WO2013075143A1 - Cœur dans réacteur à cuve, ses procédés d'utilisation et de fabrication - Google Patents

Cœur dans réacteur à cuve, ses procédés d'utilisation et de fabrication Download PDF

Info

Publication number
WO2013075143A1
WO2013075143A1 PCT/US2012/065952 US2012065952W WO2013075143A1 WO 2013075143 A1 WO2013075143 A1 WO 2013075143A1 US 2012065952 W US2012065952 W US 2012065952W WO 2013075143 A1 WO2013075143 A1 WO 2013075143A1
Authority
WO
WIPO (PCT)
Prior art keywords
product
reactant
fluid
reactor
utility
Prior art date
Application number
PCT/US2012/065952
Other languages
English (en)
Inventor
Zhijun Jia
Mark Jacob
Edward THIELE
Daniel Peterson
Chadwick KORTHIUS
Steven VALLEE
Original Assignee
Chart Industries, Inc.
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 Chart Industries, Inc. filed Critical Chart Industries, Inc.
Publication of WO2013075143A1 publication Critical patent/WO2013075143A1/fr

Links

Classifications

    • 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
    • B01J3/00—Processes of utilising sub-atmospheric or super-atmospheric pressure to effect chemical or physical change of matter; Apparatus therefor
    • B01J3/04—Pressure vessels, e.g. autoclaves
    • 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
    • B01J19/248—Reactors comprising multiple separated flow channels
    • B01J19/249—Plate-type reactors
    • 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
    • B01J2219/24—Stationary reactors without moving elements inside
    • B01J2219/2401—Reactors comprising multiple separate flow channels
    • B01J2219/245—Plate-type reactors
    • B01J2219/2451—Geometry of the reactor
    • B01J2219/2453—Plates arranged 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
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/24—Stationary reactors without moving elements inside
    • B01J2219/2401—Reactors comprising multiple separate flow channels
    • B01J2219/245—Plate-type reactors
    • B01J2219/2451—Geometry of the reactor
    • B01J2219/2456—Geometry of the plates
    • B01J2219/2458—Flat plates, i.e. plates which are not corrugated or otherwise structured, e.g. plates with cylindrical shape
    • 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
    • B01J2219/24—Stationary reactors without moving elements inside
    • B01J2219/2401—Reactors comprising multiple separate flow channels
    • B01J2219/245—Plate-type reactors
    • B01J2219/2451—Geometry of the reactor
    • B01J2219/2456—Geometry of the plates
    • B01J2219/2459—Corrugated plates
    • 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
    • B01J2219/24—Stationary reactors without moving elements inside
    • B01J2219/2401—Reactors comprising multiple separate flow channels
    • B01J2219/245—Plate-type reactors
    • B01J2219/2461—Heat exchange aspects
    • B01J2219/2462—Heat exchange aspects the reactants being in indirect heat exchange with a non reacting heat exchange medium
    • 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
    • B01J2219/24—Stationary reactors without moving elements inside
    • B01J2219/2401—Reactors comprising multiple separate flow channels
    • B01J2219/245—Plate-type reactors
    • B01J2219/2476—Construction materials
    • B01J2219/2477—Construction materials of the catalysts
    • B01J2219/2479—Catalysts coated on the surface of plates or inserts
    • 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
    • B01J2219/24—Stationary reactors without moving elements inside
    • B01J2219/2401—Reactors comprising multiple separate flow channels
    • B01J2219/245—Plate-type reactors
    • B01J2219/2476—Construction materials
    • B01J2219/2477—Construction materials of the catalysts
    • B01J2219/2481—Catalysts in granular from between plates
    • 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
    • B01J2219/24—Stationary reactors without moving elements inside
    • B01J2219/2401—Reactors comprising multiple separate flow channels
    • B01J2219/245—Plate-type reactors
    • B01J2219/2476—Construction materials
    • B01J2219/2477—Construction materials of the catalysts
    • B01J2219/2482—Catalytically active foils; Plates having catalytically activity on their own
    • 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
    • B01J2219/24—Stationary reactors without moving elements inside
    • B01J2219/2401—Reactors comprising multiple separate flow channels
    • B01J2219/245—Plate-type reactors
    • B01J2219/2476—Construction materials
    • B01J2219/2483—Construction materials of the plates
    • B01J2219/2485—Metals or 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
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/24—Stationary reactors without moving elements inside
    • B01J2219/2401—Reactors comprising multiple separate flow channels
    • B01J2219/245—Plate-type reactors
    • B01J2219/2491—Other constructional details
    • B01J2219/2492—Assembling means
    • B01J2219/2493—Means for assembling plates together, e.g. sealing means, screws, bolts
    • 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
    • B01J2219/24—Stationary reactors without moving elements inside
    • B01J2219/2401—Reactors comprising multiple separate flow channels
    • B01J2219/245—Plate-type reactors
    • B01J2219/2491—Other constructional details
    • B01J2219/2497—Size aspects, i.e. concrete sizes are being mentioned in the classified document
    • 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
    • B01J2219/24—Stationary reactors without moving elements inside
    • B01J2219/2401—Reactors comprising multiple separate flow channels
    • B01J2219/245—Plate-type reactors
    • B01J2219/2491—Other constructional details
    • B01J2219/2498—Additional structures inserted in the channels, e.g. plates, catalyst holding meshes

Definitions

  • This invention relates to heat exchange chemical reactors. REFERENCE TO AN EARLIER APPLICATION
  • the Fischer-Tropsch synthesis reaction involves converting a reactant composition comprising H 2 and CO in the presence of a catalyst to aliphatic hydrocarbon products.
  • the reactant composition may comprise the product stream from another reaction process such as steam reforming (product stream H 2 /CO ⁇ 3), partial oxidation (product stream H 2 /CO ⁇ 2), autothermal reforming (product stream H 2 /CO ⁇ 2.5), C0 2 reforming (H 2 /CO ⁇ 1 ), coal gasification (product stream H 2 /CO ⁇ 1 ), and combinations thereof.
  • the aliphatic hydrocarbon products may range from methane to paraffinic waxes of up to 100 carbon atoms or more.
  • the reactor is preferably formed as a stack of plates, with flow channels defined between the plates, the flow channels for the different fluids alternating in the stack.
  • this is preferably in the form of a corrugated metal substrate carrying the catalyst in a ceramic coating, such corrugated structures being removable from the channels when the catalyst is spent.
  • One embodiment relates to a reactor, comprising:
  • (C1 ) a core section having a top end, a bottom end, and an interior comprising a plurality of thermally conductive, parallel parting plates extending vertically between the top and bottom ends; the parting plates separating and defining a plurality of alternating process and utility channels; the process channels extending vertically between the top and bottom ends; and
  • (C2) a bottom header defining an interior product region; the bottom header sealingly attached to and extending downward from the bottom end;
  • the parting plates may be suitably made from flat metal, the type of which is not particularly limited.
  • the parting plates may be suitably made from one or more of aluminum, 3000 series aluminum, 3003 aluminum, 5000 series aluminum, 5085 aluminum, 6000 series aluminum, 6061 aluminum, stainless steel, copper, titanium, monel, inconel, nickel, platinum, rhodium, chromium, brass, alloys thereof, or combination thereof.
  • the heat exchange reactor is substantially wholly enclosed by the pressure vessel such that the pressure within the heat exchange reactor is balanced by the pressure in the interior region of the pressure vessel.
  • the heat exchange reactor has top and bottom ends, a bottom header, and process channels open at the top end such that the process channels fluidly communicate with both the interior region of the pressure vessel and the interior product region in the bottom header.
  • the interior region of the pressure vessel is in fluid communication with the interior product region of the bottom header by way of the process channels.
  • a process fluid e.g., reactant fluid, or the like
  • Sufficiently pressurizing the vessel's interior region drives the process fluid down into the process channels from the open top end, through the process channels, and into the interior product region in the bottom header.
  • part of the process fluid may suitably undergo reaction in the process channels and be converted to product, which also flows into the interior product region together with unreacted process fluid.
  • the heat exchange reactor is sealed on its sides, with the exception that side headers may be present to inject and remove a utility fluid into and from the utility channels.
  • the utility and process channels are configured to provide for co-current or countercurrent flow of the utility and process streams. Put another way, it is preferred that the process and utility channels are configured such that their respective streams run parallel or antiparallel to one another, and not at right angles to one another.
  • the heat exchanger can be configured to separate and direct the respective utility and process streams in a low cost manner.
  • the pressure vessel can be made of steel or steel alloy, and the heat exchange reactor may be made of aluminum or aluminum alloy.
  • the parting plates are spaced apart from one another, and the spaces therebetween define the respective process and utility channels.
  • the spacing is not particularly limited.
  • the parting plates may be spaced apart from one another by a distance ranging from 0.1 -20 mm, which range includes all values and subranges therebetween, including 0.1 , 0.2, 0.3, 0.4, 0.5, 0.6, 0.7, 0.8, 0.9, 1 , 2, 3, 4, 5, 6, 7, 8, 9, 10, 15, and 20 mm, or any combination thereof.
  • the parting plates may have different spacing depending on whether two adjacent plates define a process channel or a utility channel therebetween. For example, two adjacent plates defining a process channel may have a greater or lesser spacing between them than do two adjacent plates defining a utility channel.
  • the spacing between adjacent parting plates may be suitably adjusted according to considerations of structural support, reaction conditions, heat removal, fin height, catalyst type, fluid flow, and the like.
  • the parting plate spacing may be constant, i.e., it may be the same for each of the process channels, utility channels, or both.
  • the parting plate spacing for one or both of the process and utility channels may vary along the stack direction.
  • each of the process channels is defined by parting plates having the same spacing.
  • each of the utility channels is defined by parting plates having the same spacing.
  • the spacing for process channels is greater than the spacing for the utility channels. It should follow that since the parting plates are parallel, the spacing defining a particular channel between parting plates will be the same for whole of that channel.
  • the pressure vessel is adapted to contain a pressurized process fluid in the interior region at a pressure sufficient to force the process fluid into the process channels at the top end and downward through the bottom end into the interior product region.
  • the bottom header is sealingly attached to the bottom end by a weld or with a flanged connection.
  • the flanged connection may allow for easier removal and insertion of catalyst from or into the process channels.
  • the bottom header may suitably be made from metal, the type of which is not particularly limited.
  • the bottom header may independently include or be made from one or more metal such as aluminum, 3000 series aluminum, 3003 aluminum, 5000 series aluminum, 5085 aluminum, 6000 series aluminum, 6061 aluminum, stainless steel, copper, titanium, monel, inconel, nickel, platinum, rhodium, chromium, brass, alloys thereof, or combination thereof.
  • the reactor includes a process fluid outlet extending from the bottom header through the pressure bearing wall and in fluid communication with the interior product region.
  • Reaction product, unreacted process fluid, and the like may suitably collected in the interior product region and sent downstream, for example to a second reactor or heat exchange reactor.
  • the reactor may include more than one heat exchanger enclosed therein, and the process fluid outlets of each may be collected into a single process fluid outlet, which may suitably exit the reactor through a single outlet extending through the pressure bearing wall.
  • the reaction product may be separated from the unreacted process fluid components, whereupon the separated reaction product may be sent downstream, and the unreacted process fluid may be returned to the reactor for further reaction.
  • the process fluid outlet may suitably include a flanged connection between the bottom header and the pressure bearing wall.
  • one or more of the process channels, utility channels, or both contain one or more fins, catalysts, or a combination thereof.
  • the fins may be independently and suitably chosen from one or more of corrugated, castellated, herringbone, perforated, straight, or serrated materials, or a combination thereof.
  • the fins may be suitably optimized in consideration of structure and/or heat transfer.
  • the fins may provide structural support to adjacent parting plates or improve heat transfer between process and utility fluids.
  • the structure and/or arrangement of the may be considered to form one or more "mini-channels", which may direct the flow or contribute to directing the flow of a fluid such as a process fluid or utility fluid as it travels through the channel.
  • the mini-channels run in the machine or process direction, such that the process fluid therein flows straight through from the top end to the bottom end of the heat exchange reactor.
  • the process and utility channels may each have fins arranged to have respective mini- channels which are parallel or substantially so.
  • the mini-channels run in a direction other than the process direction, for example wherein a cross-flow is desired between the process and utility channels is desired, the mini-channels in the respective channels may be aligned in a direction other than parallel, for example, 90 degrees to one another.
  • the fins may be independently and suitably made from metal, the type of which is not particularly limited.
  • the one or more of the process channel and/or utility channel fins may independently include or be made from one or more metal such as aluminum, 3000 series aluminum, 3003 aluminum, 5000 series aluminum, 5085 aluminum, 6000 series aluminum, 6061 aluminum, stainless steel, copper, titanium, monel, inconel, nickel, platinum, rhodium, chromium, brass, alloys thereof, or combination thereof.
  • the height of the process channel fins is not particularly limited.
  • the process channel fins, if present, may have a height ranging from 0.1 - 20 mm, the height being measured as the distance between adjacent vertical parting plates, e.g.
  • This height range includes all values and subranges therebetween, including 0.1 , 0.2, 0.3, 0.4, 0.5, 0.6, 0.7, 0.8, 0.9, 1 , 2, 3, 4, 5, 6, 7, 8, 9, 10, 15, and 20 mm, or any combination thereof.
  • the width of the process channel fins is not particularly limited.
  • the width of the process channel fins e.g., the distance between two fins, may suitably range from 0.1 - 20 mm, the width being measured normal to the process channel fin height, i.e., parallel to the plane of an adjacent parting plate.
  • This width range includes all values and subranges therebetween, including 0.1 , 0.2, 0.3, 0.4, 0.5, 0.6, 0.7, 0.8, 0.9, 1 , 2, 3, 4, 5, 6, 7, 8, 9, 10, 15, and 20 mm, or any combination thereof.
  • the process channel fins may suitably have a catalyst coating, for example, a washcoated catalyst.
  • the height of the utility channel fins is not particularly limited.
  • the utility channel fins may have a height ranging from 0.5 - 20 mm, the height being measured as the distance between adjacent vertical parting plates, e.g. the separation distance between adjacent parting plates defining that channel.
  • This height range includes all values and subranges therebetween, including 0.5, 0.6, 0.7, 0.8, 0.9, 1 , 1 .1 , 1 .2, 1 .3, 1 .4, 1 .5, 2, 3, 4, 5, 6, 7, 8, 9, 10, 15, and 20 mm, or any combination thereof.
  • the width of the utility channel fins is not particularly limited.
  • the width of the utility channel fins e.g., the distance between two fins, may suitably range from 0.1 - 20 mm, the width being measured normal to the process channel fin height, i.e., parallel to the plane of an adjacent parting plate.
  • This width range includes all values and subranges therebetween, including 0.1 , 0.2, 0.3, 0.4, 0.5, 0.6, 0.7, 0.8, 0.9, 1 , 2, 3, 4, 5, 6, 7, 8, 9, 10, 15, and 20 mm, or any combination thereof.
  • the fins are adapted to direct the flow of utility fluid in the utility channels and/or process fluid in the process channels.
  • the sides of the heat exchange reactor e.g., the side edges of the process channels, are suitably sealed such that the only way for the process fluid to enter the process channels is through the top end, wherein the process channels fluidly communicate with the interior region of the pressure vessel.
  • the sides may be sealed by the inclusion of one or more process channel side bars.
  • the process channel side bars seal the side edges of the process channels between adjacent parting plates and extend vertically between the top and bottom ends such that they prevent fluid communication between the side regions of the process channels and the interior region of the pressure vessel.
  • the process channel side bars may be suitably disposed within the process channels at the outer edges thereof and define the height of the process channels between adjacent parting plates, or they may be sealingly attached to the outside edges of the process channels.
  • the process channel side bars are disposed within the process channels, they may help provide structural support between adjacent parting plates, and particularly at the outer edges of the process channels. For example, these side bars may resist compression or expansion damage of the process channel during manufacturing, use, or both.
  • the process channel side bars may be made from metal, the type of which is not particularly limited.
  • the process channel side bars may be made from or include one or more of aluminum, 3000 series aluminum, 3003 aluminum, 5000 series aluminum, 5085 aluminum, 6000 series aluminum, 6061 aluminum, stainless steel, copper, titanium, monel, inconel, nickel, platinum, rhodium, chromium, brass, alloys thereof, or combination thereof.
  • the heat exchange reactor may suitably include one or more process channel support bars disposed within the process channels between adjacent parting plates and extending vertically between the top and bottom ends.
  • these support bars may help provide structural support between adjacent parting plates, or further direct the flow along the process channel.
  • these support bars may resist compression or expansion damage of the process channel during manufacturing, use, or both.
  • the process channel support bars may be made from the same or different metal as the process channel side bars.
  • the heat exchange reactor may suitably include utility channel top and bottom bars at the top and bottom ends.
  • the utility channel top and bottom bars suitably seal the top and bottom edges of the utility channels between adjacent parting plates and prevent fluid communication between the utility channels and both the interior region of the pressure vessel and the interior product region of the bottom header.
  • the sides of the heat exchange reactor may be suitably sealed to prevent fluid communication between the interior fluid region and the sides or side edges of both the utility channels and process channels.
  • the heat exchange reactor may include utility channel side bars; the utility channel side bars sealing the side edges of the utility channels between adjacent parting plates and preventing fluid communication between the interior region and the utility channels.
  • the utility channel side bars may help provide structural support between adjacent parting plates, and particularly at the outer edges of the utility channels.
  • these side bars may resist compression or expansion damage of the utility channel during manufacturing, use, or both.
  • the utility channel side bars may be made from metal, the type of which is not particularly limited.
  • the utility channel side bars may be made from or include one or more of aluminum, 3000 series aluminum, 3003 aluminum, 5000 series aluminum, 5085 aluminum, 6000 series aluminum, 6061 aluminum, stainless steel, copper, titanium, monel, inconel, nickel, platinum, rhodium, chromium, brass, alloys thereof, or combination thereof.
  • the heat exchange reactor may include utility channel support bars disposed within the utility channels between adjacent parting plates; the support bars providing structural support between adjacent parting plates.
  • these support bars may help provide structural support between adjacent parting plates, or further direct the flow along the utility channel.
  • these support bars may resist compression or expansion damage of the utility channel during manufacturing, use, or both.
  • the utility channel support bars may be made from the same or different metal as the process channel side bars.
  • the utility channel side bars and/or support bars may define the spacing of utility channels between adjacent parting plates.
  • the heat exchange reactor may include first and second side headers to provide for a flow of a utility fluid through the utility channels.
  • the first and second side headers define respective interior utility fluid regions and are sealingly attached to the core section such that the first side header interior utility fluid region is in fluid communication with the second side header interior utility fluid region through one or more of the utility channels.
  • the side headers may be placed along one or more of the sides of the core section such that they communicate with the side edges of one or more of the utility channels.
  • first and second side headers may be placed on opposite sides of the core section such that their respective interior utility fluid regions are in fluid communication with each other (and the utility channels) through opposing side edges of the utility channels.
  • first and second side headers may be placed on the same side of the core section such that their respective interior utility fluid regions are in fluid communication with each other (and the utility channels) through the same-side edges of the utility channels.
  • first and second side headers are placed at upper and lower portions (upper defined as nearer the top end, and lower defined as nearer the bottom end) of the core section.
  • the utility fluid enters and exits the core section through upper and lower side portions thereof, while the process fluid enters the core section from the upper end and exits into the bottom header at the lower end.
  • the side headers may be made from the same or different material as the side bars or support bars.
  • the reactor may include a utility fluid inlet extending through the pressure bearing wall into the first side header and in fluid communication with the first side header interior utility fluid region; and a utility fluid outlet extending through the pressure bearing wall into the second side header and in fluid communication with the second side header interior utility fluid region.
  • the utility fluid inlet and outlet may each include a flanged connection between the side headers and the pressure bearing wall.
  • the heat exchange reactor includes utility channel side bars
  • the utility channel side bars do not seal the side edges at the interior utility fluid regions, in consideration of allowing fluid communication between the interior utility fluid regions and utility channels.
  • one or more of the utility channels may additionally include directional fins; the fins adapted to direct the flow of a utility fluid between one or more of the interior utility fluid regions and the utility channels.
  • the fins adapted to direct the flow of a utility fluid between one or more of the interior utility fluid regions and the utility channels.
  • one or more directional fins may be included in those areas of the utility channel near the side headers/interior utility fluid region to help transition the flow of the utility stream between the vertical direction and the interior utility fluid regions of the side headers.
  • the directional fins may be one or more of corrugated, castellated, herringbone, perforated, straight, serrated, or a combination thereof.
  • the directional fins may be independently and suitably made from metal, the type of which is not particularly limited.
  • they may include or be made from one or more metal such as aluminum, 3000 series aluminum, 3003 aluminum, 5000 series aluminum, 5085 aluminum, 6000 series aluminum, 6061 aluminum, stainless steel, copper, titanium, monel, inconel, nickel, platinum, rhodium, chromium, brass, alloys thereof, or combination thereof.
  • the height, width and thickness of the directional fins may be suitably and independently selected from those given for the utility channel fins.
  • the flow of a utility stream in the utility channel may be directed in whole or part by the flow between the interior utility fluid regions, the locations of side headers and their respective utility fluid inlets and outlet, and/or the flow direction of a utility stream in the utility channel may be directed in whole or in part by using fins or mini-channels along the desired flow direction for the utility stream.
  • the utility stream may be driven by a pump, thermosyphon or a combination thereof.
  • the heat exchange reactor may be made from any suitable material, the type of which is not paryticularly limted.
  • all or part of the heat exchange reactor may include or be made from one or more of aluminum, 3000 series, 3003 aluminum, 5000 series, 5085 aluminum, 6000 series, 6061 aluminum, stainless steel, copper, titanium, monel, inconel, nickel, platinum, rhodium, chromium, brass, alloys thereof, or combination thereof.
  • the core section may uses the FINTEC line of heat exchangers and/or reactors such as available from Chart Energy & Chemicals, Inc., of LaCrosse, Wl.
  • the core uses the SHIMTECTM line of heat exchangers and/or reactors such as available from Chart Energy & Chemicals, Inc., of LaCrosse, Wl.
  • SHIMTECTM line of heat exchangers and/or reactors such as available from Chart Energy & Chemicals, Inc., of LaCrosse, Wl.
  • the heat exchange reactor may be suitably made according to known methods, for example using one or more of brazing, bonding, diffusion bonding, diffusion brazing, laser welding, hot isostatic pressing, clamping, welding, or combination thereof.
  • one or more additional heat exchange reactors may be enclosed within the pressure vessel.
  • the pressure shell may include a flange sealingly attached thereto; the flange having a surface facing the interior region and forming part of the pressure bearing wall; the flange being removable to provide access to the heat exchange reactor.
  • the core section of the heat exchange reactor has height (H), width (W), and length (L) dimensions, which dimensions independently range from 6"H x 1 "W x 6"L to 5 ⁇ x 6'W x 30'L; the height being measured in a vertical direction between the top and bottom ends, the width being measured in a horizontal direction normal to the parting plates, and the length being measured in a horizontal direction parallel to the parting plates.
  • H, W, and L ranges independently include all values and subranges therebetween, including: for the height range, 6, 7, 8, 9, 10, 1 1 , 12 inches, 1 ⁇ ", 1 '2", 1 '3", 1 '4", 1 '5", 1 '6", 2", 3", 4" and 5", and any combination thereof; for the width range, 1 , 2, 3, 4, 5, 6, 7, 8, 9, 10, 1 1 , 12 inches, 1 ⁇ ", 1 '2", 1 '3", 1 '4", 1 '5", 1 '6", 2', 3', 4', 5', and 6', and any combination thereof; and for the length range, 6, 7, 8, 9, 10, 1 1 , 12 inches, 1 ⁇ ", 1 '2", 1 '3", 1 '4", 1 '5", 1 '6", 2', 3', 4', 5', 6', 7', 8', 9', 10', 1 1 ', 12', 15', 20', 22', 24', 26
  • Various fluid passageways or pipes may connect the core through the kettle wall to a corresponding passageway or pipe outside the kettle.
  • one or more feed gas lines, drain lines, process stream lines, utility stream lines, injection stream lines may connect through the kettle to the core. See, for example, attached Dwg. Nos. 17687Z and 17582Z.
  • the core is aluminum
  • the pressure vessel is steel or stainless steel.
  • one or more transition joints may be used to connect the aluminum core side to the steel or stainless steel pressure vessel side. Suitable transition joints include the type obtainable from Dynamic Materials Corporation in Boulder, Colorado. In one embodiment, explosion-welded clad metal transition joints may be used.
  • the transition joint may include a corrosion resistant coating.
  • the coating resists penetration by hydrogen gas or other gas.
  • one or more bellows may be used to connect part of the aluminum core side to the steel or stainless steel kettle side.
  • Suitable bellows include the type obtainable from U.S. Bellows, Inc., in Houston, Texas.
  • H is a measure of the length of the process channel
  • W is a measure of the thickness of the stack of channels and parting plates
  • L is a measure of the width of the process channel, e.g., a measure of the side-to-side distance process channel side bar to opposing process channel side bar.
  • the HWL of the core section is 5'x6'x28'.
  • the reactor may be suitably adapted to operate at a differential pressure of ⁇ 20 barg between the interior region and the interior product region at a
  • a differential pressure may be defined as the absolute value of the difference between the referenced regions' pressures.
  • aforementioned pressure range independently include all values and subranges therebetween, including 0, .1 , .2, .3, .4, .5, .6, .7, .8, .9, 1 , 2, 3, 4, 5, 6, 7, 8, 9, 10, 12.5, 15, 17.5, and 20 barg, and any combination thereof.
  • the reactor may be adapted to operate at a pressure of ⁇ 150 barg in the interior region at a temperature ranging from -100 to 750°F.
  • This pressure range includes all values and subranges therebetween, including 0, .1 , .2, .3, .4, .5, .6, .7, .8, .9, 1 , 2, 3, 4, 5, 6, 7, 8, 9, 10, 12.5, 15, 17.5, 20, 25, 50, 75, 100, 1 10, 120, 130, 140, and 150 barg, and any combination thereof.
  • the aforementioned ranges for temperatures independently include all values and subranges therebetween, including -100, -90, -80, -70, -60, -50, -40, -30, -20, -10, -9, -8, -7, -6, - 5, -4, -3, -2, -1 , 0, 1 , 2, 3, 4, 5, 6, 7, 8, 9, 10, 15, 20, 25, 50, 75, 100, 200, 300, 400, 500, 600, 700, and 750 °F.
  • Another embodiment relates to a method for making the reactor described herein, which includes:
  • the reactor is particularly suitable for carrying out an exothermic reaction or an endothermic reaction.
  • suitable reactions include out one or more of the following reactions: catalytic reaction, endothermic reaction, exothermic reaction, acetylation, addition reaction, alkylation, dealkylation, hydrodealkylation, reductive alkylation, amination, aromatization, arylation, autothermal reforming, carbonylation, decarbonylation, reductive carbonylation, carboxylation, reductive carboxylation, reductive coupling, condensation, cracking, hydrocracking, cyclization, cyclooligomerization, dehalogenation, dimerization, epoxidation, esterification, exchange, Fischer-Tropsch, halogenation, hydrohalogenation, homologation, hydration, dehydration, hydrogenation, dehydrogenation, hydrocarboxylation, hydroformylation, hydrogenolysis, hydrometallation, hydrosilation, hydrolysis, hydrotreating, hydrodesulferization/hydrodenitrogenation, isomer
  • the reactor is suitable for carrying out one or more hydrogenation reaction, dehydrogenation reaction, oxidation reaction, Fischer-Tropsch reaction, gas to liquid reaction, steam reformation, or a combination thereof.
  • the reaction is a Fischer-Tropsch reaction.
  • Another embodiment relates to a process, carried out in the reactor, which process includes: heating or cooling the utility channels with a utility stream; and
  • the process includes increasing or decreasing the amount of process fluid relative to the amount of process cooling fluid in the interior region.
  • the process may include increasing or decreasing the amount of cooling process fluid relative to the amount of process fluid in the interior region.
  • the reaction is one or more of catalytic reaction, endothermic reaction, exothermic reaction, acetylation, addition reaction, alkylation,
  • hydrodesulferization/hydrodenitrogenation isomerization, methanation, methanol synthesis, methylation, demethylation, metathesis, nitration, oxidation, partial oxidation, polymerization, reduction, Sabatier reaction, steam reforming, carbon dioxide reforming, sulfonation, telomerization, transesterification, trimerization, water gas shift, reverse water gas shift, phase change reaction, evaporation, absorption, adsorption, or a combination thereof.
  • reaction may be an endothermic reaction, exothermic reaction, Fisher-Tropsch reaction, or combination thereof.
  • hydrodesulferization/hydrodenitrogenation product or reactant isomerization product or reactant, methanation product or reactant, methanol synthesis product or reactant, methylation product or reactant, demethylation product or reactant, metathesis product or reactant, nitration product or reactant, oxidation product or reactant, partial oxidation product or reactant, polymerization product or reactant, reduction product or reactant, Sabatier reaction product or reactant, steam reforming product or reactant, carbon dioxide reforming product or reactant, sulfonation product or reactant, telomerization product or reactant, transesterification product or reactant, trimerization product or reactant, water gas shift product or reactant, reverse water gas shift product or reactant, phase change reaction product or reactant, evaporation product or reactant, absorption product or reactant, adsorption product or reactant, reactant fluid, product fluid, diluent fluid, injection fluid, catalyst regeneration fluid, scrubbing fluid, catalyst, liquid catalyst, gase
  • the process fluid may be one or more of a liquid, gas, or liquid / gas mixture, vapor, liquid droplets, liquid water, steam, synthesis gas, carbon monoxide, carbon dioxide, hydrogen gas, nitrogen gas, oxygen gas, aliphatic hydrocarbon, hydrocarbon, methane, ethane, propane, butane, isobutane, pentane, Ci-Ci 00 hydrocarbon, wax, unsaturated hydrocarbon, steam reformation product stream, partial oxidation product stream, autothermal reforming product stream, C0 2 reforming product stream, coal gasification product stream, desulfurized reactant stream, reactant fluid, product fluid, diluent fluid, injection fluid, catalyst regeneration fluid, scrubbing fluid, catalyst, liquid catalyst, gaseous catalyst, or any combination thereof.
  • a liquid, gas, or liquid / gas mixture vapor, liquid droplets, liquid water, steam, synthesis gas, carbon monoxide, carbon dioxide, hydrogen gas, nitrogen gas, oxygen gas, aliphatic hydrocarbon, hydrocarbon, methane,
  • reactant fluid may suitably refer to a process fluid which contains one or more reactants intended for the subject invention.
  • the utility channels are adapted to contain a utility fluid, the utility fluid being one or more of a heating fluid, cooling fluid, liquid, gas, or liquid / gas mixture, vapor, liquid droplets, air, steam, liquid water, nitrogen, argon, carbon monoxide, carbon dioxide, molten salt, oil, mineral oil, aliphatic hydrocarbon, hydrocarbon, methane, ethane, ethylene, propane, butane, isobutane, pentane, isopentane, hexane, mixed refrigerant, vapor
  • Another embodiment relates to a process, which is not limited to the reactor herein, and may be suitably carried out in other types of reactors.
  • This embodiment relates to a process for controlling the rate or temperature or both of a catalyzed exothermic reaction, which process includes: contacting a cooling process fluid with one or more of a reactant for the exothermic reaction, a catalyst for the exothermic reaction, or a combination thereof;
  • reaction may be one or more of catalytic reaction, acetylation, addition reaction, alkylation, dealkylation, hydrodealkylation, reductive alkylation, amination, aromatization, arylation, autothermal reforming, carbonylation, decarbonylation, reductive carbonylation, carboxylation, reductive carboxylation, reductive coupling,
  • hydrohalogenation homologation, hydration, dehydration, hydrogenation, dehydrogenation, hydrocarboxylation, hydroformylation, hydrogenolysis, hydrometallation, hydrosilation, hydrolysis, hydrotreating, hydrodesulferization/hydrodenitrogenation, isomerization,
  • the catyalyzed exothermic reaction is a Fisher-Tropsch reaction.
  • the process includes increasing or decreasing the amount of reactant or catalyst relative to the amount of cooling process fluid. In another embodiment, the process includes increasing or decreasing the amount of cooling process fluid relative to the amount of the reactant or catalyst.
  • the heat exchange reactor includes one or more catalyst retention screens disposed between the bottom end and the bottom header in fluid communication with the process channels and the product interior region. In another embodiment, the heat exchange reactor includes one or more catalyst retention screens disposed between the top end and the interior region in fluid communication with the process channels and the interior region. Combinations of screens at the top and bottom may be used.
  • the second fluid is one or more of a liquid, gas, liquid / gas mixture, vapor, liquid droplets, liquid water, steam, synthesis gas, carbon monoxide, carbon dioxide, hydrogen, nitrogen, oxygen, argon, air, aliphatic hydrocarbon, hydrocarbon, methane, ethane, propane, butane, isobutane, pentane, Ci-Ci 00 hydrocarbon, wax, unsaturated hydrocarbon, coal gasification product, desulfurized reactant or product, catalytic reaction product or reactant, endothermic reaction product or reactant, exothermic reaction product or reactant, acetylation product or reactant, addition reaction product or reactant, alkylation product or reactant, dealkylation product or reactant, hydrodealkylation product or reactant, reductive alkylation product or reactant, amination product or reactant, aromatization product or reactant, arylation product or reactant, autothermal reforming product or reactant, carbonylation product or reactant, decarbonylation product
  • hydrodesulferization/hydrodenitrogenation product or reactant isomerization product or reactant, methanation product or reactant, methanol synthesis product or reactant, methylation product or reactant, demethylation product or reactant, metathesis product or reactant, nitration product or reactant, oxidation product or reactant, partial oxidation product or reactant, polymerization product or reactant, reduction product or reactant, Sabatier reaction product or reactant, steam reforming product or reactant, carbon dioxide reforming product or reactant, sulfonation product or reactant, telomerization product or reactant, transesterification product or reactant, trimerization product or reactant, water gas shift product or reactant, reverse water gas shift product or reactant, phase change reaction product or reactant, evaporation product or reactant, absorption product or reactant, adsorption product or reactant, reactant fluid, product fluid, cooling process fluid, diluent fluid, injection fluid, catalyst regeneration fluid, scrubbing fluid, catalyst, liquid

Landscapes

  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Physical Or Chemical Processes And Apparatus (AREA)

Abstract

L'invention porte sur un réacteur qui comprend une cuve sous pression ayant une paroi de support de pression entourant une région interne pouvant être mise sous pression; une entrée de fluide de traitement s'étendant à travers la paroi en communication fluidique avec la région interne; un réacteur d'échange de chaleur disposé à l'intérieur de la cuve sous pression; le réacteur d'échange de chaleur ayant un extérieur, le réacteur d'échange de chaleur comportant en outre : une section centrale ayant une extrémité supérieure, une extrémité inférieure et un intérieur comportant une pluralité de plaques de séparation thermoconductrices parallèles s'étendant verticalement entre les extrémités supérieure et inférieure; les plaques de séparation séparant et définissant une pluralité de canaux alternés de traitement et de service; les canaux de traitement s'étendant verticalement entre les extrémités supérieure et inférieure; un collecteur inférieur définissant une région de produit interne.
PCT/US2012/065952 2011-11-18 2012-11-19 Cœur dans réacteur à cuve, ses procédés d'utilisation et de fabrication WO2013075143A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US201161561643P 2011-11-18 2011-11-18
US61/561,643 2011-11-18

Publications (1)

Publication Number Publication Date
WO2013075143A1 true WO2013075143A1 (fr) 2013-05-23

Family

ID=48430261

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/US2012/065952 WO2013075143A1 (fr) 2011-11-18 2012-11-19 Cœur dans réacteur à cuve, ses procédés d'utilisation et de fabrication

Country Status (1)

Country Link
WO (1) WO2013075143A1 (fr)

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US10710043B2 (en) 2014-09-24 2020-07-14 Raven Sr, Llc Compact and maintainable waste reformation apparatus
CN112191198A (zh) * 2020-11-11 2021-01-08 北京水木滨华科技有限公司 一种异丁烯氧乙酰化反应装置及方法
CN113663701A (zh) * 2020-05-13 2021-11-19 苏州科技大学 单原子熔融盐催化剂及其制备方法和聚光太阳能催化反应系统

Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5100609A (en) * 1990-11-19 1992-03-31 General Electric Company Enhancing load-following and/or spectral shift capability in single-sparger natural circulation boiling water reactors
US6695044B1 (en) * 1999-03-27 2004-02-24 Chart Heat Exchangers Limited Partnership Heat exchanger
US6736201B2 (en) * 1997-06-03 2004-05-18 Chart Heat Exchangers Limited Heat exchanger and/or fluid mixing means
US7266976B2 (en) * 2004-10-25 2007-09-11 Conocophillips Company Vertical heat exchanger configuration for LNG facility
US20080107585A1 (en) * 2004-11-03 2008-05-08 Singh Shashi P Maximum reaction rate converter process for exothermic reactions
US20100240780A1 (en) * 2009-03-23 2010-09-23 Thomas Charles Holcombe Fischer-Tropsch Reactions Using Heat Transfer Tubes with a Catalyst Layer on the Outside Surfaces
US7998345B2 (en) * 2007-07-09 2011-08-16 Chart Inc. Plate fin fluid processing device

Patent Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5100609A (en) * 1990-11-19 1992-03-31 General Electric Company Enhancing load-following and/or spectral shift capability in single-sparger natural circulation boiling water reactors
US6736201B2 (en) * 1997-06-03 2004-05-18 Chart Heat Exchangers Limited Heat exchanger and/or fluid mixing means
US6695044B1 (en) * 1999-03-27 2004-02-24 Chart Heat Exchangers Limited Partnership Heat exchanger
US7266976B2 (en) * 2004-10-25 2007-09-11 Conocophillips Company Vertical heat exchanger configuration for LNG facility
US20080107585A1 (en) * 2004-11-03 2008-05-08 Singh Shashi P Maximum reaction rate converter process for exothermic reactions
US7998345B2 (en) * 2007-07-09 2011-08-16 Chart Inc. Plate fin fluid processing device
US20100240780A1 (en) * 2009-03-23 2010-09-23 Thomas Charles Holcombe Fischer-Tropsch Reactions Using Heat Transfer Tubes with a Catalyst Layer on the Outside Surfaces

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US10710043B2 (en) 2014-09-24 2020-07-14 Raven Sr, Llc Compact and maintainable waste reformation apparatus
US11179693B2 (en) 2014-09-24 2021-11-23 Raven Sr, Inc. Compact and maintainable waste reformation apparatus
CN113663701A (zh) * 2020-05-13 2021-11-19 苏州科技大学 单原子熔融盐催化剂及其制备方法和聚光太阳能催化反应系统
CN113663701B (zh) * 2020-05-13 2023-12-01 苏州科技大学 单原子熔融盐催化剂及其制备方法和聚光太阳能催化反应系统
CN112191198A (zh) * 2020-11-11 2021-01-08 北京水木滨华科技有限公司 一种异丁烯氧乙酰化反应装置及方法

Similar Documents

Publication Publication Date Title
CA2554221C (fr) Procede pour realiser une reaction chimique limitee d'equilibre au moyen de la technologie des micro-canaux
CA2597161C (fr) Reacteurs catalytiques
CA2451416C (fr) Reacteur catalytique
JP4446388B2 (ja) 触媒反応器及び方法
CA2593609C (fr) Reacteur catalytique
CA2478333C (fr) Reacteurs a microcanaux a regulation thermique
US7235218B2 (en) Catalytic reactors
JP2010502432A5 (fr)
TW201740072A (zh) 反應裝置
NO333822B1 (no) Fremgangsmåte for å gjennomføre Fisher-Tropsch syntese
WO2013075143A1 (fr) Cœur dans réacteur à cuve, ses procédés d'utilisation et de fabrication
Rostrup-Nielsen et al. Steam reforming opportunities and limits of the technology
AU2010240925B2 (en) Process for the preparation of hydrogen and carbon monoxide containing gas
US20090253814A1 (en) Compact reactor
WO2010133621A1 (fr) Procédé pour préparer un mélange de monoxyde de carbone et d'hydrogène
GB2441509A (en) Fischer-Tropsch synthesis
WO2007003959A1 (fr) Production d'hydrocarbures liquides
JP6834183B2 (ja) 熱処理装置

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 12849879

Country of ref document: EP

Kind code of ref document: A1

NENP Non-entry into the national phase

Ref country code: DE

122 Ep: pct application non-entry in european phase

Ref document number: 12849879

Country of ref document: EP

Kind code of ref document: A1