US3195989A - Integral tube furnace and oxidizer - Google Patents
Integral tube furnace and oxidizer Download PDFInfo
- Publication number
- US3195989A US3195989A US208265A US20826562A US3195989A US 3195989 A US3195989 A US 3195989A US 208265 A US208265 A US 208265A US 20826562 A US20826562 A US 20826562A US 3195989 A US3195989 A US 3195989A
- Authority
- US
- United States
- Prior art keywords
- tube
- chamber
- oxidizer
- vessel
- reformer
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Lifetime
Links
Images
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
- C01B3/382—Multi-step processes
-
- 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
- B01J19/24—Stationary reactors without moving elements inside
- B01J19/2415—Tubular reactors
- B01J19/2425—Tubular reactors in parallel
-
- 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
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/06—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds in tube reactors; the solid particles being arranged in tubes
- B01J8/062—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds in tube reactors; the solid particles being arranged in tubes being installed in a furnace
-
- 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
-
- 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
-
- 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
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
- B01J2208/00327—Controlling the temperature by direct heat exchange
- B01J2208/00336—Controlling the temperature by direct heat exchange adding a temperature modifying medium to the reactants
- B01J2208/00353—Non-cryogenic fluids
- B01J2208/00362—Liquid
-
- 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
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
- B01J2208/00477—Controlling the temperature by thermal insulation means
- B01J2208/00495—Controlling the temperature by thermal insulation means using insulating materials or refractories
-
- 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
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
- B01J2208/00504—Controlling the temperature by means of a burner
-
- 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
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
- B01J2208/0053—Controlling multiple zones along the direction of flow, e.g. pre-heating and after-cooling
-
- 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
- C01B2203/025—Processes for making hydrogen or synthesis gas containing a partial oxidation step
- C01B2203/0261—Processes for making hydrogen or synthesis gas containing a partial oxidation step containing a catalytic partial oxidation step [CPO]
-
- 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
- C01B2203/0811—Methods of heating the process for making hydrogen or synthesis gas by combustion of fuel
-
- 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
- C01B2203/0811—Methods of heating the process for making hydrogen or synthesis gas by combustion of fuel
- C01B2203/0816—Heating by flames
-
- 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
- C01B2203/0866—Methods of heating the process for making hydrogen or synthesis gas by combination of different heating methods
-
- 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
- C01B2203/0877—Methods of cooling by direct injection of fluid
-
- 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
- C01B2203/1052—Nickel or cobalt 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
-
- 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
- C01B2203/12—Feeding the process for making hydrogen or synthesis gas
- C01B2203/1205—Composition of the feed
- C01B2203/1211—Organic compounds or organic mixtures used in the process for making hydrogen or synthesis gas
- C01B2203/1235—Hydrocarbons
- C01B2203/1241—Natural gas or methane
-
- 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
- C01B2203/16—Controlling the process
- C01B2203/1695—Adjusting the feed of the 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
- C01B2203/80—Aspect of integrated processes for the production of hydrogen or synthesis gas not covered by groups C01B2203/02 - C01B2203/1695
- C01B2203/82—Several process steps of C01B2203/02 - C01B2203/08 integrated into a single apparatus
Definitions
- This invention relates to furnaces with catalyst filled tubes used in reforming light hydrocarbons to produce hydrogen and carbon monoxide mixtures. More particularly, the invention contemplates a reformer tube having an oxidizer integrally formed therewith.
- Prior reformer systems have included the oxidizer as a separate unit downstream from the tube furnace. Such an arrangement leaves a hiatus in .the flow stream between the furnace and the oxidizer wherein unpredictable and sometimes undesired reactions take place. It is an object of this invention to eliminate these reactions.
- Gas from the reformer furnace could be cooled in order to prevent undesired reactions, however, unless cooling is rapid there is jeopardy of excessive carbon deposition. Rapid quenching at the furnace outlet has been employed to quickly cool the gas through the critical carbon deposition temperature range. But cooling has imposed thermal shock problems and has penalized oxidizer performance by necessitating operation at reduced temperatures.
- the present invention contemplates an apparatus ca pable of combining primary reformation and subsequent oxidation in a single unit.
- this teaching offers the direct availability of reformer furnace product gas for oxidation at a high temperature. Intermediate piping has been eliminated. Geometries in the lower regions of tube furnaces are Well suited to accommodating oxidizers. Additionally, the present advance gives rise to more compact systems occupying little ground area. Maintenance opportunities arise from the possibility of repairing or removing some of the oxidizers while others are on stream.
- FIGURE I is an isometric view of a preferred embodiment of a reformer furnace with oxidizers mounted therein.
- FIGURE II is an enlarged sectional elevation view depicting one reformer tube and its secondary oxidizer.
- FIGURE III is sectional elevation view of a reformer and its corresponding secondary oxidizer according to a second embodiment with a quench apparatus mounted therein.
- FIGURE IV is a broken sectional elevation view depicting the oxidizer exit with a quench boot.
- Natural gas, methane or any normally gaseous hydrocarbon containing one to four carbon atoms in its molecule and which is of satisfactory low sulfur content may serve as the feed gas. In some cases it may be economical to use a narrow boiling gasoline fraction. (Then special catalysts might be necessary and high steam to carbon ratios would be used to resist coke deposition from higher boiling hydrocarbons.)
- CO may be desulfurized by bubbling it through a potassium permanganate solution (KMnO With a methane feed tube furnaces are generally oper ated with from 1.8 to 9.0 moles of oxidant per mole of product H Inlet pressures from atmospheric to 400 p.s.i.g., preheat temperature from 500 F. to 1000 F., heater zone outlet temperatures from 1450" F. to 2300 F. and space velocities from 500 to 5000 standard cubic feet of theoretical H yield per hour per cubic foot of catalyst are usually employed.
- preheat temperature from 500 F. to 1000 F.
- heater zone outlet temperatures from 1450" F. to 2300 F.
- space velocities from 500 to 5000 standard cubic feet of theoretical H yield per hour per cubic foot of catalyst are usually employed.
- FIGURE 1 the mixture of hydrocarbon and oxidant is passed through preheater tubes 2 wherein it is preheated by flue gases. Thereafter, the feed gas is transmittcd via inlet manifold 3 and flexible inlet conduits 4 to reformer tubes 6 which are positioned by support means shown as counterweight 7 and pulleys 8.
- Reformer furnace 1 includes a setting generally designated 9 which has roof 11 and floor 12 slidably penetrated by tubes 6.
- Setting 9 defines heater zone 13 embraced by a pair of stepped oppositely disposed side walls 14.
- Above steps 16 each side Wall 14 slopes inwards upwardly so that the side walls define a number of coplanar surfaces faced with refractory material.
- Each refractory surface has a bottom 17 and an upper extremity 18.
- the cross section of heater zone 13, although being gener ally rectangular is substantially that produced by the outline of a number of regular trapezoids stacked large base on small base with a common axis of symmetry.
- heater means shown as sets of linear burners 19 which project their flame streams through longitudinal troughs 21 upward each to sweep on associated coplanar surface.
- each of these surfaces can be uniformly heated to evenly emit radiation therefrom.
- Inner rims Z2 divert the streams of flame away from direct impingement onto tubes 6.
- Control means are associated with each burner to regulate the intensity of heat flux input.
- Control means are associated with each burner to regulate the intensity of heat flux input.
- the catalyst in the furnace tubes employed to produce synthesis gas is suitably a nickel catalyst, such as reduced nickel oxide, nickel-thoria-magnesia, nickel-alumina-magnesia, nickel-magnesia, nickel on carbon, or nickel on alumina.
- nickel catalysts may include cobalt molybdate supported on alumina, a group VIII metal on metal oxide on a suitable support, nickel and iron on a support or carrier, and the like.
- Secondary shell 27 has upper end 28 and lower end 29 and contains oxidizer catalyst which can be the same as that used for the reformer catalyst.
- an oxygen containing gas is supplied to each oxidizer from manifold 31 via oxygen conduit 32 and oxygen port 33.
- the oxygen content of this gas generally depends upon the degree to which the elimination of diluent nitrogen from the hydro gen stream is required. 7
- exit port 354 communicates with annular space 36 between shell 27 and tube 6 in the vicinity of upper end 28 of the shell to conduct the gas to outlet manifold 37.
- FIGURES III and IV the product gas exits via quench chamber 38 formed by quench housing 39. Cooling means are shown in FIGURE III as spray 41 and in FIGURE IV as bath 42.
- oxidizer shells 27 are embraced by refractory enclosure 43.
- a reformer system which includes a primary reformer and oxidizer for use in the production of hydrogen and hydrogen and carbon monoxide mixtures from a hydrocarbon comprising in combination wall means defining an enclosed heating chamber;
- At least one tube positioned to extend through said chamber defining a primary reformer reaction zone
- inlet means for introducing a feed comprising hydrocarbon and an oxidant into said tube, said tube containing a suitable catalyst;
- heater means heating said chamber to heat said tube
- vessel means connected in flow series with said tube to receive substantially reformed gas from the tube, said vessel means containing a catalyst and defining an oxidizer reaction zone;
- a refractory enclosure entirely encompassing said vessel means and separating said vessel means from said heating chamber and from ambient conditions, said enclosure including a refractory wall common with said heating chamber wall means penetrated by said tube;
- a reformer system which includes a primary reformer and oxidizer for use in the production of hydrogen and hydrogen and carbon monoxide mixtures from a hydrocarbon comprising in combination wall means having end and side walls defining an enclosed first chamber;
- enclosure means having refractory end and side walls adjacent said first chamber defining an enclosed second chamber, the second chamber being separated from the first chamber by a refractory wall common to both said chambers and from ambient conditions 7 by said end and side walls;
- a plurality of tubes defining heated primary reformer reaction zones positioned to extend through the first chamber and into the second chamber;
- heater means heating the first chamber to heat the tubes in the chamber; inlet means for introducing a feed comprising a hydocarbon and an oxidant into said tubes, said tubes 4 to receive substantially reformed gas from the tubes, said vessel means containing a catalyst and defining an oxidizer reaction Zone; said vessel means being disposed within said second chamber the enclosure means thereof encompassing said vessel means and separating the vessel means for the first chamber and from ambient conditions;
- a reformer system which includes a primary reformer and oxidizer for use in the production of hydrogen and hydrogen and carbon monoxide mixtures from a hydrocarbon comprising in combination wall means including side walls and roof and floor walls defining an elongated enclosed upright first chamber; enclosure means having refractory end and side walls adjacent and below said first chamber defining an enclosed second chamber, the second chamber being separated from said first chamber by a refractory wall which is common with the floor of the first chamber;
- At least one straight tube defining a heated primary reformer reaction zone having an upstream end and a downstream end;
- conduit means communicating with a source of feed comprising a hydrocarbon and an oxidant conncted to the upstream end of the tube to deliver the feed thereto, the tube containing a suitable primary reformer catalyst;
- V 1 a plurality of burners penetrating said refractory surfaces to introduce streams of flames which sweep said refractory surfaces heating the surfaces to radiate energy to said tube; vessel connected in flow series with said tube to receive substantially reformed gas from the tube, said vessel containing a catalyst and defining an oxidizer reactionzone, said vessel being disposed within the second chamber, the enclosure means thereof encompassing the vessel and separating the vessel from the first chamber and from ambient conditions; means for introducing an oxygen containing gas into said v'esselnear the upstream end of the vessel for oxidizing unconverted hydrocarbon therein; and outlet means for exhausting product gas from the vessel.
- V 1 a plurality of burners penetrating said refractory surfaces to introduce streams of flames which sweep said refractory surfaces heating the surfaces to radiate energy to said tube
- vessel connected in flow series with said tube to receive substantially reformed gas from the tube, said vessel containing a catalyst and defining an oxidizer reactionzone, said vessel being disposed within the second chamber, the
Landscapes
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Health & Medical Sciences (AREA)
- General Health & Medical Sciences (AREA)
- Inorganic Chemistry (AREA)
- Hydrogen, Water And Hydrids (AREA)
- Catalysts (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Description
F. M. PYZEL INTEGRAL TUBE FURNACE AND OXIDIZER July 20, 1965 2 Sheets-Sheet 1 Filed July 9, 1962 INVENTOR FPED/P/CA M PYZfL ATTORNEY July 20, 1965 F. M. PYZEL INTEGRAL TUBE FURNACE AND OXIDIZER 2 Sheets-Sheet 2 til Filed July 9, 1962 INVENTOR FQED/e/cK M P zq wi ATTORNEY United States Patent 3,195,989 INTEGRAL TUBE FURNACE AND ()XIDIZER Frederick M. Pyzel, Rye, N.Y., assignor to Foster Wheeler Corporation, New York, N.Y., a corporation of New York Filed July 9, 1962, do. No. 208,265 3 Claims. (all. 23-288) This invention relates to furnaces with catalyst filled tubes used in reforming light hydrocarbons to produce hydrogen and carbon monoxide mixtures. More particularly, the invention contemplates a reformer tube having an oxidizer integrally formed therewith.
A typical reforming process involved in this apparatus is represented by the following equation for methane:
CH4 H20 H2 This equation merely characterizes the main reaction performed. In actual practice, CO might also be added as an oxidant. Complete conversion is not obtained nor is the selectivity toward CO formation 100 percent as indicated by the idealized equation. In any event, unconverted hydrocarbon appears in the product gas.
To increase H and CO yield, the furnace is followed by an oxidizing step wherein partial combustion of unconverted hydrocarbon may be represented for methane by the following equation:
This reaction is exotherrnal.
Prior reformer systems have included the oxidizer as a separate unit downstream from the tube furnace. Such an arrangement leaves a hiatus in .the flow stream between the furnace and the oxidizer wherein unpredictable and sometimes undesired reactions take place. It is an object of this invention to eliminate these reactions.
Gas from the reformer furnace could be cooled in order to prevent undesired reactions, however, unless cooling is rapid there is jeopardy of excessive carbon deposition. Rapid quenching at the furnace outlet has been employed to quickly cool the gas through the critical carbon deposition temperature range. But cooling has imposed thermal shock problems and has penalized oxidizer performance by necessitating operation at reduced temperatures.
The present invention contemplates an apparatus ca pable of combining primary reformation and subsequent oxidation in a single unit.
Basically, this teaching offers the direct availability of reformer furnace product gas for oxidation at a high temperature. Intermediate piping has been eliminated. Geometries in the lower regions of tube furnaces are Well suited to accommodating oxidizers. Additionally, the present advance gives rise to more compact systems occupying little ground area. Maintenance opportunities arise from the possibility of repairing or removing some of the oxidizers while others are on stream.
These and other features will appear more fully from the accompanying drawings wherein:
FIGURE I is an isometric view of a preferred embodiment of a reformer furnace with oxidizers mounted therein.
FIGURE II is an enlarged sectional elevation view depicting one reformer tube and its secondary oxidizer.
FIGURE III is sectional elevation view of a reformer and its corresponding secondary oxidizer according to a second embodiment with a quench apparatus mounted therein.
FIGURE IV is a broken sectional elevation view depicting the oxidizer exit with a quench boot.
ice
Natural gas, methane or any normally gaseous hydrocarbon containing one to four carbon atoms in its molecule and which is of satisfactory low sulfur content may serve as the feed gas. In some cases it may be economical to use a narrow boiling gasoline fraction. (Then special catalysts might be necessary and high steam to carbon ratios would be used to resist coke deposition from higher boiling hydrocarbons.)
In advance of the reformer furnace 1 it is often necessary to desulfurize the hydrocarbon by contact with activated carbon. Analogously, CO may be desulfurized by bubbling it through a potassium permanganate solution (KMnO With a methane feed tube furnaces are generally oper ated with from 1.8 to 9.0 moles of oxidant per mole of product H Inlet pressures from atmospheric to 400 p.s.i.g., preheat temperature from 500 F. to 1000 F., heater zone outlet temperatures from 1450" F. to 2300 F. and space velocities from 500 to 5000 standard cubic feet of theoretical H yield per hour per cubic foot of catalyst are usually employed.
In FIGURE 1, the mixture of hydrocarbon and oxidant is passed through preheater tubes 2 wherein it is preheated by flue gases. Thereafter, the feed gas is transmittcd via inlet manifold 3 and flexible inlet conduits 4 to reformer tubes 6 which are positioned by support means shown as counterweight 7 and pulleys 8.
Along steps 16 are arranged heater means shown as sets of linear burners 19 which project their flame streams through longitudinal troughs 21 upward each to sweep on associated coplanar surface. Thus, each of these surfaces can be uniformly heated to evenly emit radiation therefrom. Inner rims Z2 divert the streams of flame away from direct impingement onto tubes 6.
Control means (not shown) are associated with each burner to regulate the intensity of heat flux input. By altering the firing rate of any set of paired burners disposed at the same elevation in steps 16, different levels of reformer tubes 6 can be subjected uniformly to heat flux intensities. With temperature gradient reducing down the tubes, it is usual to add from 50 to 65 percent of the total heat influx to the tubes in upper level 23, 25 to 40 percent in middle level 24 and the balance in lower level 26.
The catalyst in the furnace tubes employed to produce synthesis gas is suitably a nickel catalyst, such as reduced nickel oxide, nickel-thoria-magnesia, nickel-alumina-magnesia, nickel-magnesia, nickel on carbon, or nickel on alumina. Other suitable catalysts may include cobalt molybdate supported on alumina, a group VIII metal on metal oxide on a suitable support, nickel and iron on a support or carrier, and the like.
The substantially reformed gas leaving catalyst tubes 6 passes into secondary shell 27. Secondary shell 27 has upper end 28 and lower end 29 and contains oxidizer catalyst which can be the same as that used for the reformer catalyst. v
As best seen from FIGURES II and III, an oxygen containing gas is supplied to each oxidizer from manifold 31 via oxygen conduit 32 and oxygen port 33. The oxygen content of this gas generally depends upon the degree to which the elimination of diluent nitrogen from the hydro gen stream is required. 7
Throughout the figures the same numerals indicate like elements. In FIGURE II, exit port 354 communicates with annular space 36 between shell 27 and tube 6 in the vicinity of upper end 28 of the shell to conduct the gas to outlet manifold 37. Furnace tubes 6 are .gen= 'erally spaced at two diameters center to center. If there is fear of crowding the secondary shells alternate tubes can be kneed to opposite sides (as shown in FIGURE III) to accommodate more compact geometries.
In the embodiment of FIGURES III and IV the product gas exits via quench chamber 38 formed by quench housing 39. Cooling means are shown in FIGURE III as spray 41 and in FIGURE IV as bath 42.
' As shown in FIGURE I, oxidizer shells 27 are embraced by refractory enclosure 43.
It will be understood by those skilled in steam reforming and related equipment that wide changes may be made in the details of this system without departing from the main theme of invention defined by the claims.
What is claimed is:
1. .A reformer system which includes a primary reformer and oxidizer for use in the production of hydrogen and hydrogen and carbon monoxide mixtures from a hydrocarbon comprising in combination wall means defining an enclosed heating chamber;
at least one tube positioned to extend through said chamber defining a primary reformer reaction zone;
support means for positioning the tube;
inlet means for introducing a feed comprising hydrocarbon and an oxidant into said tube, said tube containing a suitable catalyst;
heater means heating said chamber to heat said tube;
vessel means connected in flow series with said tube to receive substantially reformed gas from the tube, said vessel means containing a catalyst and defining an oxidizer reaction zone;
' a refractory enclosure entirely encompassing said vessel means and separating said vessel means from said heating chamber and from ambient conditions, said enclosure including a refractory wall common with said heating chamber wall means penetrated by said tube;
means for introducing an oxygen containing gas into said vessel means'near the upstream end thereof to react with unconverted hydrocarbon therein;
and outlet means for exhausting product gas from said vessel means.
2. A reformer system which includes a primary reformer and oxidizer for use in the production of hydrogen and hydrogen and carbon monoxide mixtures from a hydrocarbon comprising in combination wall means having end and side walls defining an enclosed first chamber;
enclosure means having refractory end and side walls adjacent said first chamber defining an enclosed second chamber, the second chamber being separated from the first chamber by a refractory wall common to both said chambers and from ambient conditions 7 by said end and side walls; v
a plurality of tubes defining heated primary reformer reaction zones positioned to extend through the first chamber and into the second chamber;
support means for positioning said tubes;
heater means heating the first chamber to heat the tubes in the chamber; inlet means for introducing a feed comprising a hydocarbon and an oxidant into said tubes, said tubes 4 to receive substantially reformed gas from the tubes, said vessel means containing a catalyst and defining an oxidizer reaction Zone; said vessel means being disposed within said second chamber the enclosure means thereof encompassing said vessel means and separating the vessel means for the first chamber and from ambient conditions;
means for introducing an oxygen containing gas into said vessel means near the upstream ends thereof to react with unconverted hydrocarbon therein;
and outlet means for exhausting product gas from said vessel means. 7
3. A reformer system which includes a primary reformer and oxidizer for use in the production of hydrogen and hydrogen and carbon monoxide mixtures from a hydrocarbon comprising in combination wall means including side walls and roof and floor walls defining an elongated enclosed upright first chamber; enclosure means having refractory end and side walls adjacent and below said first chamber defining an enclosed second chamber, the second chamber being separated from said first chamber by a refractory wall which is common with the floor of the first chamber;
at least one straight tube defining a heated primary reformer reaction zone having an upstream end and a downstream end;
means supporting said tube vertically to extend length wise through the first chamber with the upstream end slidably penetrating through the roof of the chamber and the downstream end slidably penetrating through the floor of the chamber into the second chamber;
conduit means communicating with a source of feed comprising a hydrocarbon and an oxidant conncted to the upstream end of the tube to deliver the feed thereto, the tube containing a suitable primary reformer catalyst;
refractory surfaces in said first chamber on opposite sides of said tube;
a plurality of burners penetrating said refractory surfaces to introduce streams of flames which sweep said refractory surfaces heating the surfaces to radiate energy to said tube; vessel connected in flow series with said tube to receive substantially reformed gas from the tube, said vessel containing a catalyst and defining an oxidizer reactionzone, said vessel being disposed within the second chamber, the enclosure means thereof encompassing the vessel and separating the vessel from the first chamber and from ambient conditions; means for introducing an oxygen containing gas into said v'esselnear the upstream end of the vessel for oxidizing unconverted hydrocarbon therein; and outlet means for exhausting product gas from the vessel. V 1
References Cited by the Examiner V UNITED STATES PATENTS 2,338,295 1/44 Mekler 122356 2,638,879 5/53 Hess 122-356 2,660,519 11/53 McCarthy 23288.92 2,667,410 1/54 Pierce 28-288.92 X 2,700,598 1/55 Odell 48-215 X 2,818,326 12/57 Eastman et al. 48215 X 2,894,826 7/59 Stengel 23288.92 3,062,197 11/62 Fleischer.
FOREIGN PATENTS 596,819 4/60 Canada. I
MORRISO. WOLK, Primary Examiner.
Claims (1)
1. A REFORMER SYSTEM WHICH INCLUDES A PRIMARY REFORMER AND OXIDIZER FOR USE IN THE PRODUCTION OF HYDROGEN AND HYDROGEN AND CARBON MONOXIDE MIXTURES FROM A HYDROCARBON COMPRISING IN COMBINATION WALL MEANS DEFINING AN ENCLOSED HEATING CHAMBER; AT LEAST ONE TUBE POSITIONED TO EXTEND THROUGH SAID CHAMBER DEFINING A PRIMARY REFORMER REACTION ZONE; SUPPORT MEANS FOR POSITIONING THE TUBE; INLET MEANS FOR INTRODUCING A FEED COMPRISING HYDROCARBON AND AN OXIDANT INTO SAID TUBE, SAID TUBE CONTAINING A SUITABLE CATALYST; HEATER MEANS HEATING SAID CHAMBER TO HEAT SAID TUBE; VESSEL MEANS CONNECTED IN FLOW SERIES WITH SAID TUBE TO RECEIVE SUBSTANTIALLY REFORMED GAS FROM THE TUBE, SAID VESSEL MEANS CONTAINING A CATALYST AND DEFINING AN OXIDIZER REACTION ZONE; A REFRACTORY ENCLOSURE ENTIRELY ENCOMPASSING SAID VESSEL MEANS AND SEPARATING SAID VESSEL MEANS FROM SAID HEATING CHAMBER AND FROM AMBIENT CONDITIONS, SAID ENCLOSURE INCLUDING A REFRACTORY WALL COMMON WITH SAID HEATING CHAMBER WALL MEANS PENETRATED BY SAID TUBE; MEANS FOR INTRODUCING AN OXYGEN CONTAINING GAS INTO
Priority Applications (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US208265A US3195989A (en) | 1962-07-09 | 1962-07-09 | Integral tube furnace and oxidizer |
| GB27148/63A GB1047627A (en) | 1962-07-09 | 1963-07-09 | Improvements in or relating to the reformation of light hydrocarbon feeds |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US208265A US3195989A (en) | 1962-07-09 | 1962-07-09 | Integral tube furnace and oxidizer |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| US3195989A true US3195989A (en) | 1965-07-20 |
Family
ID=22773939
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| US208265A Expired - Lifetime US3195989A (en) | 1962-07-09 | 1962-07-09 | Integral tube furnace and oxidizer |
Country Status (2)
| Country | Link |
|---|---|
| US (1) | US3195989A (en) |
| GB (1) | GB1047627A (en) |
Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3267915A (en) * | 1965-06-11 | 1966-08-23 | Foster Wheeler Corp | Fired heater |
| US3269465A (en) * | 1964-08-03 | 1966-08-30 | Lummus Co | Process heater |
| US3274978A (en) * | 1964-02-24 | 1966-09-27 | Lummus Co | Vertical tube fluid heater |
| US3348923A (en) * | 1965-10-01 | 1967-10-24 | Foster Wheeler Corp | Tube design for terrace wall furnace |
| US3361118A (en) * | 1966-04-08 | 1968-01-02 | Selas Corp Of America | Tube heater |
| US3419362A (en) * | 1965-06-25 | 1968-12-31 | Chemical Construction Corp | Fluid heater |
| US3475135A (en) * | 1963-10-24 | 1969-10-28 | App Eau Gaz Ind Const | Reforming furnace for producing synthesis gas |
| US3479166A (en) * | 1964-05-01 | 1969-11-18 | John H Hirt | Apparatus for producing gases of predetermined characteristics |
| US3532472A (en) * | 1967-03-20 | 1970-10-06 | Shell Oil Co | Apparatus for carrying out partial oxidation of organic compounds |
| US4499055A (en) * | 1981-09-14 | 1985-02-12 | Exxon Research & Engineering Co. | Furnace having bent/single-pass tubes |
| US20070234974A1 (en) * | 2006-04-10 | 2007-10-11 | The Cust-O-Fab Companies, Llc | Fired heater and flue gas tunnel therefor |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH01261201A (en) * | 1988-04-12 | 1989-10-18 | Mitsubishi Gas Chem Co Inc | Hydrocarbon reforming reactor |
| JPH0218303A (en) * | 1988-07-07 | 1990-01-22 | Mitsubishi Gas Chem Co Inc | Reactor and process for reforming hydrocarbon |
Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2338295A (en) * | 1941-04-25 | 1944-01-04 | Universal Oil Prod Co | Heating of fluids |
| US2638879A (en) * | 1947-06-30 | 1953-05-19 | Selas Corp Of America | Apparatus for heat treatment of fluent substances |
| US2660519A (en) * | 1948-04-23 | 1953-11-24 | Chemical Construction Corp | Fluid heater |
| US2667410A (en) * | 1950-01-04 | 1954-01-26 | Phillips Petroleum Co | Apparatus for reforming hydrocarbons |
| US2700598A (en) * | 1946-10-31 | 1955-01-25 | Standard Oil Dev Co | Process for reforming hydrocarbons |
| US2818326A (en) * | 1956-08-07 | 1957-12-31 | Texas Co | Method of shutting down the gas generator |
| US2894826A (en) * | 1957-12-09 | 1959-07-14 | Commercial Solvents Corp | Apparatus for reforming hydrocarbons |
| CA596819A (en) * | 1960-04-26 | Bliss Charles | Fluid heater | |
| US3062197A (en) * | 1959-07-23 | 1962-11-06 | Selas Corp Of America | Tube heater |
-
1962
- 1962-07-09 US US208265A patent/US3195989A/en not_active Expired - Lifetime
-
1963
- 1963-07-09 GB GB27148/63A patent/GB1047627A/en not_active Expired
Patent Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CA596819A (en) * | 1960-04-26 | Bliss Charles | Fluid heater | |
| US2338295A (en) * | 1941-04-25 | 1944-01-04 | Universal Oil Prod Co | Heating of fluids |
| US2700598A (en) * | 1946-10-31 | 1955-01-25 | Standard Oil Dev Co | Process for reforming hydrocarbons |
| US2638879A (en) * | 1947-06-30 | 1953-05-19 | Selas Corp Of America | Apparatus for heat treatment of fluent substances |
| US2660519A (en) * | 1948-04-23 | 1953-11-24 | Chemical Construction Corp | Fluid heater |
| US2667410A (en) * | 1950-01-04 | 1954-01-26 | Phillips Petroleum Co | Apparatus for reforming hydrocarbons |
| US2818326A (en) * | 1956-08-07 | 1957-12-31 | Texas Co | Method of shutting down the gas generator |
| US2894826A (en) * | 1957-12-09 | 1959-07-14 | Commercial Solvents Corp | Apparatus for reforming hydrocarbons |
| US3062197A (en) * | 1959-07-23 | 1962-11-06 | Selas Corp Of America | Tube heater |
Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3475135A (en) * | 1963-10-24 | 1969-10-28 | App Eau Gaz Ind Const | Reforming furnace for producing synthesis gas |
| US3274978A (en) * | 1964-02-24 | 1966-09-27 | Lummus Co | Vertical tube fluid heater |
| US3479166A (en) * | 1964-05-01 | 1969-11-18 | John H Hirt | Apparatus for producing gases of predetermined characteristics |
| US3269465A (en) * | 1964-08-03 | 1966-08-30 | Lummus Co | Process heater |
| US3267915A (en) * | 1965-06-11 | 1966-08-23 | Foster Wheeler Corp | Fired heater |
| US3419362A (en) * | 1965-06-25 | 1968-12-31 | Chemical Construction Corp | Fluid heater |
| US3348923A (en) * | 1965-10-01 | 1967-10-24 | Foster Wheeler Corp | Tube design for terrace wall furnace |
| US3361118A (en) * | 1966-04-08 | 1968-01-02 | Selas Corp Of America | Tube heater |
| US3532472A (en) * | 1967-03-20 | 1970-10-06 | Shell Oil Co | Apparatus for carrying out partial oxidation of organic compounds |
| US4499055A (en) * | 1981-09-14 | 1985-02-12 | Exxon Research & Engineering Co. | Furnace having bent/single-pass tubes |
| US20070234974A1 (en) * | 2006-04-10 | 2007-10-11 | The Cust-O-Fab Companies, Llc | Fired heater and flue gas tunnel therefor |
Also Published As
| Publication number | Publication date |
|---|---|
| GB1047627A (en) | 1966-11-09 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US4079017A (en) | Parallel steam reformers to provide low energy process | |
| US4162290A (en) | Parallel steam reformers to provide low energy process | |
| US3195989A (en) | Integral tube furnace and oxidizer | |
| US4678600A (en) | Heat exchange reforming process and reactor | |
| US5112578A (en) | Reactor for reforming hydrocarbon and process for reforming hydrocarbon | |
| US4650651A (en) | Integrated process and apparatus for the primary and secondary catalytic steam reforming of hydrocarbons | |
| US7255840B2 (en) | Autothermal reactor and method for production of synthesis gas | |
| RU2560363C2 (en) | Hydrocarbon reforming method | |
| EP0033128B1 (en) | Catalytic steam reforming of hydrocarbons | |
| US2655442A (en) | Process and apparatus for the manufacture of synthesis gas | |
| GB2181740A (en) | Generation of synthesis gas | |
| EP0242199A1 (en) | Process and apparatus for the production of synthesis gas | |
| JPS6158801A (en) | Method of improving hydrocarbon and reactor | |
| NO168574B (en) | PROCEDURE FOR THE PREPARATION OF A PRODUCT GAS CURRENT CONTAINING HYDROGEN AND CARBONOXIDE | |
| JPH0522641B2 (en) | ||
| EA000777B1 (en) | Process and process unit for the preparation of ammonia synthesis gas | |
| KR102441364B1 (en) | CO-enriched syngas production | |
| JPS59107901A (en) | Manufacture of product gas containing hydrogen and carbon oxide and apparatus therefor | |
| US2894826A (en) | Apparatus for reforming hydrocarbons | |
| RU2261756C2 (en) | Method and reactor for performing non-adiabatic catalytic reactions | |
| JPH0123173B2 (en) | ||
| JP2002147720A (en) | Premixing burner block for partial oxidation method | |
| US6884368B2 (en) | Process for the production of a mixture comprising hydrogen and CO | |
| US5019356A (en) | Steam reformer with internal heat recovery | |
| KR19990068003A (en) | Apparatus for producing heat treatment atmospheres |