JPS5845283B2 - How to fill the catalyst - Google Patents

Description

DETAILED DESCRIPTION OF THE INVENTION The present invention relates to a method of filling a cylindrical catalyst body into a gas or liquid processing reactor.

Recently, boilers, incinerators, chemical equipment,
2. Description of the Related Art Increasingly, devices are being installed to treat harmful substances or substances with bad smells contained in gases emitted from automobiles and the like.

When installing a dry catalyst treatment device as an exhaust gas treatment device, the catalyst filled in the reactor is usually spherical,
Most are in the form of pellets or crushed pieces.

However, when solid substances coexist in the processing gas, spherical,
In a catalyst layer using a catalyst body in the form of pellets or crushed pieces, there is a risk of clogging due to accumulation of solid substances in the catalyst layer.

In such cases, it is known that clogging of the catalyst layer can be prevented by filling the cylinder with a catalyst body and passing gas in the axial direction of the cylinder.

In this case, if the cylindrical catalyst bodies are packed closely together with individual catalyst bodies in contact with each other, not only will the outer active surface of the cylindrical catalyst body not be used effectively, but also the catalyst The disadvantage is that the differential pressure of the fluid passing through is large, which increases the operating cost and equipment cost of the device.

An object of the present invention is to provide a new method for improving the conventionally known method of arranging a cylindrical catalyst, thereby reducing the above-mentioned drawbacks and improving the performance of the device.

In order to achieve the above object, the present invention has the following configuration.

That is, a large number of cylindrical catalyst bodies are arranged in parallel inside a reactor, and a fluid is passed through the catalyst body in the axial direction of the catalyst body to cause the fluid to react by contacting the fluid with the catalyst body. In the filling method, when cylindrical catalyst bodies are regularly arranged at regular intervals in the reactor,
This is a catalyst filling method characterized in that the value of is in the range of 0.4 to 15.

Further, the present invention will be explained in detail with reference to the drawings.

The cross-sectional shape of the cylindrical catalyst used in the present invention may be circular, oval, triangular, square, or star-shaped, but is not particularly limited.
A circular or elliptical shape is preferable for catalyst production.

Further, the cross-sectional shape of the outside of the cylinder and the cross-sectional shape of the inside may be different, and there is no particular limitation on these shapes.

On the other hand, regarding the arrangement of the cylindrical catalyst bodies, the catalyst bodies are arranged so that the individual catalyst bodies are almost evenly dispersed in the reactor, and the value of K shown in the above formula is 0.4 to 15. It is necessary to ensure that the range is within the range.

Figures 1 to 3 illustrate the arrangement of catalyst bodies according to the present invention, in which a cylindrical catalyst body 1 and a lattice 2 are combined; Figure 1 is an orthogonal lattice, and Figure 2 is a parallel lattice. , FIG. 3 shows a case where an oblique lattice and a cylindrical catalyst body are used.

4 and 5 show a configuration in which projections 3 are provided on a part of the outside of the catalyst body without using a grid so that the projections are in contact with each other; FIG. FIG. 5 shows the application to a square cylindrical catalyst body.

The protrusion is not limited to this example, and the protrusion need not always be provided at a fixed position on each catalyst body, and a structure in which the protrusion directly contacts the outer circumferential wall of another catalyst body may be used.

Next, the effect of dispersing the catalyst will be explained.

According to the present invention, by regularly dispersing the cylindrical catalysts at regular intervals, the outer side of the cylindrical catalyst body The gas flow rate passing through the catalyst is increased, the catalyst on the outer surface of the cylindrical catalyst body is effectively used, and the activity of the catalyst as a whole is improved.In addition, the gas flow path of the catalyst packed bed is expanded. This has the dual effect of reducing the differential pressure of the fluid passing through the catalyst layer.

In addition, if the dispersion is very coarse, that is, if the value of K becomes large, the flow rate of the fluid passing through the catalyst decreases compared to the surface area of the catalyst, which increases the size of the device and reduces the efficiency of the catalyst, which is not preferable.

However, in this application, the relationship between the surface area of the cylindrical catalyst body and the flow rate of the fluid passing through the reactor is expressed by the value of K, and this value is limited to a certain range, so that the device size does not need to be larger than necessary. This also provides an excellent effect in that the size of the device can be made appropriate, so the device can be designed extremely economically.

As is clear from the implementation, the present invention
A range of 0.7 to 5 is appropriate and should preferably be 0.7 to K to 5.

Further, although the present invention is exemplified by gas processing, it is not limited to gas reactions, but is also applicable to structures that provide absorbents, adsorbents, and other functions in processes such as liquid processing, reactions, and gas absorption and adsorption. Needless to say, it is also applicable.

Example 1 The apparatus shown in FIG. 6 was used to treat the exhaust gas of a boiler using heavy oil as the firing material.

FIG. 6 shows a part of the exhaust gas taken out from the flue 4 of the boiler through a pipe 5, and the exhaust gas is led through a heater 6 to a reactor 9 having an inlet 8 and an outlet 8, and is then brought out from an outlet 12 by a blower 11. Figure 2 shows a device for releasing gas from the reactor.

Moreover, 14 is supplied to the inlet T from here.

The reactor 9 is equipped with an alumina cylindrical catalyst (outer diameter: 35ttrx1, inner diameter: 20111m) carrying 5% by weight of iron oxide.
It has a structure in which 19 catalyst layers 10 are arranged in series as shown in FIG. 7 in a structure 13 having a length of 500 cm.

FIG. 1 shows the arrangement of the catalyst bodies. First, a single catalyst body is placed at the center of the structure 14, and from this catalyst body, touches are made at equal intervals on the rays arranged every 600. The structure is such that a medium is arranged and other catalyst bodies are arranged so that the center of each catalyst body forms an equilateral triangle.

The inner diameter of the structure 13 was varied depending on the value of each catalyst layer.

In this embodiment, when =1, the inner diameter of the structure 13 is 20
It becomes 511I.

Boiler exhaust gas was supplied to the apparatus shown in FIG. 6 at a rate of 50 ON gauze, heated to 400° C. by heater 6, and ammonia gas was added in an amount equal to the NO concentration in the exhaust gas.

The exhaust gas components are shown in Table 1. FIG. 8 shows experimental results obtained by using the apparatus shown in FIG. 1, using the gases shown in Table 1, and varying the value of K under the above conditions.

Judging from the results shown in FIG. 8, the activity of the catalyst is at its maximum when the value is around 1.

On the other hand, if the value is less than 0.4, the pressure difference across the catalyst layer will increase rapidly, which is not preferred in practice.

Furthermore, when the value becomes 15 or more, the activity of the catalyst layer as a whole decreases.

Therefore, the effect of the present invention is remarkable when the value is 0.4.
to 111, preferably from 0.7 to 5.

Example 2 An apparatus for oxidizing and removing methanol from methanol-containing air is shown using the apparatus shown in FIG.

Methanol-containing air is sent from the blower 11 to the reactor 9 from the slot 1 via the heater 6.

The reactor 9 is equipped with five stages of catalyst layers 10 in series, and the air from which methanol has been removed is discharged from the outlet 8. Sixteen media (the dimensions are the same as in Example 1) are arranged in a square cross-sectional structure 13 as shown in FIG.

FIG. 10 shows the arrangement of the catalyst bodies, which are arranged at equal intervals vertically and horizontally, and when K=1, the length of the inner side of the structure 13 is 168 squares.

4001 methanol was added to the above apparatus by changing the value of K.
) 1111 was supplied at a flow rate of 500 Nm, heated to 150° C. by heater 6, supplied to the reactor, and discharged from outlet 8.

The results obtained are shown in FIG.

In this example as well, results showing the same behavior as in FIG. 8 were obtained.

[Brief explanation of the drawing]

1 to 5 illustrate the arrangement of catalyst bodies according to the present invention. 6 and 9 are schematic diagrams of the apparatus used in Examples 1 and 2, respectively. Figures 1 and 10 are diagrams showing the arrangement of catalyst bodies in the reactors shown in Figures 6 and 9, and Figures 8 and 11 show the experimental results of Example 1 and Example 2, respectively. This is a graph showing. 1... Catalyst body, 2... Lattice, 3...
... Protrusion, 4 ... Flue, 5 ... Pipe, 6 ... Heater, T ... Inlet, 8 ...
...Outlet, 9...Reactor, 10...
... Catalyst layer, 11 ... Blower, 12 ...
...Exhaust port, 13...Structure, 14...
・Ammonia gas cylinder.

Claims (1)

[Claims] 1. A large number of cylindrical catalyst bodies are arranged in parallel inside a reactor, and a fluid is caused to react by passing a fluid in the axial direction of the catalyst bodies and bringing the fluid into contact with the catalyst bodies. In the method for packing catalyst bodies for the purpose of the present invention, when cylindrical catalyst bodies are regularly arranged at regular intervals in the reactor, the value of K shown by is in the range of 0.4 to 15. A method for filling a catalyst body, characterized in that: