US20090294103A1 - Process to reduce the temperature of a hydrogen and carbon monoxide containing gas and heat exchanger for use in said process - Google Patents

Process to reduce the temperature of a hydrogen and carbon monoxide containing gas and heat exchanger for use in said process Download PDF

Info

Publication number
US20090294103A1
US20090294103A1 US12/539,870 US53987009A US2009294103A1 US 20090294103 A1 US20090294103 A1 US 20090294103A1 US 53987009 A US53987009 A US 53987009A US 2009294103 A1 US2009294103 A1 US 2009294103A1
Authority
US
United States
Prior art keywords
metal alloy
gas
heat exchanger
temperature
alloy surface
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.)
Abandoned
Application number
US12/539,870
Inventor
Franciscus Gerardus Van Dongen
Winnifred De Graaf
Thian Hoey Tio
Anthonij Wolfert
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.)
Individual
Original Assignee
Individual
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Individual filed Critical Individual
Priority to US12/539,870 priority Critical patent/US20090294103A1/en
Publication of US20090294103A1 publication Critical patent/US20090294103A1/en
Abandoned legal-status Critical Current

Links

Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
    • F28F21/00—Constructions of heat-exchange apparatus characterised by the selection of particular materials
    • F28F21/08—Constructions of heat-exchange apparatus characterised by the selection of particular materials of metal
    • F28F21/081—Heat exchange elements made from metals or metal alloys
    • F28F21/087—Heat exchange elements made from metals or metal alloys from nickel or nickel alloys
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/02—Apparatus characterised by being constructed of material selected for its chemically-resistant properties
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B32—LAYERED PRODUCTS
    • B32B—LAYERED PRODUCTS, i.e. PRODUCTS BUILT-UP OF STRATA OF FLAT OR NON-FLAT, e.g. CELLULAR OR HONEYCOMB, FORM
    • B32B15/00—Layered products comprising a layer of metal
    • B32B15/01—Layered products comprising a layer of metal all layers being exclusively metallic
    • B32B15/013—Layered products comprising a layer of metal all layers being exclusively metallic one layer being formed of an iron alloy or steel, another layer being formed of a metal other than iron or aluminium
    • 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
    • C01B3/36—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 oxygen or mixtures containing oxygen as gasifying agents
    • 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
    • C01B3/382—Multi-step processes
    • 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
    • C01B3/386—Catalytic partial combustion
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22C—ALLOYS
    • C22C27/00—Alloys based on rhenium or a refractory metal not mentioned in groups C22C14/00 or C22C16/00
    • C22C27/06—Alloys based on chromium
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22C—ALLOYS
    • C22C30/00—Alloys containing less than 50% by weight of each constituent
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F22—STEAM GENERATION
    • F22B—METHODS OF STEAM GENERATION; STEAM BOILERS
    • F22B37/00—Component parts or details of steam boilers
    • F22B37/02—Component parts or details of steam boilers applicable to more than one kind or type of steam boiler
    • F22B37/04—Component parts or details of steam boilers applicable to more than one kind or type of steam boiler and characterised by material, e.g. use of special steel alloy
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
    • F28F19/00—Preventing the formation of deposits or corrosion, e.g. by using filters or scrapers
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00049—Controlling or regulating processes
    • B01J2219/00051—Controlling the temperature
    • B01J2219/00074—Controlling the temperature by indirect heating or cooling employing heat exchange fluids
    • B01J2219/00087—Controlling the temperature by indirect heating or cooling employing heat exchange fluids with heat exchange elements outside the reactor
    • B01J2219/00094—Jackets
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/02—Apparatus characterised by their chemically-resistant properties
    • B01J2219/025—Apparatus characterised by their chemically-resistant properties characterised by the construction materials of the reactor vessel proper
    • B01J2219/0277—Metal based
    • B01J2219/029—Non-ferrous metals
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B23—MACHINE TOOLS; METAL-WORKING NOT OTHERWISE PROVIDED FOR
    • B23K—SOLDERING OR UNSOLDERING; WELDING; CLADDING OR PLATING BY SOLDERING OR WELDING; CUTTING BY APPLYING HEAT LOCALLY, e.g. FLAME CUTTING; WORKING BY LASER BEAM
    • B23K9/00—Arc welding or cutting
    • B23K9/04—Welding for other purposes than joining, e.g. built-up welding
    • 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
    • C01B2203/02—Processes for making hydrogen or synthesis gas
    • C01B2203/0205—Processes for making hydrogen or synthesis gas containing a reforming step
    • C01B2203/0227—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step
    • C01B2203/0233—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step the reforming step being a steam reforming step
    • 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
    • C01B2203/02—Processes for making hydrogen or synthesis gas
    • C01B2203/0205—Processes for making hydrogen or synthesis gas containing a reforming step
    • C01B2203/0227—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step
    • C01B2203/0238—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step the reforming step being a carbon dioxide reforming step
    • 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
    • C01B2203/02—Processes for making hydrogen or synthesis gas
    • C01B2203/025—Processes for making hydrogen or synthesis gas containing a partial oxidation step
    • C01B2203/0255—Processes for making hydrogen or synthesis gas containing a partial oxidation step containing a non-catalytic partial oxidation step
    • 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
    • C01B2203/08—Methods of heating or cooling
    • C01B2203/0805—Methods of heating the process for making hydrogen or synthesis gas
    • C01B2203/0838—Methods of heating the process for making hydrogen or synthesis gas by heat exchange with exothermic reactions, other than by combustion of fuel
    • C01B2203/0844—Methods of heating the process for making hydrogen or synthesis gas by heat exchange with exothermic reactions, other than by combustion of fuel the non-combustive exothermic reaction being another reforming reaction as defined in groups C01B2203/02 - C01B2203/0294
    • 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
    • C01B2203/08—Methods of heating or cooling
    • C01B2203/0872—Methods of cooling
    • C01B2203/0883—Methods of cooling by indirect heat exchange
    • 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
    • C01B2203/14—Details of the flowsheet
    • C01B2203/142—At least two reforming, decomposition or partial oxidation steps in series
    • 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
    • C01B2203/14—Details of the flowsheet
    • C01B2203/148—Details of the flowsheet involving a recycle stream to the feed of the process for making hydrogen or synthesis gas
    • 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
    • Y02P20/141—Feedstock
    • 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

Definitions

  • the invention is directed to a process to reduce the temperature of a hydrogen and carbon monoxide containing gas by contacting the gas with a metal alloy surface having a lower temperature than the temperature of the gas.
  • a disadvantage of the above apparatus is that in use coke will form on the interior surface of the tubes because part of the carbon monoxide reacts to carbon and carbon dioxide. Furthermore part of the surface will erode resulting eventually in an unacceptable low mechanical integrity of the tubes. These effects are especially significant when the amount of steam in the hot gas is below 50 vol %.
  • Such a hot CO and H 2 containing gas is for example obtained when performing a partial oxidation of natural gas, refinery gas, methane and the like in the absence of added steam as described in WO-A-9639354.
  • This object is achieved with the following process.
  • Process to reduce the temperature of a hydrogen and carbon monoxide containing gas by contacting the gas with a metal alloy surface having a lower temperature than the temperature of the gas, wherein the metal alloy surface comprises between 0 and 20 wt % iron, between 0 and 5 wt % aluminium, between 0 and 5 wt % silicon, between 20 and 50 wt % chromium and at least 35 wt % nickel, wherein the metal alloy surface maintains it lower temperature than the temperature of the gas by making use of coolant water.
  • the metal alloy surface layer comprises between 0 and 20 wt % and preferably between 0 and 7 wt % iron, preferably between 0 and 4 wt %, between 0 and 5 wt % aluminium, between 0 and 5 wt % silicon, between 20 and 50 wt % chromium, preferably between 30 and 50 wt % chromium, and at least 35 wt % nickel.
  • the nickel content balances the total to 100%.
  • aluminium and/or silicon in the metal alloy surface when the concentration of steam in the hot gas is lower than 50 vol %, preferably lower than 30 vol % and more preferably lower than 15 vol %.
  • concentration of steam in the hot gas is lower than 50 vol %, preferably lower than 30 vol % and more preferably lower than 15 vol %.
  • the resulting aluminium oxide and silicon oxide layers will provide an improved protection against coke formation and erosion when the conditions become more reducing at such low steam concentrations.
  • REM titanium and/or REM (reactive elements) are added to the metal alloy. Examples of REM are Y 2 O 3 , La 2 O 3 , CeO 2 , ZrO 2 and HfO 2 . The total content of these added compounds is between 0 and 2 wt %.
  • the metal alloy surface layer is supported with a metal alloy support layer having better mechanical properties than said surface layer.
  • the metal alloy support layer may be any metal alloy having the required mechanical strength for a particular application. Typically these metal alloys will contain more iron than the surface layer, suitably more than 7 wt % and even up to 98 wt %.
  • Other suitable metals, which can be present in this metal alloy, are chromium, nickel and molybdenum.
  • suitable metal allow support layers are carbon steels and so called low alloy steels having a typical Cr content of between 1-9 wt % and Mo content 0.1-2.25 wt %, austenitic stainless steels, for example the AISI 300 series (examples 304, 310, 316) with a typical Cr content of between 18-25% and Ni content of between 8-22%, cast materials, like for example HK-40, HP-40 and HP-modified, nickel based alloys, for example Inconel 600, Inconel 601, Inconel 690 and Incoloy 800 and ferritic stainless steels, which are Fe based alloys having a low nickel content, e.g. less than 2 wt % and a Cr content of above 12 wt %.
  • austenitic stainless steels for example the AISI 300 series (examples 304, 310, 316) with a typical Cr content of between 18-25% and Ni content of between 8-22%
  • cast materials like for example HK-40, HP-40 and HP
  • the two layers of metal alloys may be prepared by methods known to one skilled in the art.
  • the metal alloy composite is made by means of a building-up welding method resulting in a weld-mounted multi-layered metal surface.
  • This method is preferred because it enables one to make difficult tubular structures, as used in the heat exchanger, having the metal alloy surface according to the present invention.
  • Such a method is characterized in that the desired metal alloy for use as the surface layer is first atomized by gas atomization to form a powder of said alloy.
  • the iron content of said powder is substantially zero.
  • a layer of the metal alloy is subsequently applied on the support metal alloy by built-up welding by plasma powder welding of said powder. After machining the weld metal a flat metal alloy surface is obtained.
  • Thickness of the surface metal alloy may range suitably from 1 to 5 mm and preferably 1 to 3 mm. It has been found that the iron content in the metal alloy layer may contain iron in a situation wherein the starting powder did not contain iron. This is due to migration of iron from the support layer to the surface layer during the welding step. Care should be taken to limit the migration of iron to the surface layer such that the end iron content in the surface layer will be below 7 wt % and preferably below 4 wt %. The iron migration effect can be limited by using a low iron-content support layer, increasing the layer thickness and/or by applying the layer in more than one step. A preferred method to perform such a building-up welding method is described in EP-A-1043084, which publication is hereby incorporated by reference. This publication describes a method to obtain coke resistant furnace reactor tubes for a steam cracker process, which is aimed at preparing lower olefins, e.g. ethylene and propylene.
  • the gas is suitably obtained in a partial oxidation process of a hydrocarbon feedstock, for example coal, petroleum coke, residual refinery fractions, bituminous oils, such as ORIMULSION (trademark of Intevep S.A. Venezuela), natural gas, refinery gas, associated gas or (coal bed) methane and the like.
  • a hydrocarbon feedstock for example coal, petroleum coke, residual refinery fractions, bituminous oils, such as ORIMULSION (trademark of Intevep S.A. Venezuela), natural gas, refinery gas, associated gas or (coal bed) methane and the like.
  • ORIMULSION trademark of Intevep S.A. Venezuela
  • natural gas refinery gas
  • the feedstock to the partial oxidation may also comprise recycle fractions comprising hydrocarbons and carbon dioxide as may be obtained in downstream processes which use the CO/H 2 containing gas as feedstock.
  • the temperature of the hydrogen and carbon monoxide containing gas is preferably reduced from a temperature of between 1000 and 1500° C. to a temperature between 300 and 750° C.
  • the hydrogen to CO molar ratio will depend on the feedstock of the partial oxidation process.
  • an H 2 to CO molar ratio of the hot gas is preferably between 0.5 and 1.5.
  • the feedstock is a gaseous feedstock, like for example natural gas, this ratio is preferably between 1.6 and 2.5.
  • the reduction of the temperature of the resulting hot gas according to the process of the present invention is preferably performed at the exterior of water cooled tubes as placed in a vessel.
  • heat exchanger vessels are described in EP-A-342767 and EP-A-722999.
  • the reduction of the temperature of the resulting hot gas according to the process of the present invention is preferably performed at the interior of a conduit.
  • the metal alloy surface maintains it lower temperature than the temperature of the gas in one by contacting the metal alloy support layer at its free side with coolant water as for example described in the aforementioned EP-A-257719.
  • the gas is cooled by passing the gas through one or more conduits, which conduits are submerged in coolant water as contained in a vessel in which vessel steam is formed and discharged from said vessel and wherein the interior of the tubes consists of the metal alloy surface layer and the exterior of the tubes consist of the metal alloy support layer.
  • the invention is thus also related to a heat exchanger apparatus suited for lowering the temperature of a hot gas, comprising a vessel having a compartment for cooling water, an inlet for the gas to be cooled, an outlet for cooled gas, an outlet for heated steam and a collecting space for maintaining generated steam and at least one primary evaporator tube positioned in the compartment for cooling water and fluidly connected to the inlet for the gas to be cooled, and at least one steam tube for withdrawal of generated steam from the collecting space for maintaining generated steam and an inlet for fresh water, wherein the interior of the primary evaporator tube material consists of the above defined metal alloy surface and the exterior consists of the above defined metal alloy support layer.
  • the above apparatus may suitably comprise at least one secondary tube-shell heat exchanger vessel, which is used as ‘super heater module’.
  • Said extra vessel is positioned in the compartment for cooling water, such that the generated steam can be further heated against partially cooled gas from the primary evaporator tube.
  • coolant water as used in the claims refers to water in the gaseous phase having a cooling capacity relative to the partially cooled gas.
  • An example of such an apparatus is described in the above-mentioned EP-A-257719. More preferably the primary evaporator tube is fluidly connected to the tube side of the super heater module and the steam tube for withdrawal of generated steam is fluidly connected to the shell side of the super heater module.
  • a gas mixture as produced in a partial oxidation of natural gas and having the properties as listed in Table 1 was contacted for 4000 hours and at about 600° C. with a metal alloy surface having the composition as listed in Table 2.
  • the metal alloy surface was positioned on top of a support layer by the building-up welding method as described in EP-A-1043084.
  • the support layer was a low alloy steel having the properties of the metal used in Comparative A (see Table 2). Visual inspection and mechanical inspection showed no deterioration of the metal alloy surface after 4000 hours. Furthermore no coke formation was observed.
  • Example 1 Comparative A Ni 42 54 Cr 39 25 1.0 Al — 3 Fe 15.5 16 97.85 (balance) Ti 0.2 0.2 Mo 2.4 0.9 0.6 Mn 0.9 0.9 0.55
  • Example 1 was repeated except that a different metal alloy surface was used (See Table 2). The results were as in Example 1.
  • Example 1 was repeated except that a different metal alloy surface was used (See Table 2). In contrast to Examples 1 and 2 heavy coke formation was observed.

Abstract

Process to reduce the temperature of a hydrogen and carbon monoxide containing gas by contacting the gas with a metal alloy surface having a lower temperature than the temperature of the gas, wherein the metal alloy surface comprises between 0 and 20 wt % iron, between 0 and 5 wt % aluminium, between 0 and 5 wt % silicon, between 20 and 50 wt % chromium and at least 35 wt % nickel, wherein the metal alloy surface maintains it lower temperature than the temperature of the gas by making use of coolant water.

Description

  • This application is a division of application Ser. No. 10/493,328, filed Apr. 21, 2004, pending.
  • The invention is directed to a process to reduce the temperature of a hydrogen and carbon monoxide containing gas by contacting the gas with a metal alloy surface having a lower temperature than the temperature of the gas.
  • Such a process is described in EP-A-257719. This publication describes a vessel comprising tubes through which a hot carbon monoxide and hydrogen containing gas flows. The gas is reduced in temperature because the temperature of the tube surface has a reduced temperature relative to the hot gas. The temperature of the tubes is kept at a lower value because the tubes are submerged in water. In the cooling process water will evaporate. By ensuring that fresh water is supplied to the vessel the temperature of the tubes can be kept at a lower temperature than the hot gas. The tubes are typically made from metal alloys comprising substantially of iron. Iron containing alloys are preferred because of their mechanical strength in combination with their relative low cost. Furthermore usage of these alloys makes it possible to manufacture the complicated tube structures of an apparatus as disclosed in EP-A-257719.
  • A disadvantage of the above apparatus is that in use coke will form on the interior surface of the tubes because part of the carbon monoxide reacts to carbon and carbon dioxide. Furthermore part of the surface will erode resulting eventually in an unacceptable low mechanical integrity of the tubes. These effects are especially significant when the amount of steam in the hot gas is below 50 vol %. Such a hot CO and H2 containing gas is for example obtained when performing a partial oxidation of natural gas, refinery gas, methane and the like in the absence of added steam as described in WO-A-9639354.
  • It is the object of the present invention to provide a process to reduce the temperature of the hot gas wherein the above described problems such a coke formation and erosion are avoided or at least minimized.
  • This object is achieved with the following process. Process to reduce the temperature of a hydrogen and carbon monoxide containing gas by contacting the gas with a metal alloy surface having a lower temperature than the temperature of the gas, wherein the metal alloy surface comprises between 0 and 20 wt % iron, between 0 and 5 wt % aluminium, between 0 and 5 wt % silicon, between 20 and 50 wt % chromium and at least 35 wt % nickel, wherein the metal alloy surface maintains it lower temperature than the temperature of the gas by making use of coolant water.
  • Applicants found that coke formation and erosion can be reduced when the process according to the invention is used. Because the alloy layer, which contacts the hot gas, does not comprise a substantial amount of iron less coke formation and erosion is observed. A preferred support layer, which is not in direct contact with the hot gas, provides the mechanical strength to the metal alloy surface layer. This is advantageous because this feature makes it possible to construct for example the larger diameter tubes as in an apparatus according to EP-A-257719 in an economical manner.
  • The metal alloy surface layer comprises between 0 and 20 wt % and preferably between 0 and 7 wt % iron, preferably between 0 and 4 wt %, between 0 and 5 wt % aluminium, between 0 and 5 wt % silicon, between 20 and 50 wt % chromium, preferably between 30 and 50 wt % chromium, and at least 35 wt % nickel. The nickel content balances the total to 100%.
  • It has been found beneficial to have at least some aluminium and/or silicon in the metal alloy surface when the concentration of steam in the hot gas is lower than 50 vol %, preferably lower than 30 vol % and more preferably lower than 15 vol %. Preferably between 1-5 wt % aluminium and between 1-5 wt % silicon is present in said alloy layer under such low steam content conditions. The resulting aluminium oxide and silicon oxide layers will provide an improved protection against coke formation and erosion when the conditions become more reducing at such low steam concentrations. More preferably next to aluminium and silicon a small amount of titanium and/or REM (reactive elements) are added to the metal alloy. Examples of REM are Y2O3, La2O3, CeO2, ZrO2 and HfO2. The total content of these added compounds is between 0 and 2 wt %.
  • Preferably the metal alloy surface layer is supported with a metal alloy support layer having better mechanical properties than said surface layer. The metal alloy support layer may be any metal alloy having the required mechanical strength for a particular application. Typically these metal alloys will contain more iron than the surface layer, suitably more than 7 wt % and even up to 98 wt %. Other suitable metals, which can be present in this metal alloy, are chromium, nickel and molybdenum. Examples of suitable metal allow support layers are carbon steels and so called low alloy steels having a typical Cr content of between 1-9 wt % and Mo content 0.1-2.25 wt %, austenitic stainless steels, for example the AISI 300 series (examples 304, 310, 316) with a typical Cr content of between 18-25% and Ni content of between 8-22%, cast materials, like for example HK-40, HP-40 and HP-modified, nickel based alloys, for example Inconel 600, Inconel 601, Inconel 690 and Incoloy 800 and ferritic stainless steels, which are Fe based alloys having a low nickel content, e.g. less than 2 wt % and a Cr content of above 12 wt %.
  • The two layers of metal alloys may be prepared by methods known to one skilled in the art. Preferably the metal alloy composite is made by means of a building-up welding method resulting in a weld-mounted multi-layered metal surface. This method is preferred because it enables one to make difficult tubular structures, as used in the heat exchanger, having the metal alloy surface according to the present invention. Such a method is characterized in that the desired metal alloy for use as the surface layer is first atomized by gas atomization to form a powder of said alloy. Preferably the iron content of said powder is substantially zero. A layer of the metal alloy is subsequently applied on the support metal alloy by built-up welding by plasma powder welding of said powder. After machining the weld metal a flat metal alloy surface is obtained. Thickness of the surface metal alloy may range suitably from 1 to 5 mm and preferably 1 to 3 mm. It has been found that the iron content in the metal alloy layer may contain iron in a situation wherein the starting powder did not contain iron. This is due to migration of iron from the support layer to the surface layer during the welding step. Care should be taken to limit the migration of iron to the surface layer such that the end iron content in the surface layer will be below 7 wt % and preferably below 4 wt %. The iron migration effect can be limited by using a low iron-content support layer, increasing the layer thickness and/or by applying the layer in more than one step. A preferred method to perform such a building-up welding method is described in EP-A-1043084, which publication is hereby incorporated by reference. This publication describes a method to obtain coke resistant furnace reactor tubes for a steam cracker process, which is aimed at preparing lower olefins, e.g. ethylene and propylene.
  • The gas is suitably obtained in a partial oxidation process of a hydrocarbon feedstock, for example coal, petroleum coke, residual refinery fractions, bituminous oils, such as ORIMULSION (trademark of Intevep S.A. Venezuela), natural gas, refinery gas, associated gas or (coal bed) methane and the like. In case a gaseous feedstock like natural gas is used the partial oxidation is preferably performed in the absence of significant amounts of added steam, and preferably in the absence of added steam, as moderator gas. The feedstock to the partial oxidation may also comprise recycle fractions comprising hydrocarbons and carbon dioxide as may be obtained in downstream processes which use the CO/H2 containing gas as feedstock. An example of a suitable partial oxidation process is the so-called Shell Gasification Process as described in the Oil and Gas Journal, Sep. 6, 1971, pp 85-90. Publications describing examples of partial oxidation processes are U.S. Pat. No. 4,132,065, EP-A-291111, WO-A-9722547, WO-A-9639354 and WO-A-9603345.
  • The temperature of the hydrogen and carbon monoxide containing gas is preferably reduced from a temperature of between 1000 and 1500° C. to a temperature between 300 and 750° C. The hydrogen to CO molar ratio will depend on the feedstock of the partial oxidation process.
  • For example when a solid or liquid feedstock is used an H2 to CO molar ratio of the hot gas is preferably between 0.5 and 1.5. When the feedstock is a gaseous feedstock, like for example natural gas, this ratio is preferably between 1.6 and 2.5.
  • In case the feedstock of the partial oxidation is a solid hydrocarbon feed, for example coal or petroleum coke, the reduction of the temperature of the resulting hot gas according to the process of the present invention is preferably performed at the exterior of water cooled tubes as placed in a vessel. Examples of such heat exchanger vessels are described in EP-A-342767 and EP-A-722999.
  • In case the feedstock of the partial oxidation is a liquid or gaseous (at ambient conditions) hydrocarbon feed as described above the reduction of the temperature of the resulting hot gas according to the process of the present invention is preferably performed at the interior of a conduit. In such an embodiment the metal alloy surface maintains it lower temperature than the temperature of the gas in one by contacting the metal alloy support layer at its free side with coolant water as for example described in the aforementioned EP-A-257719. In such an embodiment the gas is cooled by passing the gas through one or more conduits, which conduits are submerged in coolant water as contained in a vessel in which vessel steam is formed and discharged from said vessel and wherein the interior of the tubes consists of the metal alloy surface layer and the exterior of the tubes consist of the metal alloy support layer.
  • The invention is thus also related to a heat exchanger apparatus suited for lowering the temperature of a hot gas, comprising a vessel having a compartment for cooling water, an inlet for the gas to be cooled, an outlet for cooled gas, an outlet for heated steam and a collecting space for maintaining generated steam and at least one primary evaporator tube positioned in the compartment for cooling water and fluidly connected to the inlet for the gas to be cooled, and at least one steam tube for withdrawal of generated steam from the collecting space for maintaining generated steam and an inlet for fresh water, wherein the interior of the primary evaporator tube material consists of the above defined metal alloy surface and the exterior consists of the above defined metal alloy support layer.
  • Preferably the above apparatus may suitably comprise at least one secondary tube-shell heat exchanger vessel, which is used as ‘super heater module’. Said extra vessel is positioned in the compartment for cooling water, such that the generated steam can be further heated against partially cooled gas from the primary evaporator tube. In this embodiment the term coolant water as used in the claims refers to water in the gaseous phase having a cooling capacity relative to the partially cooled gas. An example of such an apparatus is described in the above-mentioned EP-A-257719. More preferably the primary evaporator tube is fluidly connected to the tube side of the super heater module and the steam tube for withdrawal of generated steam is fluidly connected to the shell side of the super heater module.
  • The invention will be illustrated by the following non-limiting examples.
    • EXAMPLE 1
  • A gas mixture as produced in a partial oxidation of natural gas and having the properties as listed in Table 1 was contacted for 4000 hours and at about 600° C. with a metal alloy surface having the composition as listed in Table 2. The metal alloy surface was positioned on top of a support layer by the building-up welding method as described in EP-A-1043084. The support layer was a low alloy steel having the properties of the metal used in Comparative A (see Table 2). Visual inspection and mechanical inspection showed no deterioration of the metal alloy surface after 4000 hours. Furthermore no coke formation was observed.
  • TABLE 1
    CO 33 (mol %)
    H2 55
    H2O 7.5
    CO2 4.5
    Soot 50-100 ppm
  • TABLE 2
    Example 1 2 Comparative A
    Ni 42 54
    Cr 39 25 1.0
    Al — 3
    Fe 15.5 16 97.85 (balance)
    Ti 0.2 0.2
    Mo 2.4 0.9 0.6
    Mn 0.9 0.9 0.55
    • EXAMPLE 2
  • Example 1 was repeated except that a different metal alloy surface was used (See Table 2). The results were as in Example 1.
    • COMPARATIVE EXPERIMENT A
  • Example 1 was repeated except that a different metal alloy surface was used (See Table 2). In contrast to Examples 1 and 2 heavy coke formation was observed.

Claims (6)

1. A heat exchanger apparatus suited for lowering the temperature of a hot gas, comprising a vessel having a compartment for cooling water, an inlet for the gas to be cooled, an outlet for cooled gas, an outlet for heated steam and a collecting space for maintaining generated steam and at least one primary evaporator tube positioned in the compartment for cooling water and fluidly connected to the inlet for the gas to be cooled, and at least one steam tube for withdrawal of generated steam from the collecting space for maintaining generated steam and an inlet for fresh water, wherein the interior of the primary evaporator tube material has a metal alloy surface comprising between 0 and 20 wt % iron, between 0 and 5 wt % aluminium, between 0 and 5 wt % silicon, between 20 and 50 wt % chromium and at least 35 wt % nickel, which surface layer is supported by a metal alloy support layer having better mechanical properties than said surface layer.
2. A heat exchanger according to claim 1, wherein the content of chromium in the metal alloy surface is more than 25 wt %.
3. A heat exchanger according to claim 2, wherein the metal alloy surface comprises between 1 and 5 wt % aluminium.
4. A heat exchanger according to claim 3, wherein the metal alloy surface comprises between 1 and 5 wt % silicon.
5. A heat exchanger according to claim 4, wherein the metal alloy surface comprises between 0 and 2 wt % titanium.
6. A heat exchanger according to claim 5, wherein the metal alloy surface layer is applied to the metal alloy support layer by means of a building-up welding method.
US12/539,870 2001-10-22 2009-08-12 Process to reduce the temperature of a hydrogen and carbon monoxide containing gas and heat exchanger for use in said process Abandoned US20090294103A1 (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
US12/539,870 US20090294103A1 (en) 2001-10-22 2009-08-12 Process to reduce the temperature of a hydrogen and carbon monoxide containing gas and heat exchanger for use in said process

Applications Claiming Priority (5)

Application Number Priority Date Filing Date Title
EP01204009.3 2001-10-22
EP01204009 2001-10-22
PCT/EP2002/011801 WO2003036165A2 (en) 2001-10-22 2002-10-22 Process to reduce the temperature of a hydrogen and carbon monoxide containing gas and heat exchanger for use in said process
US10/493,328 US7597067B2 (en) 2001-10-22 2002-10-22 Process to reduce the temperature of a hydrogen and carbon monoxide containing gas and heat exchanger for use in said process
US12/539,870 US20090294103A1 (en) 2001-10-22 2009-08-12 Process to reduce the temperature of a hydrogen and carbon monoxide containing gas and heat exchanger for use in said process

Related Parent Applications (2)

Application Number Title Priority Date Filing Date
US10/493,328 Division US7597067B2 (en) 2001-10-22 2002-10-22 Process to reduce the temperature of a hydrogen and carbon monoxide containing gas and heat exchanger for use in said process
PCT/EP2002/011801 Division WO2003036165A2 (en) 2001-10-22 2002-10-22 Process to reduce the temperature of a hydrogen and carbon monoxide containing gas and heat exchanger for use in said process

Publications (1)

Publication Number Publication Date
US20090294103A1 true US20090294103A1 (en) 2009-12-03

Family

ID=8181114

Family Applications (3)

Application Number Title Priority Date Filing Date
US10/493,328 Active 2025-10-18 US7597067B2 (en) 2001-10-22 2002-10-22 Process to reduce the temperature of a hydrogen and carbon monoxide containing gas and heat exchanger for use in said process
US10/493,323 Expired - Fee Related US7422706B2 (en) 2001-10-22 2002-10-22 Process to prepare a hydrogen and carbon monoxide containing gas
US12/539,870 Abandoned US20090294103A1 (en) 2001-10-22 2009-08-12 Process to reduce the temperature of a hydrogen and carbon monoxide containing gas and heat exchanger for use in said process

Family Applications Before (2)

Application Number Title Priority Date Filing Date
US10/493,328 Active 2025-10-18 US7597067B2 (en) 2001-10-22 2002-10-22 Process to reduce the temperature of a hydrogen and carbon monoxide containing gas and heat exchanger for use in said process
US10/493,323 Expired - Fee Related US7422706B2 (en) 2001-10-22 2002-10-22 Process to prepare a hydrogen and carbon monoxide containing gas

Country Status (10)

Country Link
US (3) US7597067B2 (en)
EP (2) EP1438534B1 (en)
JP (2) JP4436675B2 (en)
AU (2) AU2002350598B2 (en)
GC (2) GC0000326A (en)
MY (2) MY138154A (en)
NO (2) NO20042088L (en)
RU (2) RU2300493C2 (en)
WO (2) WO2003036166A2 (en)
ZA (2) ZA200402448B (en)

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20110127469A1 (en) * 2009-11-30 2011-06-02 American Air Liquide, Inc. Process For Decreasing Or Eliminating Unwanted Hydrocarbon And Oxygenate Products Caused By Fisher Tropsch Synthesis Reactions In A Syngas Treatment Unit
WO2011066245A3 (en) * 2009-11-30 2011-07-21 L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process for decreasing or eliminating unwanted hydrocarbon and oxygenate products caused by fisher tropsch synthesis reactions in a syngas treatment unit
US20110207836A1 (en) * 2010-02-22 2011-08-25 L'Air Liquide Societe Anoyme Pour L'Etude Et L'Exploitation Des Procedes Georges Claude Process for decreasing or eliminating unwanted hydrocarbon and oxygenate products caused by fisher tropsch synthesis reactions in a syngas treatment unit

Families Citing this family (15)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US8603430B2 (en) * 2002-02-05 2013-12-10 The Regents Of The University Of California Controlling the synthesis gas composition of a steam methane reformer
US7125913B2 (en) 2003-03-14 2006-10-24 Conocophillips Company Partial oxidation reactors and syngas coolers using nickel-containing components
KR20050120719A (en) * 2003-04-15 2005-12-22 쉘 인터내셔날 리써취 마트샤피지 비.브이. Reactor for performing a steam reforming reaction and a process to prepare synthesis gas
JP4527426B2 (en) * 2004-03-25 2010-08-18 アイシン精機株式会社 Fuel reformer
EP1610081A1 (en) * 2004-06-25 2005-12-28 Haldor Topsoe A/S Heat exchange process and heat exchanger
WO2006037805A2 (en) 2004-10-08 2006-04-13 Shell Internationale Research Maatschappij B.V. Process to prepare ethylene and/or propylene from a carbon containing feedstock
KR101170198B1 (en) * 2004-11-18 2012-07-31 프랙스에어 테크놀로지, 인코포레이티드 Steam methane reforming method
US7037485B1 (en) * 2004-11-18 2006-05-02 Praxair Technology, Inc. Steam methane reforming method
US7354660B2 (en) 2005-05-10 2008-04-08 Exxonmobil Research And Engineering Company High performance alloys with improved metal dusting corrosion resistance
US7485767B2 (en) 2005-06-29 2009-02-03 Exxonmobil Chemical Patents Inc. Production of synthesis gas blends for conversion to methanol or Fischer-Tropsch liquids
US20070237710A1 (en) * 2006-04-05 2007-10-11 Genkin Eugene S Reforming apparatus and method for syngas generation
WO2007142739A2 (en) 2006-05-31 2007-12-13 Exxonmobil Chemical Patents Inc. Synthesis gas production and use
EP1995543A1 (en) * 2007-05-10 2008-11-26 AGC Flat Glass Europe SA Heat exchanger for oxygen
GB201115929D0 (en) 2011-09-15 2011-10-26 Johnson Matthey Plc Improved hydrocarbon production process
US20180155261A1 (en) * 2016-11-17 2018-06-07 Exxonmobil Research And Engineering Company Method for converting natural gas to dimethyl ether

Citations (22)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US488513A (en) * 1892-12-20 Joiin anderson
US2587530A (en) * 1948-03-13 1952-02-26 Rossi Giovanni Water and fire tube for steam boilers
US2820437A (en) * 1952-11-24 1958-01-21 Ilune Georges Heat-exchange evaporator apparatus
US3918410A (en) * 1974-06-19 1975-11-11 Handelsbolaget Broderna Backma Boiler for heating of water and generating of steam
US4132065A (en) * 1977-03-28 1979-01-02 Texaco Inc. Production of H2 and co-containing gas stream and power
US4433644A (en) * 1981-11-06 1984-02-28 Fitzpatrick James J Steam boilers
US4487744A (en) * 1982-07-28 1984-12-11 Carpenter Technology Corporation Corrosion resistant austenitic alloy
US4488513A (en) * 1983-08-29 1984-12-18 Texaco Development Corp. Gas cooler for production of superheated steam
US4505232A (en) * 1983-03-28 1985-03-19 Hitachi, Ltd. Boiler tube
US4536455A (en) * 1982-07-26 1985-08-20 Jgc Corporation Centrifugally cast double-layer tube with resistance to carbon deposition
US4685427A (en) * 1986-12-08 1987-08-11 Inco Alloys International, Inc. Alloy for composite tubing in fluidized-bed coal combustor
US4690690A (en) * 1985-03-05 1987-09-01 Imperial Chemical Industries Plc Steam reforming hydrocarbons
US4796570A (en) * 1986-08-26 1989-01-10 Shell Internationale Research Maatschappij B.V. Apparatus for heating steam formed from cooling water
US4827074A (en) * 1988-04-08 1989-05-02 Idemitsu Petrochemical Co., Ltd. Method of thermally decomposing hydrocarbon and thermal decomposition tube
US4876065A (en) * 1987-05-19 1989-10-24 Vdm Nickel-Technologie Aktiengesellschaft Corrosion-resisting Fe-Ni-Cr alloy
US5324595A (en) * 1991-08-21 1994-06-28 Sandvik Ab Composite tube
US5873950A (en) * 1996-06-13 1999-02-23 Inco Alloys International, Inc. Strengthenable ethylene pyrolysis alloy
US5945067A (en) * 1998-10-23 1999-08-31 Inco Alloys International, Inc. High strength corrosion resistant alloy
US6010581A (en) * 1994-05-18 2000-01-04 Sandvik Ab Austenitic Ni-based alloy with high corrosion resistance, good workability and structure stability
US6242112B1 (en) * 1996-09-05 2001-06-05 Sandvik Ab Use of a Ni-base alloy for compound tubes for combustion plants
US6329079B1 (en) * 1999-10-27 2001-12-11 Nooter Corporation Lined alloy tubing and process for manufacturing the same
US6337459B1 (en) * 1999-04-09 2002-01-08 Daido Tokushuko Kabushiki Kaisha Multi-layered anti-coking heat resisting metal tube and the method for manufacturing thereof

Family Cites Families (19)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2647041A (en) * 1946-04-15 1953-07-28 Phillips Petroleum Co Production of hydrogen from hydrocarbons
EP0082614B1 (en) * 1981-12-21 1986-07-23 Imperial Chemical Industries Plc Process for steam reforming a hydrocarbon feedstock and catalyst therefor
GB2163449B (en) * 1984-07-18 1988-06-02 Shell Int Research Production of gas mixtures containing hydrogen and carbon monoxide
US4919844A (en) * 1984-08-16 1990-04-24 Air Products And Chemicals, Inc. Enhanced heat transfer reformer and method
GB8711156D0 (en) 1987-05-12 1987-06-17 Shell Int Research Partial oxidation of hydrocarbon-containing fuel
DE3803082A1 (en) 1988-02-03 1989-08-17 Uhde Gmbh MULTI-STAGE PROCESS FOR GENERATING H (DOWN ARROW) 2 (DOWN ARROW) AND CO-CONTAINING SYNTHESIS GAS
US6274113B1 (en) * 1994-01-04 2001-08-14 Chevron Phillips Chemical Company Lp Increasing production in hydrocarbon conversion processes
MY115440A (en) 1994-07-22 2003-06-30 Shell Int Research A process for the manufacture of synthesis gas by partial oxidation of a gaseous hydrocarbon-containing fuel using a multi-orifice (co-annular)burner
CN1104625C (en) 1995-01-20 2003-04-02 国际壳牌研究有限公司 Apparatus for cooling solids laden hot gases
US6097990A (en) 1995-04-21 2000-08-01 Takekasa; Hitoshi Input device to input characters and symbols for recording characters and symbols on a film
EG20966A (en) 1995-06-06 2000-07-30 Shell Int Research A method for flame stabilization in a process for preparing synthesis gas
US5931978A (en) 1995-12-18 1999-08-03 Shell Oil Company Process for preparing synthesis gas
JP3104622B2 (en) 1996-07-15 2000-10-30 住友金属工業株式会社 Nickel-based alloy with excellent corrosion resistance and workability
US6247113B1 (en) * 1998-05-27 2001-06-12 Arm Limited Coprocessor opcode division by data type
DK173742B1 (en) * 1998-09-01 2001-08-27 Topsoe Haldor As Process and reactor system for producing synthesis gas
US6162267A (en) * 1998-12-11 2000-12-19 Uop Llc Process for the generation of pure hydrogen for use with fuel cells
DE19926402C1 (en) 1999-06-10 2000-11-02 Steinmueller Gmbh L & C Generating steam from gases produced by non-catalytic cracking of hydrocarbons comprises passing them through one tube of double-walled heat exchanger in water-filled container, with different fluid being passed through other tube
AU4090600A (en) * 1999-06-30 2001-01-04 Rohm And Haas Company High performance heat exchangers
DE10028824A1 (en) 2000-06-10 2001-12-13 Linde Ag Synthetic gas cooling process involves input of fresh water at least partly by topping up cooling water flow in circuit

Patent Citations (23)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US488513A (en) * 1892-12-20 Joiin anderson
US2587530A (en) * 1948-03-13 1952-02-26 Rossi Giovanni Water and fire tube for steam boilers
US2820437A (en) * 1952-11-24 1958-01-21 Ilune Georges Heat-exchange evaporator apparatus
US3918410A (en) * 1974-06-19 1975-11-11 Handelsbolaget Broderna Backma Boiler for heating of water and generating of steam
US4132065A (en) * 1977-03-28 1979-01-02 Texaco Inc. Production of H2 and co-containing gas stream and power
US4433644A (en) * 1981-11-06 1984-02-28 Fitzpatrick James J Steam boilers
US4536455A (en) * 1982-07-26 1985-08-20 Jgc Corporation Centrifugally cast double-layer tube with resistance to carbon deposition
US4487744A (en) * 1982-07-28 1984-12-11 Carpenter Technology Corporation Corrosion resistant austenitic alloy
US4505232A (en) * 1983-03-28 1985-03-19 Hitachi, Ltd. Boiler tube
US4488513A (en) * 1983-08-29 1984-12-18 Texaco Development Corp. Gas cooler for production of superheated steam
US4690690A (en) * 1985-03-05 1987-09-01 Imperial Chemical Industries Plc Steam reforming hydrocarbons
US4796570A (en) * 1986-08-26 1989-01-10 Shell Internationale Research Maatschappij B.V. Apparatus for heating steam formed from cooling water
US4685427A (en) * 1986-12-08 1987-08-11 Inco Alloys International, Inc. Alloy for composite tubing in fluidized-bed coal combustor
US4876065A (en) * 1987-05-19 1989-10-24 Vdm Nickel-Technologie Aktiengesellschaft Corrosion-resisting Fe-Ni-Cr alloy
US4827074A (en) * 1988-04-08 1989-05-02 Idemitsu Petrochemical Co., Ltd. Method of thermally decomposing hydrocarbon and thermal decomposition tube
US5324595A (en) * 1991-08-21 1994-06-28 Sandvik Ab Composite tube
US5324595B1 (en) * 1991-08-21 1998-08-25 Sandvik Ab Composite tube
US6010581A (en) * 1994-05-18 2000-01-04 Sandvik Ab Austenitic Ni-based alloy with high corrosion resistance, good workability and structure stability
US5873950A (en) * 1996-06-13 1999-02-23 Inco Alloys International, Inc. Strengthenable ethylene pyrolysis alloy
US6242112B1 (en) * 1996-09-05 2001-06-05 Sandvik Ab Use of a Ni-base alloy for compound tubes for combustion plants
US5945067A (en) * 1998-10-23 1999-08-31 Inco Alloys International, Inc. High strength corrosion resistant alloy
US6337459B1 (en) * 1999-04-09 2002-01-08 Daido Tokushuko Kabushiki Kaisha Multi-layered anti-coking heat resisting metal tube and the method for manufacturing thereof
US6329079B1 (en) * 1999-10-27 2001-12-11 Nooter Corporation Lined alloy tubing and process for manufacturing the same

Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20110127469A1 (en) * 2009-11-30 2011-06-02 American Air Liquide, Inc. Process For Decreasing Or Eliminating Unwanted Hydrocarbon And Oxygenate Products Caused By Fisher Tropsch Synthesis Reactions In A Syngas Treatment Unit
WO2011066245A3 (en) * 2009-11-30 2011-07-21 L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process for decreasing or eliminating unwanted hydrocarbon and oxygenate products caused by fisher tropsch synthesis reactions in a syngas treatment unit
US8163809B2 (en) 2009-11-30 2012-04-24 L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process for decreasing or eliminating unwanted hydrocarbon and oxygenate products caused by Fisher Tropsch Synthesis reactions in a syngas treatment unit
US8168687B2 (en) 2009-11-30 2012-05-01 L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process for decreasing or eliminating unwanted hydrocarbon and oxygenate products caused by Fisher Tropsch synthesis reactions in a syngas treatment unit
US20110207836A1 (en) * 2010-02-22 2011-08-25 L'Air Liquide Societe Anoyme Pour L'Etude Et L'Exploitation Des Procedes Georges Claude Process for decreasing or eliminating unwanted hydrocarbon and oxygenate products caused by fisher tropsch synthesis reactions in a syngas treatment unit
US8202914B2 (en) 2010-02-22 2012-06-19 L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process for decreasing or eliminating unwanted hydrocarbon and oxygenate products caused by Fisher Tropsch Synthesis reactions in a syngas treatment unit

Also Published As

Publication number Publication date
WO2003036166A3 (en) 2003-10-23
US20040262579A1 (en) 2004-12-30
AU2002350598B2 (en) 2007-04-26
RU2004115603A (en) 2005-05-20
AU2002350595B2 (en) 2008-01-31
US20040241086A1 (en) 2004-12-02
EP1438259A2 (en) 2004-07-21
MY138154A (en) 2009-04-30
WO2003036166A2 (en) 2003-05-01
WO2003036165A3 (en) 2003-10-23
GC0000326A (en) 2006-11-01
JP2005506443A (en) 2005-03-03
WO2003036165A2 (en) 2003-05-01
US7597067B2 (en) 2009-10-06
NO20042086L (en) 2004-05-21
US7422706B2 (en) 2008-09-09
NO20042088L (en) 2004-05-21
MY136087A (en) 2008-08-29
JP4436675B2 (en) 2010-03-24
RU2293912C2 (en) 2007-02-20
EP1438534B1 (en) 2012-11-14
RU2300493C2 (en) 2007-06-10
GC0000404A (en) 2007-03-31
EP1438534A2 (en) 2004-07-21
RU2004115633A (en) 2005-05-27
ZA200402707B (en) 2005-02-23
JP2005515140A (en) 2005-05-26
ZA200402448B (en) 2006-05-31

Similar Documents

Publication Publication Date Title
US20090294103A1 (en) Process to reduce the temperature of a hydrogen and carbon monoxide containing gas and heat exchanger for use in said process
AU2002350595A1 (en) Process to reduce the temperature of a hydrogen and carbon monoxide containing gas and heat exchanger for use in said process
CA2711415C (en) Carburization resistant metal material
US10207242B2 (en) Alumina forming refinery process tubes with mixing element
AU2002350598A1 (en) Process to prepare a hydrogen and carbon monoxide containing gas
Tillack et al. Wrought and cast heat-resistant stainless steels and nickel alloys for the refining and petrochemical industries
CA3075483C (en) Aluminum oxide forming heat transfer tube for thermal cracking
JPS594971A (en) Build up welding
US4532109A (en) Process for providing an apparatus for treating hydrocarbons or the like at high temperatures substantially without carbon deposition
KR102382225B1 (en) Method for producing aromatic hydrocarbons
CA3124057C (en) Erosion resistant alloy for thermal cracking reactors
US11124717B1 (en) Hydroprocessing units and methods for preventing corrosion in hydroprocessing units
JPS5829355B2 (en) Hydrocarbon pyrolysis equipment
Mahajanam et al. CRA Failures in Refining Operations
GB2114599A (en) Apparatus for treating hydrocarbons or carbon monoxide-containing fluid at high temperatures substantially without carbon deposition
Watanabe A review of 28 years of work of the Japan welding engineering society's committee of chemical plant welding (CCPW)

Legal Events

Date Code Title Description
STCB Information on status: application discontinuation

Free format text: ABANDONED -- AFTER EXAMINER'S ANSWER OR BOARD OF APPEALS DECISION