Chemical apparatus and process disinfecting – deodorizing – preser – Chemical reactor – Inorganic sulfur acid or anhydride producing type
Patent
1996-08-15
1998-09-01
Straub, Gary P.
Chemical apparatus and process disinfecting, deodorizing, preser
Chemical reactor
Inorganic sulfur acid or anhydride producing type
423522, C01B 1748, C01B 1780, C01B 17765
Patent
active
058007881
DESCRIPTION:
BRIEF SUMMARY
BACKGROUND OF THE INVENTION
The present invention relates to a new reaction container and a new plant for the production of primarily sulfuric acid and a new process for the production of primarily sulfuric acid, the process relating to the so called contact process.
Sulfuric acid belongs to the basic chemicals and is the basis for a large spectrum of other products, such as hydrochloric acid, aluminum sulfate, ammonium sulfate, calcium sulfate and superphosphate. Thus, it occupies a central position in the chemical industry.
There are two industrial methods for the production of sulfuric acid, viz. the contact process and the leaden chamber process. The leaden chamber process is the oldest process and is hardly used anymore.
When producing sulfuric acid according to the contact process, one starts off from elementary sulfur, sulfur-containing minerals and/or unclean sulfuric acid. For the two former cases, the raw material is burnt to sulfur dioxide which in turn is oxidized to sulfur trioxide, which is absorbed in sulfuric acid of different concentrations, depending upon whether the final product shall be 94 to 98% or oleum. The contact mass or the catalyst for the oxidation is usually vanadium pentoxide mixed up with potassium-aluminum silicate or any other unmeltable substance. In order to further elucidate the generally used contact process, this will now be described with reference to FIG. 1.
The raw material sulfur dioxide flows in into the conduit 1 from a sulfur dioxide source (not shown). This sulfur dioxide is obtained for instance by combustion of elementary sulfur, pyrite or so called iron sulphide ore concentrate. Before this is led through the conduit 1, it has usually been cooled to about 40.degree. C., this heat being used for, e.g., steam production. To the conduit 1 is connected a conduit 2, out of which streams dried air which is mixed with the sulfur dioxide in order to adjust the right SO.sub.2 concentration by dilution, and in order to add O.sub.2 for oxidation. This air is led via a conventional air filter 4 to a drying tower 3 where it is dried by concentrated sulfuric acid. At its bottom end, the conduit 1 opens into a drying tower 5, in which the temperature is kept at between about 60.degree. and 80.degree. C. In this drying tower, the gas mixture of sulfur dioxide and air is dried by sulfuric acid. This tower is filled with, e.g., raschig rings or berl saddles. Before the gas mixture leaves the drying tower, it flows through a demister 6.
The drying in the drying tower 5 is necessary for avoiding the creation of a H.sub.2 SO.sub.4 mist in a later process step, which constitutes an important inconvenience for the environment and for the equipment.
After the drying, the gas mixture is pumped over a conduit 7 into a contact tower or converter 8, where it comes in contact with the hot catalyst mass (about 420.degree. C.) on several levels, whereby the conversion of SO.sub.2 to SO.sub.3 takes place. This reaction is strongly exothermic (about 100 kJ/mole converted SO.sub.2) and in order to maintain a suitable temperature level, the gas is let to pass a system of heat exchangers according to FIG. 1. Thus, the inflowing gas is first heat-exchanged in a heat exchanger 9 with a gas mixture mainly consisting of pure SO.sub.3 and air relating from the bottom part of the contact tower 8, which is led over a conduit 10. Thereby, the temperature of the gas flowing in from conduit 7 is increased. In order to further increase the temperature of this gas, it is thereafter led through a second heat exchanger 11 and is heat-exchanged in this heat exchanger with a gas side-outtake 12 from the contact tower 8, which is reintroduced into the contact tower after having flown through the heat exchanger 11, usually into the same level.
In order to improve the heat economy, also a part stream 13 is taken out from a lower level in the contact tower 8, which part stream is cooled in a heat exchanger 14 and then led over a conduit 42 into an intermediate absorption tower 15, where the sulfur trioxide is a
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Sandvik AB
Straub Gary P.
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