DE4313723A1 - Reactor with oxidation catalyst - Google Patents

Abstract

The invention relates to a reactor having an oxidation catalyst incorporated in the mechanical structure and three-dimensionally integrated heat exchangers for preparing sulphur trioxide from sulphur dioxide and air and simultaneously generating high-pressure steam. This object is achieved according to the invention by vertically positioned frames being arranged next to one another as sections, with frames in which the metal sponge having the active catalytic composition located on the surface is inserted in a vertical position being followed by frames containing the known tube boiler elements as steam generators, and the individual frames being firmly but detachably connected with one another to give a sandwich reactor.

Description

The invention relates to a reactor in the mechanical Structure of the integrated oxidation catalyst and spatially inte grierte heat exchangers for the production of sulfur trioxide from sulfur dioxide and air and simultaneous production of High pressure water vapor.

According to the state of the art, oxides are used today without exception tion catalysts used from the active catalyti mass, mixed with different ceramic substrates germ materials exist and to balls, strand sections, Rings or stars have been deformed. These catalysts can only be used in bulk, preferably in horizontal hordes, which are arranged on top of each other are flowed through in succession. Which are free on oxidation heat must be dissipated through heat exchangers. For this purpose, the gas stream is out of the reactor several times and inserted after the heat exchange. Reactor and heat Exchangers do not form a single structure (German patent No. 28 38 112). Attempts have also been made to use reactors vertical gas-permeable walls to build a waa enable fair flow through the catalyst bed should (German Patent No. 37 40 255). The Ver using a monolytic contact with 775 channels a square decimeter is proposed (German patent No. 31 28 060). With a conversion system that out any number of separate contact stoves, from which each have a catalyst layer and a heat exchanger in a common housing, the pipe is tried to minimize the need for cables (German patent no. 29 21 024). Even large tube reactors with a variety of Pipes with internal catalyst bed and rivers liquid cooling from the outside have been shown as a solution German Patent No. 30 06 900).  

The is liable for all proposed and practiced solutions Lack of that the catalyst with a little heat conductive ceramic carrier is connected, which also has and is not too great mechanical strength is resistant to abrasion. The result is that a large volume share of the catalyst is ineffective because of internal overheating that the reactor can be built around the catalyst bed and that, in order to avoid excessive heights, the necessary The heat exchanger must stand outside the reactor, what long gas paths between the individual units required. The gas distribution must also follow before each catalyst layer the heat exchange can be made again, which creates additional space required in the reactor.

The aim of the invention is the known oxidation Disadvantages affecting catalysts, such as low heat conductivity, no possibility of constructive Integration of the catalyst carrier into the reactor structure, up to previous spatial separation of reactor and heat exchanger too remove.

The invention has for its object a novel Reactor to develop that as a component metal sponge with applied, catalytically active mass as Contains oxidation catalyst and thereby the coupled Her Provision of sulfur trioxide and high pressure steam in one building body allows.

The object is achieved by ste vert existing frames are arranged side by side as sections, being frame, in the metal sponge with the one on the surface active catalytic mass located vertically is inserted, followed by frames, the well-known pipe contain boiler elements as steam generator and the individual Frame fixed, but detachable together to form a sandwich reactor are connected.  

The invention is illustrated by the following example become.

example

As can be seen from Fig. 1 (top view) and 2 (side view), the frames in which the catalyst is arranged are designed so that the metal sponge structure is about 0.5 m thick.

With the frame size 5.5 × 12 m (5.5 m high, 12 m wide) can hold about 33 cubic meters of catalyst sponge in one frame be accommodated. In total there are 165 in five frames Cubic meters of catalyst sponge included. The frames are as vertical lattice built into which the catalyst sponge packs are inserted.

After the first section (frame) catalyst K1 are in Strö direction of the sections W1 to W3 arranged, of which W1 is a steam superheater, W2 and W3 each have an evaporator section are, because in the first section catalyst K1 about 60% of Sulfur trioxide and heat arise. Then they follow second section catalyst K2, section evaporator W4, the section catalyst K3, the section evaporator W5. For the case that worked according to the double catalysis process is followed by the gas collector G1, through which the reaction mixture is led out of the reactor.

It is reintroduced into the gas distributor V2 Reactor. After flowing through the sections K4 and K5 follows the section water heater W6, in which the boiler feed water is brought to the evaporator temperature. Who joins Eating gas collector G2 serves to lead out the now full constantly reacted reaction mixture from the reactor.

The reactor with an integrated steam generator has a total length of about 15 m and produces 800 t of sulfur in 24 hours trioxide, 336 t high pressure steam (450 degrees Celsius, 41 bar) and an additional 340 t of hot water (260 degrees Celsius, 41 bar).

Reference list

K1 catalyst section 1
K2 catalyst section 2
K3 catalyst section 3
K4 catalyst section 4
K5 catalyst section 5
W1 heat exchanger section 1 superheater
W2 heat exchanger section 2 evaporator
W3 heat exchanger section 3 evaporator
W4 heat exchanger section 4 evaporator
W5 heat exchanger section 5 evaporator
W6 heat exchanger section 6 water heater
V1 gas distributor section 1
V2 gas distributor section 2
G1 gas collector section 1
G2 gas collector section 2
E1 reaction mixture input
E2 boiler feed water input
A1 reaction mixture output
A2 high pressure steam outlet
Z1 reaction mixture for intermediate absorption
Z2 reaction mixture from intermediate absorption

Claims (3)

1. Reactor with oxidation catalyst, the known tubular boiler elements as a heat exchanger in the flow direction of the reaction mixture, characterized in that vertically standing frames are arranged side by side as sections, with one or two sections with catalyst K1 to K5 in Fig. 1 and 2) one or more sections containing known tubular boiler elements as heat exchangers (W1 to W6 in Figs. 1 and 2) follow in the flow direction of the reaction mixture and these sections, each of which consists of a frame with a vertical lattice arranged therein , detachably directly connected to each other, with the sections of the catalyst standing vertically in the sections K1 to K5 in the lattice work, which consists of an open-celled, large-pored metal sponge with a pore size of 0.1 to 10.0 mm diameter, on the upper surface the catalytically active mass of vanadium pentoxide and additional components is applied, inset gt and the sections V1 and V2 in Figs. 1 and 2, the distributors for the entering into the reactor, the sections G1 and G2 in Figs. 1 and 2 are the collectors for the reaction mixture to be led out of the reactor, whereby there is a gas impermeable partition between the sections G1 and V2. 2. Reactor with oxidation catalyst according to claim 1 thereby characterized that on the gas collector G1 and the gas distributor V2 is dispensed with. 3. reactor with oxidation catalyst according to claim 1 and 2 da characterized in that instead of the metal sponge catalyst a conventional catalyst is used.