WO2007114271A1

WO2007114271A1 - Bubble tower type hydrocarbon synthesis reactor

Info

Publication number: WO2007114271A1
Application number: PCT/JP2007/056911
Authority: WO
Inventors: Yasuyuki Osawa; Yasuhiro Onishi; Eiichi Yamada; Yuzuru Kato; Osamu Wakamura
Original assignee: Nippon Steel Engineering Co., Ltd.
Priority date: 2006-03-30
Filing date: 2007-03-29
Publication date: 2007-10-11
Also published as: MY154308A; AU2007232919A1; CN101432394A; AU2007232919B2; JP4980344B2; CN101432394B; JPWO2007114271A1

Abstract

Bubble tower type hydrocarbon synthesis reactor (100) comprising reactor main frame (110) accommodating slurry (120) having solid catalyst particles (124) suspended in liquid hydrocarbon (122), and distributor (140) disposed at an inferior portion of the reactor main frame (110) and used to feed a synthetic gas composed mainly of hydrogen and carbon monoxide into the slurry (120), wherein the reactor main frame (110) in its interior is provided with baffle plate (150) so as to block the side-wall side of the reactor main frame (110) and open the center part thereof.

Description

Specification

Bubble column type hydrocarbon synthesis reactor

Technical field

TECHNICAL FIELD [0001] The present invention relates to a bubble column type hydrocarbon synthesis reactor, and in particular, for performing a Fischer-Tropsch synthesis reaction by blowing a synthesis gas into a slurry in which solid catalyst particles are suspended in a liquid hydrocarbon. Reactor related.

This application claims priority on Japanese Patent Application No. 2006-95020 filed on Mar. 30, 2006, the contents of which are incorporated herein by reference.

Background art

[0002] A Fischer's Tropsch synthesis reaction (hereinafter referred to as "FT reaction") that produces hydrocarbon compounds and water from synthesis gas mainly composed of hydrogen and carbon monoxide 1 One example is a bubble column type slurry bed FT reaction system in which synthesis gas is blown into a slurry in which solid catalyst particles are suspended in a liquid hydrocarbon to perform the FT reaction. Hydrocarbon compounds synthesized by FT reaction are mainly used as raw materials for fuel oils and lubricating oils.

[0003] In an FT reactor used for this bubble column type slurry bed FT reaction system (hereinafter sometimes simply referred to as "reactor"), a slurry in which solid catalyst particles are suspended in liquid hydrocarbons is used. Then, FT reaction is performed by blowing the synthesis gas in the form of bubbles from the bottom of the reactor. At this time, inside the reactor, the liquid (slurry) is mixed by the air lift effect of the rising bubbles. However, if the liquid inside the reactor is thoroughly stirred by circulation throughout the entire height of the reactor (hereinafter referred to as “general circulation”), the gaseous hydrocarbons produced by the FT reaction (mainly C power C light hydrocarbon

14

The tendency of the bubbles containing a large amount of gas to move to the lower part of the reactor is increased by the fluid mixing (hereinafter referred to as “back mixing”) by the downward flow of the slurry. As a result, there is a possibility that the reaction rate inside the reactor is reduced in the entire region and the reaction conversion rate of the synthesis gas as the raw material is reduced.

[0004] In order to solve such a problem, the following method is used in a general bubble column reactor. However, the conventional force is also performed (for example, refer nonpatent literature 1). In other words, the internal space of the reactor is divided into the height direction (vertical direction) of the reactor by a perforated plate, etc., and the flow of bubbles in the reactor is forced out of the reactor with downward force upward (“plug” It is called “flow” and is close to the state where there is no backflow of fluid. As a result, mixing (general circulation) in the entire reactor can be suppressed.

[0005] Non-Patent Document 1: Hideaki Tsuge and Koji Unno, “Use, make, and eliminate“ bubble technology ”, first edition, Industrial Research Institute, Inc., April 2004, p. 75-81

Disclosure of the invention

Problems to be solved by the invention

However, in the bubble column type slurry bed FT reaction system, the liquid flow rate may be extremely small relative to the volume of the reactor. In this case, the net rising speed of the liquid (the superficial velocity in the tower) is close to zero. For this reason, if a perforated plate is installed, the resistance of the perforated plate inhibits the rise of bubbles, and the rate of rise of the slurry accompanying the rise of bubbles is reduced, so that the rate of rise of the slurry cannot be sufficiently obtained. Therefore, the catalyst particles may be unevenly distributed in the lower part of the reactor or may be deposited on the perforated plate, resulting in a poor dispersion of the catalyst particles.

[0007] The present invention has been made in view of such problems, and in a bubble column type hydrocarbon synthesis reactor for performing a Fischer's Tropsch synthesis reaction, the back mixing of bubbles in the reactor is suppressed. At the same time, it aims to keep the dispersed state of the catalyst particles in good condition without disturbing the upward flow of the slurry.

Means for solving the problem

[0008] As a result of intensive investigations to solve the above problems, the present inventors have provided a member (for example, a baffle plate) that shields the side wall of the reactor and opens the central side. By dividing the internal space into multiple compartments in the height direction, it was found that the backflow of bubbles between adjacent compartments was suppressed, and that upward flow of bubbles and slurry could be secured at the center of the reactor. The present invention has been completed based on the findings.

[0009] That is, the bubble column type hydrocarbon synthesis reactor of the present invention includes a reactor main body containing a slurry in which solid catalyst particles are suspended in a liquid hydrocarbon; and a lower portion of the reactor main body. A synthesis gas supply unit that is provided and supplies a synthesis gas mainly composed of hydrogen and carbon monoxide to the slurry; and a baffle member that is provided in the reactor main body and prevents a downward flow of the slurry; Prepare.

[0010] In the bubble column type hydrocarbon synthesis reactor of the present invention, the baffle member may shield a part of a cross section of the reactor body.

[0011] In the bubble column type hydrocarbon synthesis reactor of the present invention, the baffle member shields a region near the side wall of the reactor main body in the reactor main body, and the center of the reaction vessel main body. And it is provided to open the area near the center!

In the bubble column type hydrocarbon synthesis reactor of the present invention, the baffle member may have a plurality of through holes.

[0013] In the bubble column type hydrocarbon synthesis reactor of the present invention, the size of the through-hole is such that the catalyst particles can pass through and the synthesis gas or the gaseous hydrocarbon produced by the reaction of the synthesis gas. It may be of a size capable of suppressing the passage of bubbles containing.

[0014] In the bubble column type hydrocarbon synthesis reactor of the present invention, the through hole may be 10 to 100 times the average particle diameter of the catalyst particles.

[0015] In the bubble column type hydrocarbon synthesis reactor of the present invention, at least a part of the through hole may be formed in a substantially tapered shape in which a cross-sectional area decreases toward the bottom.

[0016] In the bubble column type hydrocarbon synthesis reactor of the present invention, the baffle member may be inclined so that a center side of the reactor body is lower than a side wall side.

The invention's effect

[0017] According to the present invention, in the bubble column type hydrocarbon synthesis reactor for performing the Fischer-Tropsch synthesis reaction, back mixing of bubbles in the reactor can be suppressed and the upward flow of the slurry can be prevented. The dispersed state of the catalyst particles can be kept good. Therefore, according to the present invention, the reaction conversion rate of the synthesis gas as the raw material can be improved, and the reaction can be efficiently performed in the entire internal space of the reactor.

Brief Description of Drawings

FIG. 1 is a longitudinal sectional view showing the overall configuration of an FT reactor according to a first embodiment of the present invention. FIG. 2 is a perspective view showing a baffle plate provided in the FT reactor shown in FIG. 1.

FIG. 3 is a perspective view showing a modified example of the baffle plate provided in the FT reactor shown in FIG. 1.

4 is a cross-sectional view showing a through hole formed in the baffle plate shown in FIG. 2. FIG.

FIG. 5 is a cross-sectional view showing a modification of the through hole formed in the baffle plate shown in FIG.

FIG. 6 is a cross-sectional view showing a modified example of the through hole formed in the baffle plate shown in FIG.

FIG. 7 is a cross-sectional view showing a modification of the through hole formed in the baffle plate shown in FIG.

8 is a cross-sectional view showing a modification of the through hole formed in the baffle plate shown in FIG.

FIG. 9 is a sectional view showing a modification of the through hole formed in the baffle plate shown in FIG.

FIG. 10 is an explanatory view showing the flow of slurry and bubbles inside the FT reactor shown in FIG. 1.

FIG. 11 is an explanatory view showing the flow of slurry and bubbles in the vicinity of the baffle plate shown in FIG. 2.

FIG. 12 is an explanatory diagram showing the flow of slurry and bubbles in the vicinity of the baffle plate shown in FIG. 3.

FIG. 13 is an explanatory view showing the flow of slurry and bubbles in the vicinity of the through hole formed in the baffle plate shown in FIG. 2.

FIG. 14 is a longitudinal sectional view showing an overall configuration of an FT reactor according to a second embodiment of the present invention.

FIG. 15 is a longitudinal sectional view showing an overall configuration of an FT reactor according to a third embodiment of the present invention. FIG. 16 is a longitudinal sectional view showing the overall configuration of a conventional FT reactor. Explanation of symbols

[0019] 100, 200, 300 ··· Synthetic reactor, 110, 210, 310 ··· Reactor body, 120, 220, 320… Slurry, 122 ··· Liquid coal-hydrogen, 124 ··· Catalyst Particles, 130 ··· Bubbles, 140, 240, 340… Distributor (syngas supply section), 142, 242, 342 ··· Syngas injection port, 150, 250, 350 ··· Noff plate (Noff nore §material ), 152, 252, 352 ... Penetrating:? L, 152a, 1 52b, 152c, 152d ... Theno part, 153 ... Linear part

BEST MODE FOR CARRYING OUT THE INVENTION

[0020] Hereinafter, preferred embodiments of the present invention will be described in detail with reference to the accompanying drawings. In the present specification and drawings, constituent elements having substantially the same functional configuration are denoted by the same reference numerals, and redundant description is omitted.

[0021] (Configuration of conventional bubble column reactor)

First, the configuration of the conventional bubble column reactor 1 will be described with reference to FIG. FIG. 16 is a vertical sectional view showing the overall configuration of the conventional bubble column reactor 1. In the following description, as an example of a bubble column reactor, a slurry bed type reactor in which solid catalyst particles are dispersed in a liquid will be described as an example, but a conventional bubble column reactor is used. 1 is not limited to such a slurry bed type reactor, but may be a bubble column reactor that generates gas by reaction, or a bubble column reactor that contains a gas component that does not participate in the reaction in the raw material gas. Good. For example, a bubble column reactor in which a liquid not containing a solid catalyst is accommodated may be used.

As shown in FIG. 16, the conventional bubble column reactor 1 mainly includes a reactor main body 10, a distributor 40 as an example of a raw material gas supply unit, and a perforated plate 50.

[0023] The reactor main body 10 is a substantially cylindrical metal container in which a slurry 20 in which solid catalyst particles 24 are suspended in a liquid (for example, liquid hydrocarbon) 22 is accommodated. Is done. A slurry inlet 11 for introducing the slurry 20 into the reactor main body 10 is provided at the bottom of the reactor main body 10. A slurry discharge port 12 for discharging the slurry 20 is provided on the side wall of the reactor body 10. A gas discharge port 14 is provided at the top of the reactor body 10 to discharge gas generated by the reaction and unreacted raw material gas. ing. The positions where the slurry inlet 11, the slurry outlet 12 and the gas outlet 14 are provided are not limited to the positions described above.

[0024] In the reactor main body 10 configured as described above, the liquid 22 is discharged from the slurry discharge port 12 together with the catalyst particles 24, and after separating the catalyst particles 24, a part of the liquid 22 is discharged. Outside (outside of reactor body 10), the remainder is separated into catalyst inlet 24 together with separated catalyst particles 24

11 is returned to the reactor body 10.

[0025] Here, the flow rate of the liquid 22 returned from the slurry inlet 11 into the reactor main body 10 varies depending on each reaction system.

[0026] Further, in a reaction system in which the liquid 22 and catalyst particles 24 generated by the reaction are drawn out of the reactor body 10 using a filter or the like, the slurry is returned from the slurry inlet 11 into the reactor body 10. In some cases, the flow rate of the liquid 22 is zero.

The distributor 40 is disposed in the lower part of the reactor main body 10 and supplies the raw material gas into the slurry 20. In the upper part of the distributor 40, a plurality of raw material gas injection ports 42 are provided. The number and position of the raw material gas injection ports 42 are not particularly limited.

[0028] The raw material gas supplied through the distributor 40 as an external force is injected with the force of the raw material gas injection port 42 directed upward, for example (in the direction indicated by the arrow in the figure). The raw material gas blown from the distributor 40 in this way becomes bubbles 30, which are liquid when flowing in the slurry 20 from the bottom in the height direction (vertical direction) of the reactor body 10 upward. A predetermined reaction occurs when the raw material gas component dissolved in 22 comes into contact with the catalyst particles 24.

[0029] Further, as described above, the raw material gas is also blown into the bottom force of the reactor main body 10, and the blown raw material gas becomes bubbles 30 and rises in the reactor main body 10, whereby the inner portion of the reactor main body 10 is increased. In FIG. 2, the upward flow K of the slurry 20 is mainly generated in the central portion (near the central axis of the reactor main body 10), and the downward flow is mainly generated in the vicinity of the side wall of the reactor main body 10 (near the circumferential portion). A flow (general circulation) that circulates inside the reactor main body 10 occurs. However, the arrows K and J in FIG. 16 indicate the direction of the flow of the slurry 20 mainly generated in the reactor main body 10, and this flow changes with time and is always constant. It does not flow at a constant speed in a certain direction in a certain place.

[0030] When the slurry 20 inside the reactor main body 10 is agitated as a whole by such general circulation, the bubbles 30 having a low concentration of the raw material gas move to the lower part of the reactor main body 10 by back mixing. The trend is strengthened. As a result, there is a possibility that the reaction rate inside the reactor main body 10 is reduced as a whole, and the reaction conversion rate of the raw material gas is lowered.

[0031] In order to solve such a problem, in the conventional bubble column reactor 1, as a barrier member that partially blocks the flow in the reactor main body 10 in the reactor main body 10, for example, A multi-hole plate 50 is provided. The perforated plate 50 is a substantially disk-shaped member provided so as to divide the internal space of the reactor main body 10 into a plurality of portions in the height direction (vertical direction), and bubbles 30 with a low concentration of the raw material gas react. Suppresses the flow to the bottom of the vessel body 10. The perforated plate 50 is provided with a plurality of through holes 52, and the bubbles 30 and the slurry 20 can pass through the through holes 52.

Further, the slurry 20 (or the liquid 22 not containing the catalyst particles 24) is reacted in such a manner that the slurry 20 (or the liquid 22 not containing the catalyst particles 24) always flows with the lower force of the reactor main body 10 directed upward. Take out outside of vessel body 10 and circulate. Thus, the bubbles 30 are prevented from flowing from the top to the bottom through the barrier member such as the multi-hole plate 50.

[0032] Thus, by providing a barrier member such as the perforated plate 50, the flow of the slurry 20 in the reactor main body 10 is pushed out from the bottom upward in the reactor main body 10 ("plug flow" It is called a state where there is no backflow of fluid). Thereby, overall mixing (general circulation) in the reactor main body 10 can be suppressed.

[0033] However, in the bubble column type slurry bed type FT reaction system, the flow rate of the slurry 20 may be extremely small relative to the volume of the reactor body 10, and in this case, the net rate of increase of the slurry 20 is Near zero. Therefore, when the perforated plate 50 is installed in the same manner as the conventional bubble column reactor 1, the rise of the bubble 30 is hindered by the resistance of the perforated plate 50 when the bubbles 30 and the slurry 20 pass through the perforated plate 50. As the bubble 30 rises, the speed of the upward flow K of the slurry 20 is reduced, and the speed of the upward flow K of the slurry 20 cannot be sufficiently obtained. Therefore, as shown in FIG. 16, the catalyst particles 24 may be unevenly distributed in the lower part of the reactor main body 10 or may be deposited on the porous plate 50, so that the dispersed state of the catalyst particles 24 may deteriorate. This As described above, when the dispersed state of the catalyst particles 24 is poor and the concentration of the catalyst particles 24 is small, the reaction rate is lowered, and the reaction efficiency is lowered in the entire region of the reactor body 10.

[0034] Therefore, in the FT reactor according to the present invention, instead of the perforated plate 50, a member that shields the side wall side of the reactor main body 10 and opens the center side is provided.

Hereinafter, the FT reactor according to the present invention will be described in detail while showing specific embodiments.

[0035] (First embodiment)

First, based on FIG. 1, a bubble column type slurry bed FT synthesis reactor 100 (hereinafter simply referred to as “FT reactor 100”) as an example of the bubble column type hydrocarbon synthesis reactor according to the first embodiment of the present invention. ") Will be described. FIG. 1 is a vertical sectional view showing the overall configuration of the FT reactor 100 according to this embodiment.

As shown in FIG. 1, an FT reactor 100 according to this embodiment includes a reactor main body 110, a distributor 140 as an example of a synthesis gas supply unit according to the present invention, and a baffle according to the present invention. A baffle plate 150 as an example of a member is mainly provided.

[0037] The reactor main body 110 is a substantially cylindrical metal container having a diameter of about 1 to 20 m, preferably about 2 to 10 m. The height of the reactor body 10 is about 10 to 50 m, preferably about 15 to 45 m. Inside the reaction body 10, there is a solid catalyst in a liquid hydrocarbon (product of FT reaction) 122. A slurry 120 in which particles 124 are suspended is contained. A slurry inlet 111 for introducing the slurry 120 into the reactor main body 110 is provided at the bottom of the reactor main body 110. A slurry discharge port 112 for discharging the slurry 120 is provided on the side wall of the reactor main body 110. A gas discharge port 114 for discharging light hydrocarbon gas generated by FT reaction and unreacted synthesis gas is provided at the top of the reactor main body 110. The positions where the slurry inlet 111, the slurry outlet 112 and the gas outlet 114 are provided are not limited to the positions described above.

[0038] Distributor 140 is an example of a reaction gas supply unit according to the present embodiment, and is disposed in the lower part of reactor main body 110, and a synthesis gas mainly composed of hydrogen and carbon monoxide is slurry 120. Supply inside. A plurality of synthesis gas injection ports 142 are provided in the upper portion of the distributor 140. The number and position of the syngas injection ports 142 are as follows. There is no particular limitation.

[0039] The synthesis gas supplied from the external force through the distributor 140 is injected from the synthesis gas injection port 142, for example, in an upward direction (direction indicated by an arrow in the figure). The synthesis gas blown from the distributor 140 in this way becomes bubbles 130, and the liquid flows when the downward force in the height direction (vertical direction) of the reactor main body 110 flows upward in the slurry 120. When the dissolved synthesis gas component is dissolved in the hydrocarbon 122 and the catalyst particles 124 come into contact with each other, a liquid hydrocarbon synthesis reaction (FT synthesis reaction) is performed.

[0040] The baffle plate 150 is provided inside the reactor main body 110 so as to block a region near the side wall of the reactor main body 110 and open a center and a region near the center of the reactor main body 110. The baffle plate 150 divides the internal space of the reactor main body 110 into a plurality of sections in the height direction. In the present embodiment, two baffle plates 150 are provided inside the reactor main body 110. Accordingly, the internal space force S of the reactor main body 110 is divided into three sections.

[0041] The force described later in detail. As described above, the baffle plate 150 force is provided on the side wall of the reactor main body 110 so as to block the region near the light hydrocarbons generated by the FT reaction. The bubble 130 containing a large amount of gas circulates in the compartment where it is present, making it difficult to flow into other compartments. Thereby, it is possible to suppress backflow (backmixing) between the sections. In addition, the kaffle plate 150 is provided so as to open the center of the reactor main body 110 and the area near the center, thereby preventing the upward flow of the slurry 120 that is going to rise in the center of the reactor main body 110. There is nothing.

Here, the number of baffle plates 150 or the length L in the vertical direction of each section can be appropriately determined according to the height of the reactor main body 110. Specifically, the length L in the height direction of each section of the reactor main body 110 divided by the kaffle plate 150 is preferably about 0.5 to 10 times the inner diameter D of the reactor main body 110. It is more preferably about 1 to 5 times.

[0043] The ratio of the length L in the height direction of each section of the reactor main body 110 to the inner diameter D of the reactor main body 110, that is, if LZD is too small outside the above range, sufficient circulation in each section The flow does not develop and backmixing is overly suppressed. For this reason, the dispersion state of the catalyst particles 124 is deteriorated, or the residence time of the bubbles 130 is shortened by blowing the bubbles 130. There is a possibility that the reaction conversion rate of the synthesis gas, which is a material, may be reduced. On the other hand, if the LZD is too large out of the above range, the effect of dividing by the kaffle plate 150, that is, the effect of suppressing the back mixing cannot be sufficiently exhibited.

Hereinafter, the configuration of the baffle plate 150 according to the present embodiment will be described in detail based on FIG. 2 to FIG. 2 is a perspective view showing the configuration of the baffle plate 150 according to the present embodiment, and FIG. 3 is a perspective view showing the configuration of the baffle plate 150 according to a modification of the present embodiment. 4 to 9 are cross-sectional views showing examples of the configuration of the through hole 152 according to this embodiment.

[0045] As shown in FIG. 2, the kaffle plate 150 is a substantially disk-shaped member having an opening 150a formed at the center, and the baffle plate 150 blocks the difference between the side walls of the reactor main body 110. Thus, the center of the reactor main body 110 and the area near the center are opened. The baffle member of the present invention is not limited to the baffle plate 150 according to the present embodiment, and is not limited to the one in which the opening 150a is formed at the center of the substantially disk-shaped member. It is sufficient that an open space is provided in the vicinity. For example, as shown in FIG. 3, a pair of approximately half-moon shaped plates provided on the side wall of the reactor main body 10 is a pair of a noble plate 150, (in other words, a substantially disk-shaped baffle plate is divided into three parts. In other words, the opening 150'a may be formed by removing the central divided piece).

[0046] Here, the area Ac of the open portion of the baffle plate 150 (or 150 '(hereinafter omitted)) (opening 150a in the example of FIG. 2, open 150'a in the example of FIG. 3) Ac Is preferably about 35 to 65%, preferably about 10 to 90% of the area At of the horizontal cross section in the reactor body 10.

[0047] The ratio of the area of the open part of the baffle plate 150 to the area At of the horizontal cross section 10 inside the reactor main body Ac, that is, if AcZAt is too small outside the above range, the bubbles 130 and the slurry 120 rise. Since the flow is hindered, there is a possibility that a sufficient dispersion effect of the catalyst particles 124 cannot be obtained. On the other hand, if AcZAt is too large out of the above range, the effect of dividing by the kaffle plate 150, that is, the effect of suppressing backmixing will not be sufficiently exhibited. [0048] Further, the notch plate 150 is provided with a plurality of through holes 152 (or 152, hereinafter omitted). The through-hole 152 is formed in an appropriate size so as to allow passage of the liquid hydrocarbon 122 and the catalyst particles 124 and suppress passage of the bubbles 130 containing light hydrocarbons generated by the FT reaction. By setting the size of the through hole 152 as described above, it is possible to prevent the catalyst particles 124 from closing the through hole 152. Further, it is possible to prevent the bubbles 130 from passing through the through holes 152 of the baffle plate 150 and the rising bubbles 130 from passing from the bottom to the top of the baffle plate 150 as the slurry 120 descends. Can be.

More specifically, when the through hole 152 has a substantially circular cross section, the diameter of the through hole 152 is preferably 10 to 100 times the average particle diameter of the catalyst particles 124 and is preferably 30 to 50 times. Is more preferable. Further, the catalyst particles 124 according to this embodiment preferably have an average particle diameter of 10 to 1000 m, more preferably 20 to 500 m. More preferably, it is about 100 m. For example, when a catalyst particle 124 having an average particle diameter of about 100 m is used, the diameter of the through hole 152 is preferably about 1 to 10 mm, more preferably about 3 to 5 mm. The diameter of the through-hole 152 is set to be 10 times or more the average particle diameter of the catalyst particles 124 because the catalyst particles 124 to be deposited on the baffle plate 150 do not block the through-hole 152 and the baffle plate This is because it is necessary to make the diameter sufficiently larger than the diameter of the catalyst particles so that 150 can pass from the top to the bottom. In addition, the diameter of the through-hole 152 is set to 100 times or less of the average particle diameter of the catalyst particles 124. If the diameter of the through-hole 152 is too large, the flow rate of the slurry 120 passing through the through-hole 152 increases, and the bubbles 130 This is because the possibility of passing through the through hole 152 along with the slurry 120 increases. Power! This is because the possibility that the rising bubbles 130 pass through the through holes 152 is increased. Note that the diameter of the through hole 152 is a representative of the narrowest portion of the through hole 152 when the diameter of the through hole 152 is not constant, for example, when a tapered portion is provided in the through hole 152 as described later. This refers to the length (for example, the diameter if the cross section of the through hole 152 is circular, the length of one side if the cross section is square).

[0050] Further, the opening ratio ε of the through hole 152, that is, the ratio of the total opening area Ah of the through hole 152 to the area Αρ of the baffle plate 150 (excluding the area of the central opening 150a) (ε = AhZAp) 1 to 50% is preferred, and 5 to 25% is more preferred. Opening ratio ε is 1% or less The reason for the above (preferably 5% or more) is that it is necessary to obtain a sufficient amount of downflow of the slurry 120 passing through the kaffle plate 150. However, if the diameter of the through hole 152 is too large in order to increase the opening ratio ε, the possibility that the bubble 130 will pass through the through hole 152 increases as described above, which is not preferable. In addition, if the number of through holes 152 is increased in order to increase the hole area ratio ε, a sufficiently large area of the upper surface of the baffle plate 150 cannot be secured when a tapered portion described later is provided. It is not preferable. From such a viewpoint, the open area ratio ε needs to be 50% or less (preferably 25% or less). Note that the opening area of the through hole 152 used for the calculation of the open area ratio ε is, for example, when the diameter of the through hole 152 is not constant, for example, when a tapered portion or the like is provided in the through hole 152 as described later. This refers to the cross-sectional area of the narrowest portion of the through hole 152.

[0051] The through hole 152 may be formed, for example, such that the cross-sectional area (opening area) of the through hole 152 is constant as shown in FIG. Also, as shown in FIG. 5, at least a part of the through-hole 152, for example, the upper surface side of the baffle plate 150, is provided with a tapered portion 152a whose cross-sectional area becomes smaller as it is directed downward! / /.

[0052] The shape of the tapered portion is not limited to the case shown in FIG. 5, and any shape can be adopted as long as the cross-sectional area force decreases as it goes downward. For example, as shown in FIG. 6 to FIG. 8, a shape (FIG. 6) in which a straight section 153 (vertical length R) having a constant cross-sectional area is provided above the tapered section 152b, the vertical section of the tapered section 152c. A shape having a curved cross section (FIG. 7), a stepped shape (FIG. 8) in which the tapered portion 152d has a plurality of step forces, and the like can be employed.

[0053] Thus, by providing a teno rod (152a, 152b, 152c, 152d, etc.) on at least one of the through-holes 152, the area of the flat portion of the upper surface of the noble plate 150 is minimized, and the catalyst Accumulation of particles 124 on the upper surface of the baffle plate 150 can be minimized. In addition, by providing a tapered portion and increasing the cross-sectional area of the through hole 152 on the upper surface side of the baffle plate 150, the flow velocity of the slurry 120 passing through the through hole 152 on the upper surface of the baffle plate 150 can be decreased. Thereby, the effect of suppressing the bubbles 130 from passing through the through-holes 152 accompanying the slurry 120 can be further improved. [0054] The shape of the (horizontal) cross section of the through hole 152 can be substantially circular as shown in FIGS. 2, 3 and the like, but is not limited to the substantially circular shape, and other shapes (for example, Or a substantially square shape).

[0055] In addition, the cross-sectional area A (hereinafter referred to as "lower surface cross section") of the through hole 152 on the lower surface side of the baffle plate 150.

0

Cross-sectional area A (hereinafter referred to as “top surface cross section”)

0 1

The ratio _α (= Α ΖΑ) of product A ”and u) can be 1≤« ≤ 100.

1 1 0

[0056] The reason for this is that in order to enhance the separation effect of the bubbles 130 in the tapered portion 152a and the like (the effect of suppressing the bubbles 130 from passing through the through-holes 152 accompanying the slurry 120), the larger α Is preferred. This is because the flow velocity of the slurry 120 passing through the through hole 152 can be further reduced by increasing α.

[0057] Specifically, the numerical range of a is determined from the following points. That is, the bottom cross-sectional area A

When 0 is equal to the cross-sectional area A (when no taper is provided as shown in Fig. 4), h = 1, so α must be 1 or more. Note that α is 1, that is, A> A

0 1 Although it is possible, bubbles may pass from the bottom to the top of the noble plate 150 due to a decrease in the flow velocity on the lower surface side of the slurry 120 passing through the through-hole 152. 1 is preferable. On the other hand, the upper limit of α is determined by the lower limit of the aperture ratio ε. When ε = 1% (lower limit), the maximum value of a is a = 100.

[0058] When a taper portion 152a having an inclined surface with a straight vertical cross section as shown in FIG. 9 is applied as the tapered portion, the angle (opening angle) Θ of this inclined surface is a through hole. It is preferably about 30 to 60 ° with respect to the central axis of 152. The opening angle 0 needs to be small (slightly inclined) so that the catalyst particles 124 can smoothly flow through the through holes 152. However, if the opening angle Θ is too small, it is necessary to increase the thickness of the baffle plate 150 in order to secure the necessary top surface cross sectional area A. On the other hand, if the opening angle Θ is too large, it is substantially the same as when the tapered portion is not provided. From such a viewpoint, it is preferable to set the opening angle 0 to about 30 to 60 °.

[0059] The arrangement of the through holes 152 is not particularly limited, but it is preferable that the through holes 152 are arranged almost uniformly over the entire noble plate 150. In addition, the area of the flat part of the noble plate 150 is reduced. In order to reduce the length, the through holes 152 are preferably arranged in a triangular pattern. Thus, by arranging the through holes 152 in a triangular arrangement, it is possible to suppress the deposition of the catalyst particles 124 on the baffle plate 150.

[0060] The configuration of the FT reactor 100 according to the present embodiment has been described in detail above based on Figs. Next, the function and operation of the FT reactor 100 will be described based on FIGS. 10 to 13 while showing the flow of the slurry 120 and the bubbles 130 in the reactor main body 110. FIG. 10 is an explanatory diagram showing the flow of the slurry 120 and the bubbles 130 inside the reactor main body 110 according to the present embodiment. FIG. 11 and FIG. 12 are explanatory diagrams showing the flow of the slurry 120 and the bubbles 130 in the vicinity of the baffle plate 150 (or 150,) according to the present embodiment. FIG. 13 is an explanatory diagram showing the flow of the slurry 120 and the bubbles 130 in the vicinity of the through hole 152 according to the present embodiment. However, the arrows in FIGS. 10 to 13 indicate the direction of the flow that mainly occurs in the reactor main body 110, and this flow changes with time and always shows a certain point. It does not flow at a constant speed in a certain direction.

First, the flow of the slurry 120 and the bubbles 130 near the entire reactor main body 110 and the baffle plate 150 (or 150 ′) will be described with reference to FIGS. 10 to 12. As shown in FIG. 10, the synthesis gas blown from the bottom of the reactor main body 110 through the synthesis gas injection port 142 of the distributor 140 rises into the reactor main body 110 as bubbles 130. As a result, in the reactor main body 110, an upward flow A of the slurry 120 is generated mainly in the central portion (the center and the vicinity of the center of the reactor main body 110), and a downward flow is mainly generated in the vicinity of the side wall of the reactor main body 110. Arise.

[0062] In the present embodiment, since the baffle plate 150 is provided, a flow in which the bubbles 130 circulate through the entire reactor main body 110 together with the slurry 120 (general circulation) as in the prior art. ) Will not occur. That is, the kaffle plate 150 is provided close to the side wall of the reactor main body 110 so as to block the region. Therefore, the bubbles 130 containing a large amount of light hydrocarbons generated by the FT reaction are formed as shown in FIGS. As shown by arrow B in FIG. 2, the flow is hindered on the upper surface side and the lower surface side of the baffle plate 150 and circulates only in the compartments divided by the baffle plate 150. Backflow (backmixing) between strokes can be suppressed. Accordingly, since the bubbles 130 containing a large amount of light hydrocarbons can be prevented from circulating throughout the reactor main body 110, the reaction conversion rate of the synthesis gas can be increased.

On the other hand, in the present embodiment, the baffle plate 150 is provided so that the center of the reactor main body 110 and the area near the center are opened, so that unlike the conventional case, the baffle plate 150 is different from the conventional one. As shown in FIG. 4, the upward flow A of the slurry 120 and the bubbles 130 in the central portion of the reactor main body 110 is not hindered. Therefore, the catalyst particles 124 can be prevented from being unevenly distributed in the lower portion of the reactor main body 110, and the dispersed state of the catalyst particles 124 can be kept good.

[0064] Further, in the present embodiment, since the baffle plate 150 is provided with a plurality of through holes 152, the slurry containing the liquid hydrocarbon 122 and the catalyst particles 124 is as shown by an arrow C in FIG. Then, it passes through the through-hole 152 and flows downward toward the reactor main body 110. Therefore, the catalyst particles 124 to be deposited on the baffle plate 150 are allowed to flow down from the top of the baffle plate 150 through the through holes 152, thereby preventing the catalyst particles 124 from being deposited on the baffle plate 150. Further, by providing a through-hole 152 and securing a downward flow C of the slurry 120 passing through the baffle plate 150, the upward flow A of the slurry 120 and the bubbles 130 at the opening ridge 150a of the notch plate 150 is further promoted. Can do. As described above, the catalyst particles 124 are prevented from accumulating on the noble plate 150, and the upward flow A of the slurry 120 passing through the baffle plate 150 is promoted, thereby further maintaining the dispersed state of the catalyst particles 124. Can

It should be noted that what has been described above is the same when the baffle plate 150 ′ according to the modification of the present embodiment as shown in FIG. 12 is used.

Next, the function and action of the through hole 152 will be described in more detail based on FIG. As shown in FIG. 13, the bubble 130 containing a large amount of light hydrocarbon gas generated by the FT reaction is blocked by the baffle plate 150 as shown by an arrow B, passes through the baffle plate 150, and adjoins. It is restrained to move between matching sections. In addition, the catalyst particles 124 are accompanied by the downward flow of the slurry 120 as shown by the arrow C1. As shown by the arrow C2, it passes through the through hole 152 and flows downward in the reactor main body 110.

[0067] Here, comparing the velocity of the flow B of the bubble 130 and the velocity of the flow C1 of the catalyst particle 124 (and liquid hydrocarbon 122), the velocity of the flow B is much higher than the velocity of the flow C1. Because of the high speed, bubbles 130 having a specific gravity smaller than that of the slurry 120 hardly pass through the through-hole 152 along with the flow C 1 of the slurry 120 or the like. Furthermore, if the through-hole 152 is provided with the tapered portion 152a, the speed of the flow C1 of the slurry 120 passing through the upper surface of the through-hole 152 can be further reduced, so that the bubbles 130 penetrate along with the slurry 120. The effect of suppressing passage through the hole 152 can be further improved.

[0068] As described above, the bubbles 130 can be circulated in the respective sections, and the slurry 120 can be circulated through the reactor main body 110 through the baffle plate 150.

[0069] (Second Embodiment)

Next, based on FIG. 14, a bubble column type slurry bed FT synthesis reactor 200 (hereinafter simply referred to as “FT reactor 200”) as an example of the bubble column type hydrocarbon synthesis reactor according to the second embodiment of the present invention. ") Will be described. FIG. 14 is a vertical sectional view showing the overall configuration of the FT reactor 200 according to this embodiment.

As shown in FIG. 14, the FT reactor 200 according to the present embodiment includes a reactor main body 210, a distributor 240 as an example of the synthesis gas supply unit according to the present embodiment, and the present embodiment. A baffle plate 250 as an example of a baffle member.

[0071] The reactor main body 210 contains the slurry 220. A slurry inlet 211 for introducing the slurry 220 into the reactor main body 210 is provided at the bottom of the reactor main body 210. A slurry discharge port 212 for discharging the slurry 220 is provided on the side wall of the reactor main body 210. A gas outlet 214 is provided at the top of the reactor body 210 to discharge light hydrocarbon gas generated by FT reaction and unreacted synthesis gas.

[0072] Distributor 240 is an example of a reaction gas supply unit according to the present embodiment, and is disposed at the lower part of reactor main body 210, and a synthesis gas mainly composed of hydrogen and carbon monoxide is slurry 220. Supply inside. The top of this distributor 240 has multiple syngas injections A mouth 242 is provided.

[0073] The kaffle plate 250 is provided inside the reactor main body 210 so as to block a region near the side wall of the reactor main body 210 and open a center and a region near the center of the reactor main body 210. By the kaffle plate 250, the interior of the reactor main body 210 is divided into a plurality of sections in the height direction. In addition, a plurality of through holes 252 are provided in the kaffle plate 250.

[0074] In the FT reactor 200 according to the present embodiment, the upward flow D of the synthesis gas and the slurry 220 supplied from the distributor 240 in the reactor main body 10 is reduced due to having a profitable configuration. It can be lifted through an opening provided in the center of the baffle plate 250. In addition, bubbles containing a large amount of light hydrocarbons generated by the FT reaction are difficult to flow into other compartments due to the baffle plate 250, and a circulating flow E is produced in the compartment where it exists. Further, the slurry 220 passes through the through-hole 252 and generates a downward flow F. However, the arrows in FIG. 14 indicate the direction of the flow that mainly occurs in the reactor main body 210, and this flow changes with time. It does not flow at a constant speed.

[0075] Here, in the FT reactor 200 according to the present embodiment, unlike the case of the first embodiment described above, the notch plate 250 has a central portion close to the side wall of the reactor main body 110. It is installed so as to be lower than the edge, that is, inclined downward in the center of the reactor body 110. In this manner, in addition to providing the through hole 252, the effect of preventing the catalyst particles from being deposited on the noble plate 250 can be further improved by inclining the noble plate 250 downward.

[0076] The configuration and operational effects of the FT reactor 200 other than those described above are the same as those of the FT reactor 100 according to the first embodiment described above, and thus detailed description thereof is omitted.

[0077] (Third embodiment)

Next, based on FIG. 15, a bubble column type slurry bed FT synthesis reactor 300 (hereinafter simply referred to as “FT reactor 300”) as an example of a bubble column type hydrocarbon synthesis reactor according to the third embodiment of the present invention. ") Will be described. FIG. 15 is a vertical sectional view showing the overall configuration of the FT reactor 300 according to this embodiment. As shown in FIG. 15, the FT reactor 300 according to the present embodiment includes a reactor main body 310, a distributor 340 as an example of the synthesis gas supply unit according to the present embodiment, and the present embodiment. And a baffle plate 350 as an example of a baffle member.

[0079] The reactor main body 310 contains the slurry 320. A slurry inlet 311 for introducing the slurry 320 into the reactor main body 310 is provided at the bottom of the reactor main body 310. A slurry discharge port 312 for discharging the slurry 320 is provided on the side wall of the reactor main body 310. A gas outlet 314 is provided at the top of the reactor main body 310 for discharging light hydrocarbon gas generated by the FT reaction and unreacted synthesis gas.

Distributor 340 is an example of a reaction gas supply unit according to the present embodiment, and is disposed in the lower part of reactor main body 310 to supply synthesis gas mainly composed of hydrogen and carbon monoxide in slurry 320. To supply. A plurality of synthesis gas injection ports 342 are provided at the upper portion of the distributor 340.

[0081] The baffle plate 350 is provided inside the reactor main body 310 so as to shield a part of the cross section of the reactor main body 310. The baffle plate 350 divides the interior of the reactor main body 310 into a plurality of sections in the height direction. In addition, a plurality of through holes 352 are provided in the kaffle plate 350. Specifically, in the FT reactor 300 according to the present embodiment, unlike the cases of the first and second embodiments described above, the kaffle plates 350 are staggered on both sides inside the reactor main body 310. The baffle plate 350 opens one side of the cross section inside the reactor main body 310 and shields the other side at the boundary of each section.

[0082] In the FT reactor 300 according to the present embodiment, the upward flow G of the synthesis gas and the slurry 320 supplied from the distributor 340 inside the reactor main body 310 is obtained by having a profitable configuration. The opening that is not shielded by the baffle plate 350 can be raised. In addition, bubbles containing a large amount of light hydrocarbons generated by the FT reaction are difficult to flow into the other compartments due to the knot plate 350, and a circulating flow H is generated in the compartment where it exists. Furthermore, the slurry 320 passes through the through hole 252 and generates a downward flow I. However, the arrows in Fig. 15 indicate the direction of the flow that mainly occurs in the reactor main body 310. This flow changes with time and does not always flow at a constant speed in a certain direction in a certain direction.

[0083] In this way, by installing the kaffle plates 350 in a staggered manner, the upward flow G is prevented from being biased to one side in the reactor main body 310, and the slurry 320 is retained on the other side. It is possible to prevent the mixed state of the slurry 320 from being deteriorated.

[0084] The configuration and operational effects of the FT reactor 300 other than those described above are the same as those of the FT reactor 100 according to the first embodiment described above, and thus detailed description thereof is omitted.

As described above, the force described for the preferred embodiment of the present invention with reference to the accompanying drawings. Needless to say, the present invention is not limited to the powerful example. It will be apparent to those skilled in the art that various changes and modifications can be made within the scope of the claims, and these are naturally within the technical scope of the present invention. Understood.

[0086] For example, in the embodiment described above, the force baffle member described in the case where the baffle member is a plate-like baffle plate 150, 250, 350 is not limited to a plate shape, and the side wall side of the reactor main body is shielded. However, any shape can be used as long as the central side is open.

Industrial applicability

[0087] The present invention relates to a reactor main body that contains a slurry in which solid catalyst particles are suspended in liquid hydrocarbon; and is disposed at a lower portion of the reactor main body, and contains hydrogen and carbon monoxide as main components. The present invention relates to a bubble column type hydrocarbon synthesis reactor comprising: a synthesis gas supply unit that supplies the synthesis gas to the slurry; and a baffle member that is provided in the reactor main body and prevents a downward flow of the slurry.

According to the bubble column type hydrocarbon synthesis reactor of the present invention, the reaction conversion rate of the synthesis gas as a raw material can be improved and the reaction can be efficiently carried out in the entire internal space of the reactor. .

Claims

The scope of the claims

[1] A reactor main body containing a slurry in which solid catalyst particles are suspended in liquid hydrocarbon, and a lower part of the reactor main body, and a synthesis gas mainly containing hydrogen and carbon monoxide A synthesis gas supply for supplying the slurry;

A bubbling column type hydrocarbon synthesis reactor comprising: a baffle member provided in the reactor main body and blocking the downward flow of the slurry.

2. The bubble column type hydrocarbon synthesis reactor according to claim 1, wherein the baffle member shields a part of a cross section of the reactor main body.

[3] The baffle member is provided in the reactor main body so as to shield a region near the side wall of the reactor main body and to open a center and a region near the center of the reaction vessel main body! 2. The bubble column type hydrocarbon synthesis reactor according to claim 1.

[4] The bubble column hydrocarbon synthesis reactor according to claim 1, wherein the baffle member has a plurality of through-holes!

[5] The size of the through hole is such that the catalyst particles can pass therethrough and the passage of bubbles containing gaseous hydrocarbons generated by the reaction of the synthesis gas or the synthesis gas can be suppressed. The bubble column type hydrocarbon synthesis reactor according to claim 4.

6. The bubble column hydrocarbon synthesis reactor according to claim 4, wherein the through-hole is 10 to 100 times the average particle diameter of the catalyst particles.

7. The bubble column hydrocarbon synthesis reactor according to claim 4, wherein at least a part of the through-hole is formed in a substantially taper shape whose cross-sectional area decreases downward.

8. The bubble column hydrocarbon synthesis reactor according to claim 1, wherein the baffle member is inclined so that a center side of the reactor main body is lower than a side wall side.