WO2012043915A1

WO2012043915A1 - F-t bubble column reactor having a plurality of re-dispersible disks

Info

Publication number: WO2012043915A1
Application number: PCT/KR2010/007227
Authority: WO
Inventors: 이호태; 정헌; 천동현; 김학주; 양정일; 양정훈
Original assignee: 한국에너지기술연구원
Priority date: 2010-09-30
Filing date: 2010-10-21
Publication date: 2012-04-05
Also published as: KR101211376B1; KR20120033623A; WO2012043914A1

Abstract

The present invention relates to an F-T bubble column reactor having a plurality of re-dispersible disks which generates synthetic fuel through a reaction between a coal synthesis gas and a catalyst contained in slurry. The F-T bubble column reactor includes: a bubble column reactor body in which the slurry containing the catalyst is stored; a dispersive disk which is arranged at a bottom surface of the bubble column reactor body to change bubble particles of the synthetic gas supplied through an inflow tube into the uniform bubble particles and to supply the uniform bubble particles to an inside of the bubble column reactor body; and a plurality of re-dispersible disks which are arranged to divide the inside of the bubble column reactor into multiple stages in a shape of tread and uniformly redisperse the bubble particles of the synthetic gas supplied from the dispersive disk, the re-dispersible disks including rectangular through-holes which are punched into a grating structure on surfaces thereof.

Description

F-T Bubble Column Reactor with Multiple Redistribution Discs

The present invention relates to an FT bubble column reactor having a structure capable of increasing the synthesis rate of the synthesis gas, and more specifically, uniformly bubbles particles of the synthesis gas reacting with the catalyst in the reactor body Fischer-Tropsch The present invention relates to an FT bubble column reactor having a plurality of redistribution disks having a structure capable of activating a reaction with a catalyst by increasing a collection rate of syngas in the reactor body by providing a plurality of redistribution disks for redispersion. .

In general, bubble column reactors have the advantages of high heat and mass transfer and are widely used in reactions such as biochemical reactions, wastewater treatment and coal liquefaction.

In this bubble column reactor, the reaction is carried out while the reactor gas (synthesis gas) passes through a continuous phase consisting of a catalyst and a product.

At this time, the mass transfer rate through uniform contact and dispersion between the reactants and the catalyst is very important as a variable for determining the reaction efficiency.

As a main means for increasing the mass transfer rate of the reactor body, a method of increasing the fluidity in the reactor and a method of increasing the gas collection rate in the continuous phase are mainly utilized.

As a method of increasing the mass transfer rate in the reactor, there is a method of increasing the gas collection rate. The gas capture rate is defined as the volume fraction of the gas phase present in the continuous phase.

According to Letzel et al. (1999), the ratio of gas capture rate to mass transfer rate of the reactant is constant at about 0.5. Therefore, increasing the gas capture rate is an important variable for increasing the mass transfer rate.

In general, the collection rate of the reactor is influenced by the linear velocity of the reactor, the diameter of the reactor, the physical properties of the continuous phase, and the like.

That is, as the linear velocity of the reactor gas increases, the diameter of the reactor decreases, and the viscosity and surface tension of the continuous phase decrease, the collection rate of the reactor gas in the reactor tends to increase. As such, much research has been conducted on changes in the rate of collection of the reactor according to the reaction conditions or the reaction additives. However, the study on the reactor collection rate according to the design of the reactor is limited.

In addition, numerous interactions of agglomeration and cracking between the bubbles of the reactant are repeated as the reactant enters and passes through the reactor. In this process, the size of the bubble particles is usually increased, thus increasing the rate of bubble rise.

In general, the rate of rise of bubbles increases in proportion to 0.5 square of the size of the bubble particles. Increasing the bubble rise rate is negative in terms of the rate of collection of the reactor gas since it leads to a decrease in the residence time in the reactor for a unit time.

For this purpose, some researchers have been using the conventional sieve plate as a redistribution disk.

However, the size of the through-holes and the aperture ratio are very important for evenly dispersing the gas in the form of a thin plate.

Failure to do so will adversely affect the formation of a gas layer under the redistribution disk.

In particular, if a large number of redistribution disks are installed, the collection rate of the reactor gas (synthesis gas) can be increased, and the spacing of the redistribution disks will be very important.

The present invention has been made in view of the above problems, and the first object of the present invention is to uniformly redistribute the bubble particles of the synthesis gas reacting with the catalyst in the reactor body and the Fischer-Tropsch reaction. In addition, the present invention provides a FT bubble column reactor having a plurality of redistribution disks having a structure capable of activating a reaction between a catalyst and a syngas in a reactor.

Furthermore, the second object of the present invention is to prevent the formation of a gas layer under the redispersion disk, while re-dispersing the synthesis gas to maintain a constant bubble size, a plurality of ash that can increase the capture rate of the synthesis gas To provide an FT bubble column reactor having a dispersion disk.

The present invention has been made in view of the above problems, the first object of the present invention relates to a FT bubble column reactor having a plurality of redispersion disk, for this purpose is to react the coal synthesis gas with the catalyst contained in the slurry In the bubble column reactor for producing a synthetic fuel, a bubble tower reactor body in which the slurry containing the catalyst is stored; and converts the bubble particles of the synthesis gas supplied through the inlet pipe into uniform bubble particles to be supplied into the reactor body. Dispersion disk is disposed on the bottom surface of the reactor body so as to be arranged, and the inside of the reactor body is arranged in a multi-stage partition in a trade form, a plurality of ash to uniformly redistribute the bubble particles of the synthesis gas supplied from the dispersion disk It is made, including; the redistribution disk is a rectangular tube perforated in the form of a lattice structure on the surface It characterized in that holes are formed in plurality.

In the second invention, in the first invention, it is preferable that a plurality of the redistribution discs are installed at intervals ranging from 300 mm to 500 mm.

In the third invention, in the first or second invention, the pitch of each side of the through hole of the redistribution disk is preferably in the range of 2.5 mm to 6.5 mm.

In the fourth invention, in the third invention, the aperture ratio of the redistribution disk is preferably in the range of 90% to 95%.

According to the FT bubble column reactor having a plurality of redispersion disks according to the present invention, by installing a plurality of redispersion disks in the inside of the bubble column reactor body, by re-dispersing the synthesis gas while preventing the generation of a gas layer to uniform bubble size It can be maintained so that there is an effect that can increase the capture rate of the synthesis gas.

1 is a block diagram of a F-T bubble column reactor having a plurality of redistribution disk according to the present invention,

2 is a plan view showing a redistribution disk extracted in FIG.

3 is an installation conceptual diagram according to the position and number of redistribution disks;

4 is a graph showing a change in synthesis gas collection rate according to the position and number of the redistribution disk according to FIG.

5 and 6 are graphs showing the collection rate of syngas according to the pitch size of one side of the rectangular through hole of the redistribution disk.

Hereinafter, the F-T bubble column reactor having a plurality of redistribution disks according to the present invention will be described in detail together with the accompanying drawings.

1 is a block diagram of a F-T bubble column reactor having a plurality of redistribution disk of the present invention, Figure 2 is a perspective view showing a redistribution disk extracted in FIG.

As shown in Figures 1 and 2, the present invention relates to a FT bubble column reactor for producing a synthetic fuel by the catalyst in the slurry and the Fischer-Tropsch reaction contained in the slurry, more In detail, a plurality of redispersion disks are provided to uniformly redistribute bubble particles of the synthesis gas reacting with the catalyst in the reactor body and the Fischer-Tropsch reaction. It relates to a FT bubble column reactor (100) having a plurality of redistribution disk of the structure capable of activating the reaction of the catalyst and syngas.

The FT bubble column reactor 100 having a plurality of redistribution disks of the present invention includes a reactor body 10, a dispersion disk 20 disposed on a bottom surface of the reactor body 10, and an inside of the reactor body 10. It consists of a redistribution disk 30 which divides into multiple stages.

Here, a slurry (oil or wax) containing a catalyst is stored in the reactor body 10 and an outlet pipe for discharging unreacted syngas and chemical gas (methane, propane, pentane, etc.) generated by the reaction ( 12) may be provided.

The dispersion disk 20 converts the bubble particles of the synthesis gas supplied through the inlet pipe 11 into uniform bubble particles to be supplied into the reactor body 10 so that the bottom surface of the reactor body 10 can be supplied. It is a structure that is placed on.

Here, the dispersion disk 20 has a plurality of discharge holes 21 are formed on the surface is configured to uniformly supply the bubble particles of the synthesis gas.

In addition, the surface of the redistribution disk 30 has a plurality of rectangular through-holes 31 formed in the form of a lattice structure is formed to uniformly redistribute the bubble particles.

The redistribution disk 30 is arranged to be divided into a multi-stage partition within the reactor body 10, and serves to uniformly redistribute the bubble particles of the synthesis gas supplied from the dispersion disk 20.

Here, the opening ratio of the redistribution disk 30 is preferably in the range of 90% to 95%. When the opening ratio of the redistribution disk 30 is 90% or less, a pressure drop is applied to the lower portion of the redistribution disk 30. This is because an increase in gas layer results in blocking the contact between the synthesis gas and the catalyst, and in the case of more than 95%, the synthesis rate and catalyst of the synthesis gas are compared with the case where the redispersion disk 30 is not installed. It is not preferable because it does not show a big difference in terms of particle dispersing capacity.

On the other hand, the redistribution disk 30 is installed in the interior of the reactor body 10 at intervals ranging from 300mm to 500mm, the number and spacing may vary depending on the size (diameter and height) of the reactor body 10. .

In addition, the size of the pitch P of one side of each through hole 31 formed in the redistribution disk 30 is preferably in the range of 2.5 mm to 6.5 mm.

The installation interval of the redistribution disk 30 and the size of each through hole 31 will be described in detail below.

Hereinafter, the number and installation intervals of the redistribution disk according to the present invention will be described in detail with the accompanying drawings.

3 is a conceptual diagram illustrating the installation and the number of redistribution disks, and FIG. 4 is a graph illustrating a change in the synthesis gas collection rate according to the positions and the numbers of the redistribution disks.

First, as shown in FIG.

L1: A redispersion disc was installed at the bottom surface of the reactor body and 40 cm high.

L2: The redispersion disc was installed at the bottom of the reactor body and 80 cm high.

L3: A redispersion disc was installed at the bottom surface of the reactor body and 120 cm high.

L123: The variation of the synthesis gas collection rate was confirmed by installing a plurality of dispersion disks at intervals of 40 cm from each other inside the reactor body.

As a result, as shown in FIG. 4, it was observed that the collection rate of the syngas increased as the distance between the redispersing disks moved away from the bottom surface of the reactor body.

In particular, in L1, the synthesis gas collection rate was almost similar to that without the redispersion disc, and thus, it was confirmed that there was no effect of bubble splitting or redispersion of bubbles by the redistribution disc.

In addition, in the case of L2 and L3, the capture rate of syngas increased compared to L1, but the effect was insignificant.

On the other hand, when a large number of redispersion discs such as L123 are installed at 40 cm intervals, the redispersion disc continuously interferes with the increase of bubbles due to the synthesis gas coalescing, thereby increasing the capture rate of the synthesis gas.

As can be seen in the above experiment, the redispersion disk of the present invention is preferably installed in the reactor body a plurality of intervals in the range 300mm ~ 500mm.

Hereinafter, the capture rate of the synthesis gas according to the pitch of one side of the through hole of the redistribution disk according to the present invention will be described in detail with the accompanying drawings.

As shown in FIG. 5 and FIG. 6, it was observed that the collection rate of the synthesis gas was changed according to the size of the pitch of the rectangular through-hole of the redistribution disk.

First, in FIG. 5, when the pitch of one side of the through hole is in the range of 1.1 mm to 1.61 mm, it can be seen that the capture rate of the synthesis gas is lower or similar to that of the case where there is no redispersion disk at low gas flow rate. This is because gas collection rate increases at high gas flow rates, but a gas layer is formed under the redistribution disk.

In addition, even when the pitch of one side of the through hole is 1.4 mm as shown in FIG. 6, at a low gas flow rate as in the case of 1.1 mm to 1.61 mm in FIG. I could see that. This is because gas collection rate increases at high gas flow rates, but a gas layer is formed under the redistribution disk.

In addition, when the pitch is 14.1mm, regardless of the gas flow rate, the capture rate of the syngas was lower or similar to that of the nondispersed disc. This is because the size of the bubble particles generated in the distributed disk is smaller than the size of the through-hole, the size of the bubbles in the redistributed disk does not decrease, but rather the bubbles rise together to increase the speed of bubbles.

On the other hand, when the pitch P of one side of each of the through holes of the redistribution disk was in the range of 2.9 mm to 6.9 mm, it was found that the collection rate of the syngas increased.

In this case, since the size of the bubble particles generated in the dispersion disk and the size of the through-holes are similar or large, the synthesis gas is coalesced to prevent the bubbles from increasing, causing the redispersion effect of the bubbles to increase the capture rate of the synthesis gas. Could.

As described above, the present invention has been described with reference to the embodiments shown in the drawings, but this is merely exemplary, and it will be understood by those skilled in the art that various modifications and equivalent other embodiments are possible. will be.

Therefore, the true technical protection scope of the present invention will be defined by the technical spirit of the appended claims.

Claims

In the bubble column reactor for producing a synthetic fuel by reacting the coal synthesis gas with the catalyst contained in the slurry,

A bubble column reactor body 10 in which a slurry containing a catalyst is stored;

A dispersion disk 20 disposed on the bottom surface of the reactor body 10 so that the bubble particles of the synthesis gas supplied through the inlet pipe 11 can be converted into uniform bubble particles and supplied into the reactor body 10;

And a plurality of redistribution disks 30 arranged inside the reactor main body 10 in a trade form, and uniformly redistributing the bubble particles of the synthesis gas supplied from the dispersing disk 20. It's done,

F-T bubble column reactor having a plurality of redistribution disk, characterized in that formed on the surface of the redistribution disk 30 a plurality of rectangular through-holes perforated in the form of a lattice structure.
The method of claim 1,

The redistribution disk 30 is a F-T bubble tower reactor having a plurality of redistribution disk, characterized in that a plurality of intervals are installed in the range 300mm ~ 500mm.
The method according to claim 1 or 2,

F-T bubble column reactor having a plurality of redistribution disk, characterized in that the pitch (P) of one side of each through hole 31 of the redistribution disk (30) is in the range of 2.5mm ~ 6.5mm.
The method of claim 3, wherein

The opening ratio of the redistribution disk 30 is F-T bubble column reactor having a plurality of redistribution disk, characterized in that in the range of 90% ~ 95%.