of a mixture of carbon monoxide and hydrogen from methane, natural gas, associated gas or other sources of light hydrocarbons.
The partial oxidation of hydrocarbons, for example methane or natural gas, in the presence of a catalyst is an attractive route for the preparation of mixtures of carbon monoxide and hydrogen, known in the art as synthesis gas. The partial oxidation of a hydrocarbon is a highly exothermic reaction and, in the case in which methane is the hydrocarbon, proceeds by the following reaction: 2CH 4 0 2 2CO 4H 2 The optimum catalytic partial oxidation process for application on a commercial scale would give high yields of carbon monoxide and hydrogen at elevated pressures, for example about 30 bar, and very high space velocities, for example of the order of 1,000,000 Nl/kg/h. For thermodynamic reasons, in order to obtain high yields of ccrbon monoxide and hydrogen under these process conditions, it is necessary to operate the partial oxidation process at high temperatures.
The literature contains a number of documents disclosing details of experiments conducted into the catalytic partial oxidation of hydrocarbons, in particular methane, employing a wide range of catalysts. The majority of these experiments, however, have been conducted under very mild conditions or under conditions wholly unsuited to the operation of a commercial catalytic partial oxidation process.
Thus, European Patent Application publication No. 0 303 438 (EP-A-0 303 438) discloses a process for the catalytic partial oxidation of a hydrocarbonaceous feedstock in which a gaseous a, IL rpl-~er WO 95/18062 PCT/EP94/04270 2 mixture of the hydrocarbonaceous feedstock, oxygen or an oxygen-containing gas and, optionally, steam, is introduced into a catalytic partial oxidation zone to contact a catalyst retained therein. The catalyst employed in the process may comprise a wide range of catalytically active components, for example palladium, platinum, rhodium, iridium, osmium, ruthenium, nickel, chromium, cobalt, cerium, lanthanum and mixtures thereof. Further, it is stated in EP-A-0 303 438 that materials not normally considered to be catalytically active may also be employed as catalysts, for example refractory oxides such as cordierite, mullite, mullite aluminium titanate, zirconia spinels and alumina. The catalyst may be of a variety of forms, for example sheets of corrugated metal packed to form elongate channels therethrough or wire mesh.
However, preference is given in EP-A-0 303 438 to the use of catalysts in the form of monoliths.
European Patent No. 0 262 947 (EP-B-0 262 947) discloses a process for generating hydrogen by the partial oxidation of a hydrocarbon in which a mixture of the hydrocarbon and oxygen is injected into a mass of a catalyst. The catalyst disclosed in EP-B-0 262 947 comprises platinum and chromium oxide supported on a refractory solid.
D.A. Hickman and L.D. Schmidt (“Synthesis Gas Formation by Direct Oxidation of Methane over Pt Monoliths”, Journal of Catalysis 138, 267-282, 1992)) have conducted experiments into the partial oxidation of methane in the presence of catalysts comprising either platinum or rhodium. The catalysts employed were in the form of a polycrystalline platinum foil or rhodium or platinum supported on a ceramic foam carrier. The partial oxidation reactions were conducted at substantially atmospheric pressure and at temperatures in the range of from 600 to 1500 K (337 to 1237 A.T Ashcroft et al. (“Selective oxidation of methane to synthesis gas using transition metal catalysts”, Nature, vol. ‘4, No. 6264, pages 319 to 321, 22nd March, 1990) disclose the partial oxidation of methane to synthesis gas in the presence of a range of ruthenium-containing catalysts. The objective of the experiments ~I I I= ~Bs~ C WO 95/18062 PCT/EP94/04270 3 was to establish that the partial oxidation process could be carried out under mild conditions and at low temperatures. To this end, the experiments were conducted with a low gas hourly space velocity of 40,000 /hr, a pressure of 1 atmosphere and a temperature of about 777 A single experiment is reported in which elevated pressures were applied. However, in this case, a large excess of methane was used in order to avoid the risk of explosions.
P.D.F. Vernon et al. (“Partial Oxidation of methane to Synthesis Gas”, Catalysis Letters 6 (1990) 181-186) disclose a range of experiments in which catalysts comprising nickel, ruthenium, rhodium, palladium, iridium or platinum, either supported on alumina or present in mixed oxide precursors, were applied. Again, the experiments reported are limited to a catalytic partial oxidation process employing only mild operating conditions. As a basis, a set of mild reaction conditions were selected: a pressure of 1 atmosphere, a gas hourly space velocity of 40,000 /hr, a temperature of 1050 K (777 and a methane/oxygen ratio of 2.0. From this basis, each of the process parameters was explored. From this study it was concluded that the low temperature operation gave certain operating advantages, but was only practicable at pressures of the order of 1 atmosphere. The authors report the same experiments in “Partial Oxidation of Methane to Synthesis Gas, and Carbon Dioxide as an Oxidising Agent for Methane Conversion”, Catalysis Today, 13 (1992) 417-426.
R.H. Jones et al. (“Catalytic Conversion of Methane to Synthesis Gas over Europium Iridate, Eu2Ir 2 0 7 Catalysis Letters 8 (1991) 169-174) report the selective partial oxidation of methane using the europium iridium pyrochlore Eu2Ir 2 0 7 The reaction was studied under the mild conditions of a pressure of 1 atmosphere and a temperature of 873 K (600 J.K. Hockmuth (“Catalytic Partial Oxidation of Methane over a monolith Supported Catalyst”, Applied Catalysis B: Environmental, 1 (1992) 89-100) reports the catalytic partial oxidation of methane using a catalyst comprising a combination of platinum and palladium supported on a cordierite monolith body.
-I -I I c- WO 95/18062 PCT/EP94/04270 -4 United States Patent No. 5,149,464 (US-A-5,149,464) is directed to a method for selectively oxygenating methane to carbon monoxide and hydrogen by bringing the reactant gas mixture at a temperature of about 650 °C to 900 “C into contact with a solid catalyst which is generally described as being either: a) a catalyst of the formula MxM’yOz, where: M is at least one element selected from Mg, B, Al, Ln, Ga, Si, Ti, Zr and Hf; Ln is at least one member of lanthanum and the lanthanide series of elements; M’ is a d-block transition metal, and each of the ratios x/y and y/z and is independently from 0.1 to 8; or b) an oxide of a d-block transition metal; or c) a d-block transition metal on a refractory support; or d) a catalyst formed by heating a) or b) under the conditions of the reaction or under non-oxidising conditions.
The d-block transition metals are said in US-A-5,149,464 to be selected from those having atomic number 21 to 29, 40 to 47 and 72 to 79, the metals scandium, titanium, vanadium, chromium, manganese, iron, cobalt, nickel, copper, zirconium, niobium, molybdenum, technetium, ruthenium, rhodium, palladium, silver, hafnium, tantalum, tungsten, rhenium, osmium, iridium, platinum and gold. It is stated in US-A-5,.149,464 that the preferred metals are those in Group VIII of the Periodic Table of the Elements, that is iron, osmium, cobalt, rhenium, iridium, palladium platinum, nickel and ruthenium.
The process described in US-A-5,149,464 is operated at a temperature in the range of from 650 *C to 900 with a range of from 700 °C to 800 °C being preferred. A range of experiments are described in US-A-5,149,464 in which a variety of catalysts comprising Group VIII metals were tested, including ruthenium oxide, praesidium/ruthenium oxides, pyrochlores, ruthenium on alumina, rhodium on alumina, palladium on alumina, platinum on alumina, nickel/aluminium oxide, perovskites and nickel oxide.
A similar general disclosure of a catalyst for use in the catalytic partial oxidation process is made in International Patent s 0 I L WO 95/18062 PCT/EP94/04270 5 Application publication No. WO 92/11199. WO 92/11199 specifically discloses experiments in which catalysts comprising iridium, palladium, ruthenium, rhodium, nickel and platinum supported on alumina were applied. All the experiments were conducted under mild process conditions, with typical conditions being a pressure of 1 atmosphere, a temperature of 1050 K (777 and a gas hourly space velocity of about 20,000 /hr.
As discussed hereinbefore, to be effective on a commercial scale, the catalytic partial oxidation process would need to operate at elevated pressures and at high temperatures. It has now been found that, when operated under the conditions demanded of a commercial process, the catalytic partial oxidation of hydrocarbons can, in the presence of nitrogen, yield a synthesis gas product containing a number of by-products, in particular ammonia (NH 3 and hydrogen cyanide (HCN), in low but significant amounts. It has been found that such by-products can adversely affect downstream processes to convert the carbon monoxide and/or hydrogen produced by the catalytic partial oxidation process, e.g. in the case of Fischer-Tropsch synthesis or of the commercial synthesis of methanol. The presence of by-products, in particular ammonia or hydrogen cyanide in the products of the catalytic partial oxidation process is thus undesirable.
Nitrogen is present in many natural gas feedstocks. Further, the preparation of pure, nitrogen-free oxygen on a commercial scale is both technically complex and very expensive. Accordingly, there is a need for a process for the catalytic partial oxidation of hydrocarbons when nitrogen is present during the partial oxidation reactions which may be applied on a commercial scale to produce a product of carbon monoxide and/or hydrogen containing a minimum of components such as ammonia and hydrogen cyanide.
Surprisingly, it has been found that the inclusion of sulphur or sulphur-containing compounds in the feed to the catalytic partial oxidation process significantly reduces the amounts of ammonia and hydrogen cyanide produced. Accordingly, the present invention provides a process for the catalytic partial oxidation of a LI s IB ~s9~ I WO 95/18062 PCT/EP94/04270 6 hydrocarbon feedstock, which process comprises contacting a feed mixture comprising the hydrocarbon feedstock and an oxygen-containing gas, which feed mixture also comprises nitrogen, with a catalyst capable of catalysing the partial oxidation of the hydrocarbon feedstock, wherein the feed mixture also comprises a sulphur-containing compound.
The process of the present invention may be used to prepare carbon monoxide and/or hydrogen from any gaseous hydrocarbon or hydrocarbon having a low boiling point such that it is gaseous under the conditions prevailing during the partial oxidation reactions.
The process is particularly suitable for the partial oxidation of methane, natural gas, associated gas or other sources of light hydrocarbons. In this respect, the term “light hydrocarbons” is a reference to hydrocarbons having from 1 to 5 carbon atoms. The process may be applied in the conversion of naturally occurring reserves of methane which contain a substantial amount of carbon dioxide. The feed preferably comprises methane in an amount of at least 50% by volume, more preferably at least 75% by volume, especially at least 80% by volume.
The hydrocarbon feedstock is contacted with an oxygen-containing gas during the partial oxidation process. Air may be used as the oxygen-containing gas, in which case nitrogen will be present in the feed and reaction mixture in large quantities.
Alternatively, the use of substantially pure oxygen may be preferred, in which case nitrogen may be present in much lower, but nevertheless significant, quantities. Typically, the substantially pure oxygen is prepared on a commercial scale by the distillation of liquified air. The amount of nitrogen present in the substantially pure oxygen will depend upon the operating conditions of the air distillation process. It is an advantage of the the process of the present invention that the tolerances of the air distillation process may be relaxed, thereby allowing a greater amount of nitrogen to be present in the substantially pure oxygen being used in the catalytic partial oxidation process. This, in turn, offers ~P IC~B1C 8-P~I~B ~I I WO 95/18062 PCT/EP94/04270 7 advantages in terms of a reduction in the overall capital and operating costs of the air distillation plant.
The feed may optionally comprise steam.
The feed may comprise the hydrocarbon feedstock and oxygen in an amount sufficient to give a suitable oxygen-to-carbon ratio.
Preferably, the oxygen-to-carbon ratio is in the range of from 0.3 to 0.8, more preferably from 0.45 to 0.75. References to the oxygen-to-carbon ratio refer to the ratio of oxygen in the form of molecules (02) to carbon atoms present in the hydrocarbon feedstock.
Preferably, the oxygen-to-carbon ratio is in the range of from 0.45 to 0.70, with oxygen-to-carbon ratios of the stoichiometric ratio, that is in the range of from 0.45 to 0.65, being particularly suitable.
If steam is present in the feed, the steam-to-carbon ratio (that is the ratio of molecules of steam (H 2 0) to carbon atoms in the hydrocarbon) is preferably in the range of from above 0.0 to more preferably from above 0.0 to The gaseous mixture contacted with the catalyst in the process of this invention comprises a sulphur-containing compound. The mixture may comprise one or a plurality of sulphur-containing compounds. Any suitable sulphur-containing compound may be employed which does not give rise to a significant adverse effect to the performance of the partial oxidation reaction when present in the required amount. Both organic and inorganic sulphur-containing compounds may be employed. Suitable inorganic sulphur compounds include hydrogen sulphide, carbonyl sulphide, carbon disulphide.
Suitable organic sulphur-containing compounds include the thiophenes, mercaptans and sulphides. A most suitable sulphur-containing compound is tetrahydrothiophene. If natural gas or associated gas are being employed, sulphur-containing compounds may be present in the gas as it-is produced from the reservoir.
Such sulphur-containing hydrocarbon feedstocks may conveniently be used as a feed to the process of the present invention without first undergoing a desulphurisation treatment, such as is conventionally applied.
I I IB~ r I~ -~qp ly~qlbp~pl WO 95/18062 PCT/EP94/04270 -8- The sulphur-containing compound should be present in the feed mixture in a sufficient concentration to reduce the formation of ammonia and hydrogen cyanide. However, the quantity of the sulphur-containing compound should not be so great as to significantly reduce either the activity or the selectivity of the catalyst being employed. Thus, the sulphur-containing compound is preferably present in the feed mixture in an amount to give a sulphur content in the range of from 0.05 to 100 ppm, more preferably from 0.1 to 50 ppm, especially from 0.1 to 10 ppm.
Hydrocarbon feedstocks used directly from naturally occurring reservoirs in which the sulphur content is significantly above the aforementioned upper limits may preferably be subjected to a partial sulphur removal treatment before being employed in the process of this invention.
The hydrocarbon feedstock, oxygen and its associated gases, the sulphur-containing compound and the steam, if present, are preferably well mixed prior to being contacted with the catalyst.
The process of the present invention may be operated at any suitable pressure. Preferably, the process of the present invention is operated at elevated pressures, that is pressures significantly above atmospheric pressure. The process may be operated at pressures in the range of up to 150 bar. Preferably, the operating pressure is in the range of from 2 to 125 bar, more preferably from 3 to 100 bar.
The process may be operated at any suitable temperature.
However, under the conditions of high pressure prevailing in the process, it is necessary to allow the feed gases to contact the catalyst at elevated temperatures in order to achieve the level of conversion required for a commercial scale operation. Accordingly, the process is preferably operated at a temperature of at least 950 Preferably, the operating temperature is in the range of from 950 to 1300 -more preferably in the range of from 950 to 1200 Temperatures in the range of from 1000 to 1200 “C are particularly suitable.
i 19′ 1 -~I WO 95/18062 PCT/EP94/04270 9 The feed mixture may be provided during the process at any suitable gas space velocity. It is an advantage of the process of the present invention that very high gas space velocities may be applied. Thus, typical space velocities for the process (expressed as normal litres of gas per kilograr.nme of catalyst per hotL are in the range of from 20,000 to 100,000,000 Nl/kg/hr, more preferably in the range of from 50,000 to 50,000,000 Nl/kg/hr. Space velocities in the range of from 500,000 to 30,000,000 Nl/kg/hr are particularly suitable.
Catalyst compositions suitable for use in the catalytic parti>i.
oxidation of hydrocarbons are known in the art. Preferred catalysts for use in the process of the present invention comprise, as the catalytically active component, a metal selected from Group VIII of the Periodic Table of the Elements. References in this specification to the Periodic Table of the Elements are to the CAS version, as published in the CRC Handbook of Chemistry and Physics, 68th Edition. Preferred catalysts for use in the process comprise a metal selected from ruthenium, rhodium, palladium, osmium, iridium and platinum. Catalysts comprising ruthenium, rhodium or iridium as the catalytically active metal are most suitable for use in the process.
The catalytically active metal is most suitably supported on a carrier. Suitable carrier materials are well known in the art and include the refractory oxides, such as silica, alumina, titania, zirconia and mixtures thereof. Mixed refractory oxides, that is refractory oxides comprising at least two cations may also be employed as carrier materials for the catalyst.
The catalytically active metal may be deposited on the refractory oxide carrier by techniques well known in the art. A most suitable technique for depositing the metal on the carrier is impregnation, which technique typically comprises contacting the carrier material with a solution of a compound of the catalytically active metal, followed by drying and calcining the resulting material.
L~L~ ~s L L C~PI WO 95/18062 PCT/EP94/04270 10 The catalyst may comprise the catalytically active metal in any suitable amount to achieve the required level of activity.
Typically, the catalyst comprises the active metal in an amount in the range of from 0.01 to 20% by weight, preferably from 0.02 to by weight, more preferably from 0.1 to 7.5% 5y weight.
Any suitable reaction regime may be applied in the process of the present invention in order to contact the reactants with the catalyst. One suitable regime is a fluidised bed, in which the catalyst is employed in the form of particles fluidised by a stream of gas. A preferred reaction regime for use in the process is a fixed bed reaction regime, in which the catalyst is retained within a reaction zone in a fixed arrangement. Particles of catalyst may be employed in the fixed bed regime, retained using fixed bed reaction techniques well known in the art. Alternatively, the fixed arrangement may comprise the catalyst in the form of a monolithic structure. A most preferred monolithic structure comprises a ceramic foam. Suitable ceramic foams kor use in the process are available commercially. Further, alternative forms for the catalyst include refractory oxide honeycomb monolith structures.
In a preferred embodiment of the process of this invention, the feed is contacted with a catalyst retained in a fixed arrangement, which arrangement has a high tortuosity. The term “tortuosity” is a common term in the art which, when referring to a fixed catalyst bed, can be defined as the ratio of the length of the path taken by a gas flowing through the bed to the length of the shortest straight line path through the bed. Thus, the honeycomb monolith structures have a tortuosity of 1.0. For the purposes of the present invention, the term “high tortuosity” is a reference to arrangements having a tortuosity substantially greater than that of the honeycomb monolith structures, in particular a tortuosity of at least 1.1. A fixed bed of catalyst particles typically has a tortuosity of whilst ceramic foams may be prepared having a tortuosity in the range of from 3.0 to 4.0, or even higher. In general, the tortuosity of the fixed bed arrangement is preferably in the range r ~L B~PT~U- WO 95/18062 PCT/EP94/04270 11 of from 1.1 to 10.0, more preferably to 5.0. A most suitable range of tortuosity is from 1.3 to It has been found that by employing the catalyst in a fixed bed arrangement having a high tortuosity allows the required conversion to be achieved with only a relatively very short contact time between the reacting gases and the catalyst. In this way, only a very low volume of catalyst is required, which in turn allows the very high gas space velocities of the present process to be easily achieved on a commercial scale.
It is a further preferred feature of the process of this invention that the catalyst is retained in the form of a fixed arrangement having a large number of pores. In this respect, the term “pore” is a general reference to a space or interstice in the fixed arrangement between two adjacent portions of the catalyst.
Thus, in the case of a fixed bed of catalyst particles, the term “pore” refers to the space between two adjacent pPrticles. When referring to ceramic foams, the term pore refers to the openings or spaces between adjacent portions or lands of the ceramic structure.
Thus, it will be appreciated that the pores referred to in respect of the present invention have a nominal diameter of the order of magnitude of 0.1 mm. These are to be contrasted with pores which may be present in the catalyst support material itself, which may be porous.
The fixed arrangement comprises at least 750 pores per square centimetre. Preferably, the fixed arrangement comprises from about 1000 to about 15000 pores per square centimetre, more preferably from about 1250 to about 10000 pores per square centimetre.
The gaseous mixture of the hydrocarbon feedstock and the oxygen-containing gas are preferably contacted with the catalyst under adiabatic conditions. For the purposes of this specification, the term “adiabatic” is a reference to reaction conditions in which substantially all heat loss and radiation from the reaction zone is prevented, with the exception of heat leaving in the gaseous effluent stream of the reactor.
I~ I ~QIIC- Lt~~ C -p WO 95/18062 PCT/EP94/04270 12 In a further aspect, the present invention relates to carbon monoxide or hydrogen whenever prepared by a process as hereinbefore described.
The mixture of carbon monoxide and hydrogen prepared by the process of this invention is particularly suitable for use in the synthesis of hydrocarbons, for example by means of the Fischer-Tropsch synthesis, or the synthesis of oxygenates, for example methanol. Processes for the conversion of the mixture of carbon monoxide and hydrogen into such products are well known in the art.
As mentioned hereinbefore, it is an advantageous aspect of the present invention that naturally occurring hydrocarbon sources which also comprise sulphur or sulphur-containing compounds may be subjected to catalytic partial oxidation without the need to treat the hydrocarbon feedstock to a sulphur removal stage. This is in contrast to the conventional processing of naturally occurring hydrocarbon feedstocks, such as natural or associated gas, which are subjected to a desulphurisation treatment before use. Thus, it fo-lows that sulphur removal nes-d only be applied if the carbon monoxide and/or hydrogen products of the process are to be utilised in applications which are sensitive to the presence of sulphur, such as Fischer-Tropsch synthesis. In such cases, the sulphur removal treatment may be applied to the product stream of the catalytic partial oxidation process.
Accordingly, in a further aspect, the present invention provides a process for the preparation of carbon monoxide and/or hydrogen from a hydrocarbon feedstock comprising subjecting the hydrocarbon feedstock in a first stage to a catalytic partial oxidation process as hereinbefore described and subjecting at least a portion of the product of the first stage in a second stage to a desulphurisation process.
This aspect of the present invention will be further discussed having reference to the Figure which is a schematic representation of one embodiment for a process for the catalytic partial oxidation of a sulphur containing hydrocarbon feedstock.
I -s Ib~L~IIB I -P WO 95/18062 PCT/EP94/04270 13 Referring to the Figure, a catalytic partial oxidation reactor 2 is supplied via line 4 with a feed mixture comprising substantially pure oxygen and a sulphur-containing natural gas. The substantially pure oxygen comprises a minor amount of nitrogen and is prepared by the distillation of liquified air in a distillation unit (not shown) linked to the catalytic partial oxidation processing unit by line 6. The hot product stream of the catalytic partial oxidation reactor 2 is led via line 8 to a heat exchanger in which the hot product stream is used to preheat natural gas fed to the heat exchanger by line 12. The preheated natural gas feed is supplied to the inlet of the catalytic partial oxidation reactor via line 14.
The cooled product stream of the catalytic partial oxidation reactor is removed from the heat exchanger via line 16. A product stream comprising carbon monoxide and hydrogen is withdrawn from the process via line 18 to be employed as a feed for sulphur-tolerant applications (not shown). A portion of the cooled product stream is supplied via line 20 to a desulphurisation unit 22. A substantially sulphur-free product stream is removed from the desulphurisation unit 22 via line 24 for supply to sulphur-sensitive applications.
Suitable processes for use in the desulphurisation unit for removing sulphur-containing components from the carbon monoxide/hydrogen product are well known in the art. Suitable techniques include adsorption of the sulphur-containing compounds by passing the product stream through a bed of a suitable adsorbent, for example active carbon or zinc oxide.
The process of the present invention is further described by way of the following illustrative examples, in which Examples 1 and 2 are embodiments of the present invention and Example 3 is for comparative purposes only.
Example 1 Catalyst Preparation Barium hexa-aluminate (BaA 12
O
19 was prepared as follbws: Barium (21.0 g) was added to isopropyl alcohol (1500 ml) under an atmosphere of nitrogen and the resultant mixture heated under g 3e~-4 I 4i l~sl IIII~P4PIPII WO 95/18062 PCT/EP94/04270 14 reflux for 1.5 hours. Further isopropyl alcohol (1000 ml) was added to the resulting solution. Thereafter, aluminium isopropylate (379.65 g) was added stepwise and the mixture heated under reflux for a period of 5 hours. The resulting mixture (601.87 g) was combined with demineralised water (22.5 g) and heated under reflux whilst stirring for a further 1 hour. The resulting solution was subsequently heated to evaporate the solvent to leave a solid residue. The solid was dried by heating to 120 °C and maintained at that temperature for 4 hours. Thereafter, the solid was calcined in a first stage by heating to 450 OC over a period of 4 hours and being held at that temperature for 1 hour and in a second stage by heating to 1300 °C over a period of 1 hour and being held at that temperature for 5 hours.
An aqueous solution was prepared by dissolving rhodium chloride (RhC1 3 2.0 g) and hydrochloric acid 1.0 g) in demineralised water (6.83 g) to give a rhodium concentration of 10% by weight.
The barium hexa-aluminate prepared as described hereabove (30/80 mesh, 2.0 g) was immersed in the aforementioned aqueous solution (1.07 The resulting mixture was agitated firstly in a rolling mill for 1 hour and thereafter in a rotary drier for 1 hour. The resulting material was dried in an oven by heating for 1 hour and being held at a temperature of 120 *C for 5 hours and subsequently calcined by heating for 5 hours and being held at a temperature of 500 °C for 1 hour. The resulting catalyst comprised 5.0% by weight rhodium.
Catalytic Partial Oxidation A reactor was constructed comprising a transparent sapphire tube mounted concentrically within an outer transparent polycarbonate tube. ‘The rhodium-containing catalyst prepared as hereinbefore described was loaded into the sapphire tube and retained in the form of a fixed bed of catalyst particles having a tortuosity of 1.5. A feed mixture comprising methane and oxygen, in sufficient amounts to give an oxygen-to-carbon ratio of 0.63, was thoroughly mixed just before being introduced into the reactor to contact the fixed bed of catalyst. The feed mixture was fed to the L ii I be II- _~Cb [glaaa~ass~a~a~ 9 WO 95/18062 PCT/EP94/04270 15 reactor at a pressure of, 3.2 bara and at a gas hourly space velocity (GHSV) of 1,400,000 Nl/kg/hr. The feed mixture comprised 10% by volume of nitrogen. Tetrahydrothiophene was present in the feed mixture in an amount sufficient to give a sulphur concentration of 4.5 ppmv.
The operating temperature of the catalyst bed was measured by optical pyrometry. The composition of the gas mixture leaving the reactor was measured by gas chromatography. The conversion and the selectivity of the process to carbon monoxide and hydrogen (on the basis of methane converted) was determined. The ammonia content of the product gas was determined by passing the gas stream through an aqueous solution of sulphuric acid to remove the ammonia, followed by titration of the solution. The hydrogen cyanide content was determined in a similar manner using an aqueous solution of potassium hydroxide.
The operating conditions of the reactor and the results of the experiment are summarised in the Table hereinbelow.
Example 2 The catalyst preparation and process method described in Example 1 was followed, with the exception that tetrahydrothiophene was present in the feed mixture in an amount sufficient to give a sulphur concentration of 0.6 ppm. The operating conditions of the reactor and the results of the experiment are summarised in the Table hereinbelow.
Example 3 Comparative Example The catalyst preparation and process method described in Example 1 was followed, with the exception that the feed mixture was sulphur free. The operating conditions of the reactor and the results of the experiment are summarised in the Table hereinbelow.
P Iqa bllL~-%Blllj WO 95/18062 WO 9518062PCT/EP94/04270 16 Table Eakmple 1 Example 2 Example 3 Feed composition Nq, content vol) 10 10 S content (ppmv) 1 4.5 0.6 0.0 oxygen/carbon ratio 0.63 0.63 0.63 Operating Conditions Pressure (bara) 3.2 3.2 3.2 GHSV (1000 N1/kg/hr) 1400 1400 1400 Product Stream NH.I content (ppmv) 0.6 2.3 210.02 HCN content (ppmv) T-<0.1 1 1.0 3 present as tetrahydrothiophene accuracy ppmv accuracy ppmv Claims (27) 1. A process for the catalytic partial oxidation of a hydrocarbon feedstock, which process comprises contacting a feed mixture comprising the hydrocarbon feedstock and an oxygen-containing gas, which feed mixture also comprises nitrogen, with a catalyst capable of catalysing the partial oxidation of the hydrocarbon feedstock, wherein the feed mixture also comprises a sulfur-containing compound. 2. A process according to claim 1, characterised in the hydrocarbon feedstock comprises methane, natural gas, associated gas or a source of light hydrocarbons. 3. A process according to claim 1 or claim 2, characterised in that the oxygen- containing gas is substantially pure oxygen. 4. A process according to any one of the preceding claims, characterised in that the feed comprises the hydrocarbon feedstock and the oxygen-containing gas in amounts giving an oxygen-to-carbon ratio of from 0.3 to 0.8. A process according to claim 4, wherein the oxygen-to-carbon ratio is from 0.45 to 0.75. 6. A process according to claim 4, wherein the oxygen-to-carbon ratio is from 0.45 to 0.65. 7. A process according to any one of the preceding claims, characterised in that the sulfur-containing compound is hydrogen sulfide, sulfur dioxide, carbonyl sulfide, a mercaptan, an organic sulfide, or a thiopene. 8. A process according to claim 7, wherein the thiophene is tetrahydrothiophene. 9. A process according to any one of the preceding claims, characterised in that the sulfur-containing compound is present in an amount of from 0.05 to 100 ppm. 10. A process according to claim 9, wherein the sulfur-containing compound is present in an amount of from 0.1 to 50 ppm. 11. A process according to claim 10, wherein the sulfur-containing compound is present in an amount of from 0.1 to 10 ppm. S• 12. A process according to any one of the preceding claims, characterised in that the feed is contacted with the catalyst at a pressure in the range of up to 150 bar. 13. A process according to claim 12, wherein the feed is contacted with the catalyst at a pressure in the range of from 2 to 125 bar. 14. A process according to claim 12, wherein the feed is contacted with the catalyst at a pressure in the range of from 2 to 100 bar. A process according to any one of the preceding claims, characterised in that the feed is contacted with the catalyst at a temperature in the range of from 950 to 1300 0 C. 16. A process according to claim 15, wherein the feed is contacted viith the catalyst at a temperature in the range of from 950 to 1300°C. [N:\LIBAA]00839:KEH i Is~-~L~A 17. A process according to claim 15, wherein the feed is contacted with the catalyst at a temperature in the range of from 1000 to 1200 0 C. 18. A process according to any one of the preceding claims, characterised in that the feed is contacted with the catalyst at a gas hourly space velocity in the range of from 20,000 to 100,000,000 Nl/kg/hr. 19. A process according to claim 18, wherein velocity is in the range of from 50,000 to 50,000,000 Nl/kg/hr. A process according to claim 18, wherein velocity is in the range of from 500,000 to 30,000,000 Nl/kg/hr. 21. A process according to any one of the preceding claims, characterised in that the catalyst comprises rhodium, ruthenium or iridium. 22. A process according to any one of the preceding claims, characterised in that the catalyst is retained in a fixed arrangement. 23. A process according to claim 22, wherein the catalyst is retained in the form of a fixed bed of catalyst particles or in the form of a ceramic foam. 24. A process according to claim 22, wherein the catalyst is retained in the form of a ceramic foam. A process according to any one of claims 22 to 24, characterised in that the fixed arrangement of the catalyst has a tortuosity in the range of from 1.1 to O l'ut :I.0. 26. A process according to claim 25, wherein the fixed arrangenirt catalyst has a tortuosity in the range of from 1.1 to about 27. A process according to claim 25, wherein the fixed arrangement of the catalyst has a tortuosity in the range of from 1.3 to about 28. A process according to any one of claims 22 to 27, characterised in that the 25 fixed arrangement of the catalyst has from about 1000 to about 15000 pores per square centimetre. 29. A process according to claim 28, wherein the fixed arrangement of the catalyst i" has from about 1250 to about 10000 pores per square centimetre. A process according to any one of the preceding claims, characterised in that 3o the feed is contacted with the catalyst under substantially adiabatic conditions. 31. A process for the catalytic partial oxidation of a hydrocarbon feedstock, substantially as hereinbefore described with reference to any one of the Examples but excluding the Comparative Examples. 32. A process for the preparation of carbon monoxide and/or hydrogen from a hydrocarbon feedstock comprising subjecting the hydrocarbon feedstock in a first stage to a catalytic partial oxidation process as defined in any one of claims 1 to 31 and subjecting at least a portion of the product of the first stage in a second stage to a desulphurisation process. -1i' [N:\LIBAA]00839:KEH s~slsa -a r II-- 19 33. Carbon monoxide or hydrogen whenever prepared by a process according to any one of claims 1 to 32. Dated 19 June, 1997 Shell Internationale Research Maatschappij B.V. Patent Attorneys for the Applicant/Nominated Person SPRUSON FERGUSON V. [N:\LIBAA]00839:KEH AU13173/95A 1993-12-27 1994-12-22 Process for the catalytic partial oxidation of hydrocarbons Ceased AU682239B2 (en) Applications Claiming Priority (3) Application Number Priority Date Filing Date Title EP93203703 1993-12-27 EP93203703 1993-12-27 PCT/EP1994/004270 WO1995018062A1 (en) 1993-12-27 1994-12-22 Process for the catalytic partial oxidation of hydrocarbons Publications (2) Publication Number Publication Date AU1317395A AU1317395A (en) 1995-07-17 AU682239B2 true AU682239B2 (en) 1997-09-25 Family ID=8214249 Family Applications (1) Application Number Title Priority Date Filing Date AU13173/95A Ceased AU682239B2 (en) 1993-12-27 1994-12-22 Process for the catalytic partial oxidation of hydrocarbons Country Status (18) Country Link US (1) US5720901A (en) EP (1) EP0737163B1 (en) JP (1) JPH09502695A (en) CN (1) CN1044354C (en) AT (1) ATE179395T1 (en) AU (1) AU682239B2 (en) BR (1) BR9408420A (en) CA (1) CA2179911A1 (en) CO (1) CO4410233A1 (en) DE (1) DE69418213T2 (en) DZ (1) DZ1840A1 (en) ES (1) ES2133719T3 (en) NO (1) NO962682L (en) NZ (1) NZ277807A (en) RU (1) RU2132299C1 (en) SG (1) SG48008A1 (en) WO (1) WO1995018062A1 (en) ZA (1) ZA9410245B (en) Families Citing this family (51) * Cited by examiner, † Cited by third party Publication number Priority date Publication date Assignee Title US20040228792A1 (en) * 1998-06-30 2004-11-18 Assink Gerrit Jan Barend Catalyst comprising two catalytically-active metals US6080301A (en) 1998-09-04 2000-06-27 Exxonmobil Research And Engineering Company Premium synthetic lubricant base stock having at least 95% non-cyclic isoparaffins US6475960B1 (en) 1998-09-04 2002-11-05 Exxonmobil Research And Engineering Co. Premium synthetic lubricants US6221280B1 (en) 1998-10-19 2001-04-24 Alliedsignal Inc. Catalytic partial oxidation of hydrocarbon fuels to hydrogen and carbon monoxide US6579510B2 (en) 1999-07-30 2003-06-17 Alfred E. Keller SPOX-enhanced process for production of synthesis gas US6946111B2 (en) 1999-07-30 2005-09-20 Conocophilips Company Short contact time catalytic partial oxidation process for recovering sulfur from an H2S containing gas stream US6800269B2 (en) 1999-07-30 2004-10-05 Conocophillips Company Short contact time catalytic sulfur recovery system for removing H2S from a waste gas stream US6403051B1 (en) * 1999-07-30 2002-06-11 Conoco Inc. Recovery of sulfur from H2S and concurrent production of H2 using short contact time CPOX WO2001060515A2 (en) * 2000-02-18 2001-08-23 Conoco Inc. Reticulated ceramic foam catalysts for synthesis gas production FR2805531B1 (en) * 2000-02-24 2003-02-21 Air Liquide PROCESS FOR THE PRODUCTION OF HYDROGEN BY PARTIAL OXIDATION OF HYDROCARBONS US6497856B1 (en) 2000-08-21 2002-12-24 H2Gen Innovations, Inc. System for hydrogen generation through steam reforming of hydrocarbons and integrated chemical reactor for hydrogen production from hydrocarbons US7122170B2 (en) * 2000-07-25 2006-10-17 Conocophillips Company Catalysts for SPOC™ enhanced synthesis gas production ATE378286T1 (en) * 2000-07-25 2007-11-15 Conocophillips Co SPOX-ASSISTED PROCESS FOR PRODUCING SYNTHESIS GAS EP1355719B1 (en) * 2000-12-18 2009-06-24 ConocoPhilips Company Short contact time catalytic sulfur recovery system for removing h2s from a waste gas stream US7357908B2 (en) * 2000-12-18 2008-04-15 Conocophillips Company Apparatus and catalytic partial oxidation process for recovering sulfur from an H2S-containing gas stream US7326397B2 (en) * 2000-12-18 2008-02-05 Conocophillips Company Catalytic partial oxidation process for recovering sulfur from an H2S-containing gas stream US6673230B2 (en) 2001-02-08 2004-01-06 Bp Corporation North America Inc. Process for oxygenation of components for refinery blending of transportation fuels US6872231B2 (en) * 2001-02-08 2005-03-29 Bp Corporation North America Inc. Transportation fuels US6881325B2 (en) * 2001-02-08 2005-04-19 Bp Corporation North America Inc. Preparation of components for transportation fuels US20020148754A1 (en) * 2001-02-08 2002-10-17 Gong William H. Integrated preparation of blending components for refinery transportation fuels GB0113370D0 (en) 2001-06-01 2001-07-25 Kvaerner Process Tech Ltd Process US20030103892A1 (en) * 2001-10-17 2003-06-05 Conoco Inc. Promoted cobalt-chromium oxide catalysts on lanthanide-modified supports and process for producing synthesis gas CA2470344A1 (en) * 2001-12-18 2003-06-26 Conocophillips Company Catalyst for spoc-enhanced synthesis gas production FR2833863B1 (en) * 2001-12-20 2004-08-20 Air Liquide CATALYTIC REACTOR, CORRESPONDING INSTALLATION AND REACTION METHOD US20030119658A1 (en) * 2001-12-21 2003-06-26 Conocophillips Company Recovery of rhenium from a spent catalyst via sublimation US7303606B2 (en) * 2002-01-08 2007-12-04 The Boc Group, Inc. Oxy-fuel combustion process US6783749B2 (en) * 2002-05-13 2004-08-31 The Boc Group, Inc. Gas recovery process US6911161B2 (en) * 2002-07-02 2005-06-28 Conocophillips Company Stabilized nickel-containing catalysts and process for production of syngas US7094730B2 (en) * 2002-10-31 2006-08-22 Delphi Technologies, Inc. Gas treatment device, methods for making and using the same, and a vehicle exhaust system US7074375B2 (en) * 2002-12-03 2006-07-11 Engelhard Corporation Method of desulfurizing a hydrocarbon gas by selective partial oxidation and adsorption EP1581601B1 (en) * 2002-12-17 2008-08-13 Shell Internationale Researchmaatschappij B.V. Process for the catalytic selective oxidation of sulphur compounds US7041621B2 (en) 2003-01-17 2006-05-09 Conocophillips Company Sulfided catalysts for improved performance in hydrocarbon processing US7932296B2 (en) * 2003-03-16 2011-04-26 Kellogg Brown & Root Llc Catalytic partial oxidation reforming for syngas processing and products made therefrom US8273139B2 (en) * 2003-03-16 2012-09-25 Kellogg Brown & Root Llc Catalytic partial oxidation reforming US6974843B2 (en) * 2003-04-02 2005-12-13 Conoco Phillips Company Cogeneration of organic compounds with synthesis gas by catalytic partial oxidation US7316806B2 (en) * 2003-10-29 2008-01-08 Nippon Shokubai Co., Ltd. Modifying catalyst for partial oxidation and method for modification US20050154069A1 (en) * 2004-01-13 2005-07-14 Syntroleum Corporation Fischer-Tropsch process in the presence of nitrogen contaminants US7108842B2 (en) * 2004-01-15 2006-09-19 Conocophillips Company Process for the catalytic partial oxidation of H2S using staged addition of oxygen US7022742B2 (en) * 2004-04-08 2006-04-04 Syntroleum Corporation Process to control nitrogen-containing compounds in synthesis gas US7037485B1 (en) 2004-11-18 2006-05-02 Praxair Technology, Inc. Steam methane reforming method CA2587289C (en) * 2004-11-18 2010-07-06 Praxair Technology, Inc. Steam methane reforming method US7226572B1 (en) * 2006-03-03 2007-06-05 Conocophillips Company Compact sulfur recovery plant and process US7501111B2 (en) 2006-08-25 2009-03-10 Conoco Phillips Company Increased capacity sulfur recovery plant and process for recovering elemental sulfur DK1920832T3 (en) * 2006-11-08 2012-02-27 Air Liquide Process for preparing a supported precious metal catalyst EP1920830A1 (en) * 2006-11-08 2008-05-14 L'AIR LIQUIDE, Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude Group VIII and ceria/zirconia containing catalysts for catalytic hydrocarbon reforming or oxidation US20080260631A1 (en) * 2007-04-18 2008-10-23 H2Gen Innovations, Inc. Hydrogen production process JP4496346B2 (en) * 2007-10-11 2010-07-07 石油資源開発株式会社 Hydrocarbon reforming catalyst and method for producing synthesis gas using the same JP4639247B2 (en) 2008-07-23 2011-02-23 石油資源開発株式会社 Hydrocarbon reforming catalyst, process for producing the same, and process for producing synthesis gas using the same US8007761B2 (en) * 2008-12-24 2011-08-30 Praxair Technology, Inc. Carbon dioxide emission reduction method CN101811047B (en) * 2009-02-20 2012-10-03 中科合成油技术有限公司 Iron base catalyst used for Fischer-Tropsch synthesis and preparation method and application thereof DE102010034848B4 (en) 2010-08-13 2019-05-09 Arianegroup Gmbh Dual fuel engine Citations (3) * Cited by examiner, † Cited by third party Publication number Priority date Publication date Assignee Title EP0303438A2 (en) * 1987-08-14 1989-02-15 DAVY McKEE CORPORATION Production of synthesis gas from hydrocarbonaceous feedstock WO1992011199A1 (en) * 1990-12-24 1992-07-09 British Gas Plc Improved processes for the conversion of methane to synthesis gas WO1993001130A1 (en) * 1991-07-02 1993-01-21 University Of Warwick Catalysts for the production of carbon monoxide Family Cites Families (6) * Cited by examiner, † Cited by third party Publication number Priority date Publication date Assignee Title US4927857A (en) * 1982-09-30 1990-05-22 Engelhard Corporation Method of methanol production GB8623482D0 (en) * 1986-09-30 1986-11-05 Johnson Matthey Plc Catalytic generation of hydrogen CA2020151C (en) * 1989-06-30 1997-12-09 Malcolm Leslie Hodder Green Catalytic conversion of methane US5087271A (en) * 1990-11-19 1992-02-11 Texaco Inc. Partial oxidation process EP0522744B1 (en) * 1991-07-09 1997-08-13 Imperial Chemical Industries Plc Synthesis gas production US5250083A (en) * 1992-04-30 1993-10-05 Texaco Inc. Process for production desulfurized of synthesis gas 1994 1994-12-21 CO CO94057767A patent/CO4410233A1/en unknown 1994-12-21 US US08/361,359 patent/US5720901A/en not_active Expired - Fee Related 1994-12-22 AU AU13173/95A patent/AU682239B2/en not_active Ceased 1994-12-22 BR BR9408420A patent/BR9408420A/en not_active IP Right Cessation 1994-12-22 JP JP7517769A patent/JPH09502695A/en active Pending 1994-12-22 DE DE69418213T patent/DE69418213T2/en not_active Expired - Fee Related 1994-12-22 RU RU96116138A patent/RU2132299C1/en active 1994-12-22 CN CN94194660A patent/CN1044354C/en not_active Expired - Fee Related 1994-12-22 WO PCT/EP1994/004270 patent/WO1995018062A1/en active IP Right Grant 1994-12-22 NZ NZ277807A patent/NZ277807A/en unknown 1994-12-22 ES ES95904522T patent/ES2133719T3/en not_active Expired - Lifetime 1994-12-22 CA CA002179911A patent/CA2179911A1/en not_active Abandoned 1994-12-22 AT AT95904522T patent/ATE179395T1/en active 1994-12-22 ZA ZA9410245A patent/ZA9410245B/en unknown 1994-12-22 EP EP95904522A patent/EP0737163B1/en not_active Expired - Lifetime 1994-12-22 SG SG1996006077A patent/SG48008A1/en unknown 1994-12-25 DZ DZ940139A patent/DZ1840A1/en active 1996 1996-06-25 NO NO962682A patent/NO962682L/en not_active Application Discontinuation Patent Citations (3) * Cited by examiner, † Cited by third party Publication number Priority date Publication date Assignee Title EP0303438A2 (en) * 1987-08-14 1989-02-15 DAVY McKEE CORPORATION Production of synthesis gas from hydrocarbonaceous feedstock WO1992011199A1 (en) * 1990-12-24 1992-07-09 British Gas Plc Improved processes for the conversion of methane to synthesis gas WO1993001130A1 (en) * 1991-07-02 1993-01-21 University Of Warwick Catalysts for the production of carbon monoxide Also Published As Publication number Publication date DE69418213D1 (en) 1999-06-02 NO962682L (en) 1996-08-15 SG48008A1 (en) 1998-04-17 DE69418213T2 (en) 1999-10-14 EP0737163B1 (en) 1999-04-28 US5720901A (en) 1998-02-24 AU1317395A (en) 1995-07-17 JPH09502695A (en) 1997-03-18 WO1995018062A1 (en) 1995-07-06 CA2179911A1 (en) 1995-07-06 ZA9410245B (en) 1995-08-29 ATE179395T1 (en) 1999-05-15 CN1044354C (en) 1999-07-28 CO4410233A1 (en) 1997-01-09 EP0737163A1 (en) 1996-10-16 CN1139416A (en) 1997-01-01 NZ277807A (en) 1997-04-24 RU2132299C1 (en) 1999-06-27 DZ1840A1 (en) 2002-02-17 NO962682D0 (en) 1996-06-25 ES2133719T3 (en) 1999-09-16 BR9408420A (en) 1997-08-26 Similar Documents Publication Publication Date Title AU682239B2 (en) 1997-09-25 Process for the catalytic partial oxidation of hydrocarbons US5486313A (en) 1996-01-23 Process for the preparation of carbon monoxide and/or hydrogen AU679128B2 (en) 1997-06-19 Process for the catalytic partial oxidation of hydrocarbons US6946111B2 (en) 2005-09-20 Short contact time catalytic partial oxidation process for recovering sulfur from an H2S containing gas stream US5639401A (en) 1997-06-17 Process for the catalytic partial oxidation of hydrocarbons AU672901B2 (en) 1996-10-17 Process for the catalytic partial oxidation of hydrocarbons EP1093439B1 (en) 2003-02-19 Catalytic partial oxidation with a rhodium-iridium alloy catalyst AU737880B2 (en) 2001-09-06 A process for the preparation of hydrogen and carbon monoxide EP0640561B1 (en) 1998-11-11 Process for the catalytic partial oxidation of hydrocarbons EP1049645B1 (en) 2003-04-23 Catalyst suitable for the preparation of hydrogen and carbon monoxide from a hydrocarbonaceous feedstock WO1998035908A1 (en) 1998-08-20 Catalytic partial oxidation of hydrocarbons AU671232B2 (en) 1996-08-15 Process for the catalytic partial oxidation of hydrocarbons EP1355720B1 (en) 2008-12-03 Sulfur recovery process US20020182142A1 (en) 2002-12-05 Process for the catalytic partial oxidation of a hydrocarbonaceous feedstock AU2002245146A1 (en) 2003-02-13 Sulfur recovery process MXPA00006950A (en) 2001-07-09 Catalyst suitable for the preparation of hydrogen and carbon monoxide from a hydrocarbonaceous feedstock Legal Events Date Code Title Description 2001-07-19 MK14 Patent ceased section 143(a) (annual fees not paid) or expired
Download PDF in English

None

Contact information