Apparatus and process for the continuous reaction of a liquid with a gas over a solid catalyst
View Patent ↗A reactor, which is capable of accommodating a reaction in which at least three phases are present and at least one gaseous starting material and at least one liquid starting material are reacted in cocurrent over a fixed-bed catalyst to give one or more product(s), contains at least one first zone in which a catalyst is present as a fixed bed; and at least one second zone whose size corresponds to a reactor cross section and which is separated from the at least one first zone by a distributor plate provided with at least one hole and in which at least one liquid and at least one gaseous starting material enter the reactor. The distributor plate is provided with at least one static mixer which is located in the at least one hole on at least one side of the distributor plate.
1. A reactor, comprising:
at least one first zone in which a catalyst is present as a fixed bed; and
at least one second zone whose size corresponds to a reactor cross section and which is separated from said at least one first zone by a distributor plate provided with at least one hole and in which at least one liquid and at least one gaseous starting material enter said reactor;
wherein said distributor plate is provided with at least one static mixer which is located in said at least one hole on at least one side of the distributor plate;
said reactor being capable of accommodating a reaction in which at least three phases are present and at least one gaseous starting material and at least one liquid starting material are reacted in cocurrent over a fixed-bed catalyst to give one or more product(s);
wherein a length-to-diameter ratio of the reactor is 2.6 or less.
2. The reactor as claimed in claim 1 , wherein the distributor plate comprises holes in or on which said at least one static mixer is located in such a way that a reaction mixture has to pass through said at least one static mixer in order to get from one side of the distributor plate to the other side of the distributor plate.
3. The reactor as claimed in claim 1 , wherein the reactor has a length-to-diameter ratio of 1.8 or less.
4. The reactor as claimed in claim 1 , wherein the number of static mixers per square meter of the reactor cross section is from 70 to 500.
5. The reactor as claimed in claim 1 , wherein the number of static mixers per square meter of reactor cross section is from 120 to 280.
6. The reactor as claimed in claim 1 , wherein the static mixers are uniformly distributed.
7. The reactor as claimed in claim 6 , wherein three adjacent static mixers are arranged in the shape of an equilateral triangle.
8. The reactor as claimed in claim 1 , which can be used in all modes of operation of a three-phase reactor.
9. A process, comprising:
reacting at least one gaseous starting material and, at least one liquid starting material in the presence of a fixed bed catalyst in at least one reactor as claimed in claim 1 ;
wherein the starting materials are flowing in cocurrent through the reactor.
10. The process as claimed in claim 9 , wherein butadiene or at least one butadiene-containing stream is hydrogenated to linear butene or a mixture comprising linear butene.
11. The process as claimed in claim 10 , wherein a butadiene-containing stream is used as liquid starting material which contains from 5 to 100% by weight of at least one multiply unsaturated olefin.
12. The process as claimed in claim 11 , wherein a feed stream is mixed with a further stream before entry into a first reactor so as to give a butadiene-containing stream which contains less than 20% by weight of butadiene.
13. The process as claimed in claim 10 , wherein less than the stoichiometrically required amount of hydrogen is fed in as gaseous starting material for the hydrogenation.
14. The process as claimed in claim 9 , wherein a selective reaction between a liquid and a gas is carried out.
15. The process as claimed in claim 14 , which is a hydrogenation.
16. The process as claimed in claim 9 , wherein the starting materials flow through the reactor from the top downward.
17. The process as claimed in claim 9 , which is carried out so that the mean Sauter diameter of gas bubbles dispersed in the liquid after exit from the static mixers is less than 5 mm.
18. The process as claimed in claim 9 , wherein a mean Sauter diameter of the gas bubbles dispersed in the liquid after exit from the static mixers is less than 1 mm.
19. The process as claimed in claim 9 , wherein a reaction is carried out in which a solubility of the gaseous starting material in the liquid starting material under the reaction conditions is insufficient to bring about a conversion of the starting materials.
20. The process as claimed in claim 9 , wherein a palladium-containing catalyst is used.