Fixed-bed catalytic reactor

• US 5,869,011 A
• Filed: 03/20/1996
• Issued: 02/09/1999
• Est. Priority Date: 02/01/1994
• Status: Expired due to Fees

• Current Assignee: Jing Ming Lee
• Original Assignee: Jing Ming Lee
• Inventors: Lee, Jing Ming
• Primary Examiner(s): YOON, TAE H
• Application Number:
  US08/618,987
• Time in Patent Office: 1,056 Days
• Field of Search: 48/197 R, 48/198.8, 422/200, 422/201, 518/712
• US Class Current: 422/200
• CPC Class Codes: B01J 2208/00141 Coils
• CPC Class Codes: B01J 2219/00083 Coils
• CPC Class Codes: B01J 8/025 in a cylindrical shaped bed
• CPC Class Codes: B01J 8/0285 Heating or cooling the reactor for tubular reactors in furnaces B01J8/062
• CPC Class Codes: F28D 7/08 the conduits being otherwise bent, e.g. in a serpentine or zig-zag F28D7/10 takes precedenceF28D7/0016 and F28D7/0033 take precedence
• CPC Class Codes: F28D 7/085 in the form of parallel conduits coupled by bent portions
• CPC Class Codes: F28F 2265/10 for preventing overheating, e.g. heat shields thermal insulation F28F2270/00
• CPC Class Codes: F28F 2275/02 by using bonding materials brazing F28F2275/04; by embedding elements in particular materials

Abstract

Disclosed are a fixed-bed, catalytic reactor wherein reaction heat can be exchanged against a heat exchange medium circulating indirectly through the catalyst bed, and a catalytic process comprising operation of the reactor. The reactor comprises a catalyst bed having internally embedded banks of heat exchange tubes. An inlet distributor distributes reactants for flow through the bed. The distributed fluid passes through the bed in a flow path wherein a catalytic reaction occurs. The reaction effluent is then collected from the bed by an outlet product collector. A heat exchange medium circulated through the internal heat exchange tubes adds or removes reaction heat as required for enhanced conversion in the reactor. Multiple heat exchange tubes can be used, and inlet and discharge manifolds are provided for distributing the circulating heat exchange medium. The heat exchange tubes can be spaced in accordance with the heat interchange required to optimize the reaction rate.

Claims

1. A catalytic reaction process, comprising the steps of:

introducing process fluid reactants to a reactant distributor formed adjacent an upper region of a fixed-bed catalytic reactor comprising a generally cylindrical catalyst bed extending axially upwardly from a bottom region to the upper region spaced therefrom, a flow path for fluid to pass between the upper and bottom regions, through a plurality of generally transverse catalyst layers and tube banks comprising U-bend tubes disposed in the catalyst bed, a supply manifold for feeding a heat transfer fluid to the tube banks, and an exit manifold for gathering heat transfer fluid from the tube banks;

passing the process fluid reactants along the flow path from the reactant distributor axially through the transverse catalyst layers and tube banks to a product collector for catalytic reaction in the catalyst layers, wherein the product collector is formed adjacent the bottom region of the reactor;

circulating a heat transfer fluid countercurrently from the supply manifold, through the tube banks wherein heat is exchanged between said heat transfer fluid and the process fluid reactants passing across the tube banks between the catalyst layers, and to the return manifold; and

collecting process fluid products at the product collector.

2. The process of claim 1, wherein internal walls of the reactor are thermally insulated.

3. The process of claim 1, wherein the product collector comprises a perforated gas collection pipe mounted on the inside wall of the reactor and a layer of low density heat-resistant material to support the catalyst bed.

4. The process of claim 3, wherein the reactor includes a catalyst-free zone adjacent the upper region of sufficient size to permit thermal expansion of the catalyst and the tube banks.

5. The process of claim 4, wherein the catalyst-free zone comprises a low density, heat resistant filler material.

6. The process of claim 1, wherein each tube bank comprises a plurality of laterally spaced transverse tubes.

7. The reactor of claim 6, wherein total heat transfer surface area and lateral spacing of the tubes in each tube bank are relatively varied among the separate tube banks.

8. The reactor of claim 7, wherein the tubes are most densely spaced in the bank adjacent the upper region, are progressively less densely spaced in tube banks spaced further from the upper region, and least densely spaced in the bank adjacent the bottom region.

9. The process of claim 1, wherein the heat transfer fluid comprises boiler feed water, steam, molten salt, or a process fluid.

10. The process of claim 1, wherein the process fluid reactants comprise generally stoichiometric hydrogen and nitrogen, and the process fluid product comprises ammonia.

11. The process of claim 1, further comprising the steps of:

preheating the process fluid reactants in an indirect flow heat exchanger against a stream of the process fluid products;

passing the preheated fluid reactants through the tube banks as the heat transfer fluid flowing inside said tube banks;

passing the process fluid reactants from the exit manifold to a boiler to heat boiler feed water and cool the process fluid reactants to form a preconditioned reactant stream;

passing the preconditioned reactant stream through the flow path of the catalytic reactor;

passing the process fluid product from the product collector through a boiler to heat boiler feed water and form a partially cooled product stream; and

supplying the partially cooled product stream to the indirect flow heat exchanger for the reactant preheating step.

12. The process of claim 10, further comprising the steps of:

preheating the process fluid reactants in an indirect flow heat exchanger against a stream of the process fluid product;

passing the preheated reactants through the flow path of the catalytic reactor;

passing a molten salt through the tube banks as the heat transfer fluid; and

passing heated molten salt from the return manifold through a boiler to heat boiler feed water and cool the molten salt for recirculation through the tube banks.

13. The process of claim 1 wherein the reactants comprise shift gas including a mixture of hydrogen, carbon monoxide, carbon dioxide, and steam, the process fluid product is richer in hydrogen and carbon dioxide than said process fluid reactants.

14. The process of claim 13, further comprising:

supplying boiler feed water at a temperature between about 150°

-190°

C. as the heat transfer fluid to the supply manifold;

supplying shift gas at a temperature between about 180°

14 240°

C. to the reactant distributor;

maintaining the maximum temperature in the catalyst bed below about 270°

C.; and

maintaining the process fluid product collected at the product collector at least about 10°

C. above its dewpoint.

15. The process of claim 14, wherein:

a first catalyst layer disposed between the reactant distributor and a first tube bank contains less than about 5 percent of the total catalyst volume of the catalyst bed;

a last catalyst layer disposed between a last tube bank and the product collector contains less than about 10 percent of the total catalyst volume of the catalyst bed; and

intermediate individual catalyst layers contain a generally increasing volume of the total catalyst volume of the catalyst bed from adjacent the first catalyst layer to adjacent the last catalyst layer.

16. The process of claim 1, wherein the process fluid reactants comprise synthesis gas including hydrogen and carbon oxides, and the process fluid product comprises methanol.

17. The process of claim 16, further comprising the steps of:

preheating the synthesis gas in an indirect flow heat exchanger against a stream of the process fluid product from the product collector;

passing the preheated synthesis gas through the flow path of the catalytic reactor; and

circulating boiler feed water through the tube banks as a cooling medium.

18. The process of claim 17, wherein the boiler feed water circulation includes pumping boiler feed water in a supply line from a steam drum to the supply manifold, introducing at least partially vaporized fluid from the return manifold to the steam drum, collecting steam and condensate for separation in the steam drum, obtaining steam from the steam drum, blowing down a portion of the condensate from the steam drum, and supplying makeup boiler feed water to the supply line.

19. The process of claim 1, wherein the reactants comprise a mixture of hydrocarbon and air, and the process fluid product comprises maleic anhydride.