JPS6031824A - Catalytic reaction tower - Google Patents

Abstract

PURPOSE:To make it possible to perform efficient reaction, by providing a means for moving and recirculating a catalyst layer while providing a partition part to a gas flowline so as to reversely flow gaseous streams to each other. CONSTITUTION:Stock gas is introduced into a gas flowline 12B from an introducing port 2 and passed through a ring shaped catalyst layer 8 toward a centripetal direction to reach the gas flowline 12A at a central part. Subsequently, said gas passes the catalyst layer 8 in a direction reverse to the centripetal direction to reach the outside gas flowline 12B where again converted to an upward direction. Hereinafter, the gas rises while mutually passes through the catalyst layer in a centripetal and a centrifugal directions in the same way and is reacted with the catalyst in the catalyst layer 8 to form reaction gas 3 which is, in turn, taken out of the system from an outtake port 4. Recirculated gas 5 is introduced into the gas flowline 12A from an introducing port 6 and dilutes the stock gas to carry the same upwardly.

Description

DETAILED DESCRIPTION OF THE INVENTION The present invention relates to a catalytic reaction tower, and more particularly to a catalytic reaction tower that prevents channeling, welding, carbon deposition, etc. of a catalyst layer.

Generally, as a catalytic reaction tower for causing a reaction by passing a gas through a catalyst layer, one is known in which several towers each having a catalyst layer are arranged and the gas is caused to sequentially pass through these catalyst layers to cause a reaction. In this case, the catalyst bed is (1) a fixed bed, and the reaction heat generated by the reaction in each reaction tower is recovered by heat-exchanging the reaction gas with a cooling medium such as water.

However, such a reaction tower has disadvantages in that channeling, welding, carbon deposition, short baths, etc. of the catalyst layer are likely to occur, and the structure is complicated due to the use of a plurality of catalyst beds.

The object of the present invention is to eliminate the above-mentioned drawbacks of the prior art, and to provide a catalyst that does not cause channeling, welding, carbon deposition, etc. of the catalyst layer, has a simple structure, and can efficiently carry out reactions in a column. The purpose is to provide a reaction column.

The present invention provides a catalytic reaction tower in which a gas is caused to pass through a catalyst layer to cause a reaction. It is characterized by having a partition part provided in the inner and outer gas flow paths so that the gas flow is alternately reversed, and a cooling pipe provided in a direction perpendicular to the gas flow passing through the catalyst layer. shall be.

(2) Hereinafter, the present invention will be explained in more detail with reference to the drawings.

FIG. 1 is a sectional view showing an embodiment of the catalytic reaction tower of the present invention. This device consists of an inlet 2 for a raw material gas 1, a reactant gas 3
A moving catalyst bed filled between a reaction column main body 7 having an outlet 4 for the gas and an inlet 6 for the circulating gas 5, and a gas-permeable inner cylinder 10 and an outer cylinder 11 provided in the longitudinal direction of the main body. 8 (hereinafter referred to as the catalyst layer), a cooling pipe group 9 provided in the longitudinal direction within the catalyst layer, and a gas flow provided on the inside (inner cylinder side) and outside (outer cylinder side) of the catalyst layer, respectively. channels 12A and B, such that gas flow enters channel 12B from the outer cylinder side, passes through catalyst N8 to channel 12A, and then flows in the opposite direction from channel 12A through catalyst layer 8 to channel 12B. In addition, a partition portion 30 provided in the gas flow paths 12A and 12B
and 31. A catalyst inlet 13 and a catalyst outlet 14 are provided at the upper and lower parts of the reaction column body 7, respectively. Further, the cooling pipe group 9 is
As shown in Fig. 2, a large number of thin tubes are built into the annular catalyst layer 8 concentrically (3).
The first part 4J is connected to the cooling medium discharge 1':I]5 provided at the upper and lower parts of the reaction column main body 7 and the supply port 16, respectively. Note that 17 is a catalyst hopper, 18 is a catalyst regenerator, 19 is a regenerated catalyst hopper, and 20 is a heat exchanger or a CJ gas-liquid separation tank.

In the above configuration, the raw material gas 1 is introduced into the gas flow path 12B from the inlet 2, and as indicated by the arrow in FIG.
It passes through the annular catalyst layer 8 in the center direction, reaches the central gas flow path 12A, changes direction upward from there, then passes through the catalyst layer in the opposite direction (centrifugal direction) to the outside gas flow path 12A. The gas reaches the flow path 12B, where it changes direction again in one direction, and then passes through the catalyst layer in the center direction in the same manner as described above, and in the same manner, inside the catalyst layer 8 in the center direction and in the centrifugal direction. It rises while passing alternately, reacts with the catalyst in the catalyst layer, becomes the target reaction gas 3, and is taken out of the system through the outlet 4. In addition,
The circulating gas 5 is introduced into the gas flow path 12A from the inlet 6,
Dilute the raw materials and get lucky! Watch. The catalyst is introduced into the catalyst layer 8 from the regenerated catalyst hopper 19 through the catalyst (4) inlet 13, moves from the top to the bottom at a constant speed under the action of gravity, and passes through the catalyst outlet 14.
is discharged to the outside. The discharged catalyst is introduced into the catalyst regenerator 18 via the catalyst hopper 17, heated and regenerated by steam, etc., and then mechanically transferred to the upper regenerated catalyst hopper 19 using a conveyor, etc., or by an air lift, a steam lift, etc. carried. A cooling medium is introduced into the cooling pipe group 9 from the supply port 16, and the cooling medium heated by the reaction heat is discharged from the discharge port 15, and is exchanged with another heat medium in the heat exchanger 20, so that it can be used effectively. or gas-liquid separation tank 20
The steam is separated into water and steam, and the steam is led outside for effective use.

In the catalyst tower of the present invention, it is preferable that the catalyst bed 8 works as a moving bed.
It is also possible to act as a fixed bed.

The catalytic reaction column according to the present invention can be used, for example, to carry out various catalytic reactions using carbon oxide as a raw material, such as CO conversion reactions, methanol synthesis reactions or methane synthesis reactions (5), and various reactions using other raw material gases. Can be used in catalytic reactions.

According to the present invention, the catalyst layer is not divided as in conventional methods, but is formed continuously, so it can be used not only as a fixed bed but also as a moving bed, and the catalyst can be continuously applied during the reaction. Or it can be regenerated and circulated intermittently.

In addition, since the catalyst and gas flow in countercurrent flow, the closer to the top of the tower the fresher the catalyst and the gas in which the reaction has progressed will come into contact, making it possible to increase the reaction efficiency.

Furthermore, the gas flow inside the catalyst 1M changes alternately between the central direction and the centrifugal direction, and the gas is remixed inside and outside the catalyst layer, which prevents channeling, welding, carbon deposition, short baths, etc. of the catalyst layer. Hard to occur.

In addition, since the gas flow is perpendicular to the cooling tube group, channeling caused by the installation of the cooling tubes is prevented, and since there are many opportunities for gas to come into contact with the cooling tube group, the reaction temperature is made more uniform. It is also easy to do (6). Furthermore, since the outer surface of the cooling tube is in direct contact with the catalyst layer, it is easy to increase the cooling effect. It can also have an effect.

The catalytic reaction tower of the present invention has a larger volume ratio of the catalyst layer than a multi-tubular reaction tower and has an extremely simple structure, so it is suitable for high-pressure, high-temperature reactions and generation of high-pressure steam.

[Brief explanation of the drawing]

FIG. 1 is a sectional view of a catalytic reaction tower showing an embodiment of the present invention, and FIG. 2 is a sectional view taken along the line 1 to 2 in FIG. 1 in the direction of the arrows. In the figure, ■ is the raw material gas, 3 is the reaction gas, 5 is the circulating gas, 7 is the reaction tower main body, 8 is the catalyst layer, 9 is the cooling pipe group, 1
2A and 12B are gas flow paths, 13 is a catalyst inlet, 14 is a catalyst outlet, and 18 is a catalyst regenerator. Agent Patent Attorney Takeshi Kawakita (7) Figure 1

Claims (1)

[Claims] (1) In a catalytic reaction tower in which gas is caused to pass through a catalyst layer for reaction, a means for moving and circulating the catalyst layer, a gas passage provided inside and outside the catalyst layer, and a gas entering the catalyst layer and a cooling pipe provided in the direction perpendicular to the gas flow passing through the catalyst layer. catalytic reaction tower.