JPS63223001A - Horizontal reactor - Google Patents

Abstract

PURPOSE:To enable independent control of vapor-phase composition of zone groups and carry out continuous operation for a long period, by dividing the interior of a reactor for carrying out vapor phase-solid phase reaction into three or more zones and mounting plate paddles on a stirrer under specific condition. CONSTITUTION:A horizontal reactor, equipped with a cylindrical vessel 1 having the horizontal central axis, a stirrer 7 having a rotating shaft 5 arranged in agreement with the central axis, a feed port 10 for an object for stirring and a taking outlet 11 for the product placed at both ends of the vessel 1 and two or more partition walls 2, 2', and 2'', placed perpendicular to the rotating shaft 5 and having an opening part 6 at the bottom dividing the interior of the vessel 1 into three or more zones and capable of carrying out vapor phase-solid phase reaction. In the above-mentioned reactor, the stirrer 7 is constituted of plural sets of one or more plate paddles 4 mounted in the direction of the rotating shaft and particularly two sets of the paddles forming a pair with the partition walls placed therebetween satisfy formulas I-VI. The adjacent pair of the paddle sets satisfy formula VII and I1, I2, S1, S2 and W2 are mutually equal at the same time (I1 is the clearance between the inner wall and the paddle tips on the feed side; I2 is the clearance between the inner wall and the paddle tips on the taking out side).

Description

[Detailed Description of the Invention] [Industrial Application Field] The present invention relates to a horizontal reactor for carrying out a gas phase-solid phase reaction, and in particular, the invention relates to a horizontal reactor for carrying out a gas phase-solid phase reaction, and in particular, the inside of the reaction vessel is divided into three or more zones and at least two zone groups. The present invention relates to a horizontal reactor in which the composition of the gas phase can be independently controlled and in which backflow is prevented during the transfer of particles between each zone.

[Conventional technology]

A horizontal reactor equipped with a stirrer having a horizontal rotating shaft in a cylindrical container is known as a reactor for gas phase polymerization of polyolefins and the like. These horizontal reactors can be used to completely mix powders such as polymer particles and catalyst particles, improve heat removal efficiency, and improve the residence time distribution (RT) of powders in the container.
In order to narrow the width of D), that is, to make the residence time uniform (hereinafter referred to as RTD improvement), in addition to a stirring means with a large number of rectangular flat paddles attached to a horizontal rotating shaft, A reactor capable of continuous processing is known in which one or more fixed weirs are fixed to the inner wall of the container in a direction perpendicular to the axis of rotation. (Special Publication No. 59-21321, Special Patent Application No. 61-6
(Refer to 8771) When the opening of the fixed weir in such a reactor is located at the upper part, that is, on the gas phase side, the composition of the gas phase in the reactor will be the same for each zone. On the other hand, the average molecular weight of a polymer produced in a gas phase polymerization reaction of polyolefin or the like is influenced by the partial pressure of a molecular weight regulator in the raw material gas. Therefore, when polymerization is carried out using only gases having the same composition, it is possible to control the average molecule T of the resulting polymer, but it is not possible to control the molecular weight distribution curve to an arbitrary value. For this reason, a method has been proposed in which the interior of the reactor is divided into a plurality of zones using partition walls having openings in the particle layer, and the gas composition is controlled for each zone. (Japanese Patent Publication No. 59-21321) [Problems to be Solved by the Invention] However, the above method has the following problems. That is, since the flat paddle suitably used in a horizontal gas phase polymerization reactor generates thrust in both directions on the axis of rotation, the flat paddle located behind the partition wall having an opening in the particle layer allows the thrust to pass through the opening. Particles are moved in forward and reverse directions.

Therefore, there are particles that remain in the reactor for a long time, making it impossible to expect an improvement in RTD. Therefore, it has been difficult to control the produced polymer to have desired properties. Furthermore, it is difficult for powder and granular materials to transmit pressure horizontally, so even if there is a difference in the particle layer level before and after the partition wall, the amount of particles passing through the openings in the particle layer is unlikely to change accordingly.
The level of the particle layer in the zones before and after the partition wall was unstable, making it impossible to operate continuously in a steady state for a long period of time. The present invention was made to solve the above-mentioned problems, and it is possible to freely control the gas component partial pressure in two or more zone groups in the reactor, and it also improves RTD and allows long-term use. The purpose of the present invention is to provide a gas phase-solid phase horizontal reactor that can be operated continuously.

[Means for solving problems]

a cylindrical container having a horizontal central axis; a stirrer having a rotating shaft aligned with the horizontal central axis; and a supply port for a product to be stirred and a product disposed at each end of the cylindrical container. and two or more partition walls arranged perpendicularly to the rotation axis and having an opening at the bottom and dividing the inside of the cylindrical container into three or more zones, and the three or more zones are is connected to two or more independent gas circulation systems that circulate and supply gas, and a horizontal reaction in which a gas phase-solid phase reaction is carried out in a state where a particle layer existing in the cylindrical container fills the opening of the partition wall. In Sae, the stirrer includes a plurality of paddle sets each having one or more flat paddles attached to a predetermined position in the axial direction of the rotating shaft, and in particular, two sets of paddles facing each other across the partition wall constitute a pair. The paddle groups are as follows for each pair (+
) to (V+), and conditions (vii) to (viii) are satisfied for the relationship between the adjacent pairs.

(i) 10” ≦β≦45゜ (ii) D/100≦l 1≦D/20 (iii) 12
/11≧1 (+V)1≦$2/S1≦3 (v)α≧90゜(vi) 1 <W1n/W≦4 (1≦n≦N
) n+1 (vii) 1≦W /W1°〈1.2 (1≦n≦
N-1〉 (viii) between all adjacent pairs of paddle sets,
11, 1□, s1, s2, and W2 are equal to each other.

The meanings of the symbols in the above formula are as follows.

β: Advance angle of the rotational direction of the product extraction side paddle with respect to the stirring object supply side paddle D: Inner diameter of the cylindrical container 11: Clearance between the inner wall of the container and the tip of the stirring object supply side paddle 12: The inner wall of the container and the product Clearance between the paddle on the product extraction side and the tip of the paddle SL: 1R Clearance between the paddle on the supply side of the object to be stirred and the partition wall≦2: Clearance n between the paddle on the product extraction side and the partition wall.

Wl, ta Width W2 of the flat paddles on the stirring target material supply side of the paddle group pair that sandwich the n-th partition counting from the stirring target material supply port: Width W2 of the flat paddles on the product extraction port side of the paddle group pair that sandwich the partition wall Width N: Number of partition walls α: Advance angle in the rotational direction of the stirring object supply side paddle with respect to the product extraction side paddle The above symbols will be used hereinafter with the same meaning.

[For production]

The present invention will be described in detail with reference to the drawings.

FIGS. 2 to 4 are diagrams showing the positional relationship of the flat plate paddles of the partition wall and the position of the powder surface when the present invention is carried out, and are similar to FIG. 1 showing the cross section of the embodiment. Corresponds to the Δ-8 plane. The cylindrical container 1 is divided into four zones, 1st, 2nd, 3rd, and 4th, from the upstream side of the powder 3 by partition walls 2, 2', 2''. In the case shown in the figure, one paddle There are two flat paddles 4 in the set, which are fixed to the rotating shaft 5 at an interval of 180°.When the rotating shaft 5 rotates in the direction of the arrow, the position of the powder surface corresponds to the position of the flat paddles 4.4. However, since the slope always slopes downward to the left, if the opening 6 of the partition wall is placed at the lower right, the opening will always be buried in the powder. In this state, the amount of gas passing through the opening is small, so it is possible to maintain different gas partial pressure components in the upstream zone and the downstream zone.

When the flat paddle moves through the granular material, the granular material is removed from the rear in the direction of rotation of the flat paddle, creating a coarsely packed portion.

Conversely, the powder is pushed to the front and sides of the flat paddle, creating a densely packed area. Therefore, when one of the adjacent flat paddles is advancing in the rotational direction than the other, the powder flows behind the advancing flat paddle due to the pressure of the lagging flat paddle and moves in the axial direction. This effect does not occur when the lead angle α or β exceeds 90”.
The above effect occurs strongly in the range of ≦α≦45° or 10′″≦β≦45°.Therefore, as shown in the figure, the number of paddles in the paddle set before and after the partition wall is two, and the number of paddles on the downstream side is When the advance angle β is in the range of 10°≦β≦45°, the advance angle α of the upstream paddle becomes 135°≦α≦170°, and the particles receive thrust from the upstream side to the downstream side due to the rotation of the paddle. However, thrust in the opposite direction is hardly generated. Therefore, by appropriately determining the area of the opening, the required flow of particles in the downstream direction can be ensured, and the flow of particles in the opposite direction can be virtually eliminated. Yes. If the number of paddles in the paddle set is 4 or more, the advancement angle α of the upstream paddle will be less than 90°, which will cause particles to flow in the upstream direction, which is not preferable. Also, if the rotation speed is low , when the fluidity of the granular material is poor, the fluctuation of the coarsely packed part is large. For example, when the rotation speed is low, the roughly packed part becomes small and the rate of change in particle movement m from the upstream side to the downstream side becomes large. Therefore, it becomes difficult to control the particle retention 1 in the upstream zone.In such a case, as a result of various experiments, if the width of the paddles of the paddle set before and after the partition wall is the same, 1□/1 ≧1 and S /S1 It was found that when ≧1, the movement of the powder and granular material from the upstream side to the downstream side was performed smoothly.

After conducting numerous experiments to find out what range 11 should be practically set for the inner diameter of the container, it was found that the appropriate range for 11 is D/100≦11≦D/20. . In addition, if S2/S1 is too large, the roughly filled area generated by the downstream paddle will not reach the opening, making it difficult to obtain the effects of the present invention, and the state of agitation of the powder and granular material in the clearance 82 area will deteriorate, which is extremely In this case, it becomes a dead space. Regarding this point as well, an appropriate range of 1≦S/S1≦3 was obtained through experiments.

As described above, we were able to obtain a reactor that was superior to conventional reactors, but after many experiments, the following phenomenon was discovered. In other words, as the powder moves from the upstream side to the downstream side in the reactor, its properties change due to the influence of fluctuations in the amount of liquefied gas coolant and catalyst supplied, and the flow characteristics may deteriorate, or temporarily. Due to factors such as an increase in the reaction rate in a certain stirring zone, the average level of powder accumulation in the downstream stirring zone that follows the upstream stirring zone may be higher than that of the upstream stirring zone. In such a case, the above condition (+
) to (V) may still be insufficient to improve the RTD of the powder or granular material. We reconsidered the conditions for solving these problems. As a result, it is very effective to reduce the average level of granular material accumulation in the downstream zone to be lower than that in the upstream zone; In the two paddle sets, making the width W1 of the flat paddle of the upstream paddle set larger than the width W2 of the flat paddle of the downstream paddle set (that is, Wl./W2>1) can bring about good results. I understand. Therefore, in place of conditions (11) to (iv), the width of the flat paddle is W1°.

Although reactors with W2 in the above-mentioned size relationship were manufactured and tested, good results were often not obtained.

After further consideration, this Wl. /W2〉1n” 1
7w The condition that 1n≧1, the condition that Wl is satisfied.That is, the condition that the width W1° of each flat paddle facing each partition wall on the upstream side is the same or increases sequentially from the upstream side to the downstream side, and the condition (+ ) to (V), the effect of sequentially lowering the average level of powder and granular material accumulation in each stirring zone from the supply port of the material to be stirred to the discharge port of the product is achieved first. Obtained I/I, S
This is added to the effects of Conditions 1 and 21 that apply to /S2, and it is possible to obtain the effect of further improving the RTD of powder and granular material compared to a conventional reactor that simply has a fixed weir added. Size n+1 /W, n
〉1, this is clear. In particular, the Wl effect was remarkable. Further, through numerous experiments, it was found that in addition to W1n/W > 1, the width conditions of the flat paddles in 211 paddle pairs that face each other with a partition wall in between are Wl. Adding the condition /W2≦4 0+1/W1゜<1.
It has been found that good results can be obtained by setting the condition 2 and 1≦W1.

Wl. The reason for limiting the /W2 condition to 4 is that when considering T (twice the difference between peak torque and average torque) to the torque width of the stirring device, W (width of a general flat paddle), W
l. When W2 and W2 are all equal, ΔKing is the smallest, but if the width of each paddle is large or small, ΔKing becomes large, and W1
This is because when °/W2 exceeds 4, there is a tendency for ΔT to increase rapidly.

Furthermore, even if conditions m to (vii) are satisfied, between the 8 pairs of paddle sets that sandwich the partition wall, 1 to each other, 12 to each other, S to each other,
When S and W2 are different from each other, the movement of the powder and granules between stirring zones may be disturbed and the above effect may be insufficient. Therefore, in order to ensure the above effect, the condition (v
iii) was set.

Therefore, according to conditions (vi), (vii), and (viii), Wln becomes equal or larger from the upstream side to the downstream side, but Wl. When there are pairs of paddle sets with /W2=4, Wlo is equal and Wl in all subsequent downstream pairs of paddle sets.

/W2-4. Wl in every pair of paddle groups.

/There are two or more pairs of paddle sets with different W2, that is, there is a small Wl on the upstream side during every W1°.

There are two or more types of Wl, large and small, with a large W1' on the downstream side.

is preferably present.

〔Example〕

The present invention will be described in detail below with reference to the drawings. 1st
As shown in the figures to FIG. 4, a rotating shaft 5 is arranged to coincide with the central axis of the cylindrical container 1, and a plurality of flat paddles 4.4 are fixed to the rotating shaft 5 at a plurality of locations in the axial direction. A paddle group is being made. In this way, the stirrer 7 is constructed. In FIG. 1, the position of the flat paddle in the rotational direction is shown changed as appropriate for easy understanding. Cylindrical container 1
is partitioned by partition walls 2.2' and 2'', and the first
Zone F3a, second zone 8b, third zone 3C, fourth
A zone 8d is formed. The partition walls 2.degree. 2', 2'' have openings 6 at their lower parts.The first zone 8a is provided with an inlet 10 for the object to be stirred, and the fourth zone 8d is provided with a product outlet 11.

The raw material gas and coolant supply ports and the unreacted gas discharge port are not shown in FIG. The number of flat paddles in the paddle set having the above configuration is not particularly limited, but it is desirable that the number of flat paddles in the paddle sets before and after the partition wall be three or less, as described above. Ratio of length to diameter of cylindrical container 1 L/
D is preferably 1.0 or more. Note that partition wall 2.
2'.

The 2" opening 6 is 135° to 270° in the direction of rotation of the rotational axis, with the upper direction of the vertical line as a reference in the plane perpendicular to the rotational axis.
It is desirable that the opening is within the range of 100°C, and the shape is such that the opening is always buried in the particle layer. The opening 6 shown in FIGS. 2 to 4 is within a range of 180 DEG to 225 DEG in the direction of rotation, and the width X of the opening is about 1/6 of the diameter of the container.

With such an opening shape, even if the amount of powder and granular material held is 20% of the reactor volume, the opening can be kept buried in the particle layer at all times.

If a horizontal reactor configured in this way is used to carry out, for example, the gas-phase polymerization of olefins, separate feed gas and coolant circulation systems are connected to the respective zones or zone groups to control the feed gas and coolant. is circulated to the zone, and a catalyst containing a transition metal compound is supplied from the stirring counter-dyeing supply port 10, and the granular material 3, which is a polymerizing organism, is
is stirred by the stirrer 7, moves downstream, and is extracted from the product extraction port 11. At this time, the rotational speed of the stirrer 7 is set such that the Froude number Fr is in the range of 0.05 to 3.0, particularly 0.2 to 3.0.
It is preferable to rotate it so that it becomes a range of 2.0.

The Froude number is determined by the formula Fr=Rw2/q.

Here R: length from the center of the rotation axis to the tip of the paddle, W: Angular velocity 52727 seconds Ω: Gravitational acceleration.

Further, it is preferable that the amount of powder and granular material held in the container is 20 to 80 volume G% and continuous processing is performed.

When the product is a polymer, examples of its types include:
Ethylene polymer, propylene polymer, butene polymer, ethylene propylene polymer, ethylene-butene 1
copolymers, propylene-butene 1 copolymers, propylene-butene 1-ethylene copolymers, and the like.

FIG. 5 shows a process for carrying out gas phase polymerization of polypropylene using a horizontal reactor as described above.

The first part of the horizontal reactor. Propylene gas, which is an unreacted gas discharged from the second zones 8a and 3b, is transferred to the exhaust gas line 2.
0 to the cyclone separator 30. The propylene gas from which entrained particles have been removed in the cyclone separator 30 is cooled in the condenser 21 and partially liquefied. Propylene in a gas-liquid state is introduced from the condenser 21 to the separator 22, where it is separated into gas and liquid. The propylene gas extracted from the separator 22 is supplied to the first gas supply port 24 by a blower 23. It is blown into the second zones 8a, 8b. On the other hand, the liquefied propylene extracted from the separator 22 is sent by the pump 25 to the first coolant inlet 27.
．． It is injected into the second zones 8a, 8b. Hydrogen gas and propylene gas are supplied to the gas circulation system through a hydrogen gas supply line 28 and a propylene gas supply line 29, respectively.
Controlled by a hydrogen concentration of 0. Third. The gas circulation system of the fourth zone is constructed similarly to that of the above-mentioned side zone except for the cyclone separator 30. In the figures, corresponding components are designated by the same numbers and indicated by a dash.

Next, the data obtained by implementing the present invention will be specifically shown. The diameter of the cylindrical container 1 is 430 m, and the length L is 1320 m.
The diameter of the rotating shaft is 110 mm, the clearance of the flat paddle is I 1 = 5 ax, + 2 = 55 m, 8
1 = 5 shoes, 82-10m. The number of flat paddles in each paddle set was two, and the advance angle between each paddle spacing was 90° except for the paddle sets before and after the partition wall. Cylindrical container 1 to 4
Partition walls 2°2+ and 2n were arranged at equally dividing positions, and the openings had the same shape as shown in FIGS. 2 to 4 and had a width X of 25 m. The lead angle β of the flat paddle in the downstream zone between the paddles before and after the partition walls 2.2' and 2'' was set to 45°.The lead angle α of the flat paddle in the upstream zone was set to 1359.

Regarding the width of the flat paddle of the paddle set that sandwiches the bulkhead, W1
3=72 rin. In the cylindrical container 1, inert polypropylene was charged in advance at 60% by volume based on the container volume, and the polymerization conditions were set by rotating at a rotation speed of 6 Orpm (Fr=0.826) at a temperature of 70°C and a pressure of 22N9/ciG. The inside of the cylindrical container 1 was stabilized at the bottom. The inside of the cylindrical container is stably infiltrated, and the catalyst is fed from the stirring object supply port 10 at approximately 1.59/h.
The polymerization reaction was carried out continuously by supplying at a ratio of r. The amount of powder and granules held in the cylindrical container during the steady state of the reaction was approximately 65% by volume relative to the container volume, and polypropylene was produced from the product outlet 11 at an average rate of 15 kg/hr. Note that a discharge port 31 was provided at the bottom of the second zone 8b, and the powder and granular material was sampled from there.

Production of polypropylene is carried out in two grades, among which the average molar ratio of hydrogen gas to unreacted propylene gas during the production of grade 1 is in the exhaust gas line 2.
It was 0.045 at 0 and 0.001 at exhaust gas line 20'. In addition, when producing Grade 2, the exhaust gas line 20 has a temperature of 0°015, and the exhaust gas line 20' has a temperature of 0.0.
It was 05.

Table 1 shows the polymer test results of the obtained polypropylene. VFR (melt flow rate, measurement method J-I) in Table 1
The A value of SK6758) is the MFRI of the polypropylene collected from the bottom outlet 31 of the second zone, and the B value is the MFR of the polypropylene collected from the product withdrawal port 11.
It is a value. The Q value is the value obtained by dividing the weight average molecule m by the number average molecule obtained by GPC (Japan Waters liquid chromatograph GPC150c), and represents the flow characteristics when the polymer is melted. is good. Furthermore, FhfI is the MFR when the load is 5 times (10.8N!F) the load at the time of the specific MFR measurement (normally 2.16Kg load).
It is a value obtained by dividing the value by the MFR value (above-mentioned B value) under normal load, and similarly to the Q value, the larger the F value, the better the above-mentioned flow characteristics become.

In addition, when the respective holding speeds of each zone were weighed at the completion of the polymerization reaction in the example, the first zone had 12.2 to 3 kg, the second zone had 12.11 kg (ff), the third zone had 12.6 kg, and the third zone had 12.2 to 3 kg. Zone 4 was 13.ONg.

It was found that each zone had almost the same amount of m, indicating that the m possessed by each zone was controlled smoothly.

[Comparative example]

A polymerization reaction was carried out using the same process and combination conditions as in the example except that the three partition walls in the example were removed. However, the hydrogen supply m of each hydrogen gas supply line 28, 28' was produced by maintaining the grade 1 and grade 2 hydrogen supply v1 of the example with reference to the results of the example.

Table 2 shows the polymer test results of the obtained polypropylene. Note that grade 3 in Table 2 corresponds to grade 1, and grade 4 is polypropylene produced in a hydrogen supply system, which corresponds to grade 2.

From Tables 1 and 2, it can be seen that Grade 1 and Grade 2 are polypropylenes with a larger difference in MFR than Grade 3 and Grade 4, and also have a large Q value and Fl, and have good flow characteristics.

〔Effect of the invention〕

The horizontal reactor according to the present invention is divided into three or more zones by partition walls, so that different atmospheres can be controlled between two or more zone groups, and particles can be smoothly moved between each zone without backflow. Therefore, a product having an arbitrary molecular weight distribution curve can be produced, and for example, in the case of polypropylene, it is possible to improve the flow properties.

Further, since the RT() is improved, the amount of catalyst consumed is small, and the movement of particles between the partition walls is smooth, so continuous operation for a long period of time is possible.

[Brief explanation of the drawing]

FIG. 1 is a vertical cross section of a horizontal reactor showing an embodiment of the present invention, FIGS. 2 to 4 are views taken along the line Δ-8 in FIG. 1, and FIG. It shows the state where @5 is rotated 90'. FIG. 5 is a system diagram of a process using a horizontal reactor according to an embodiment of the present invention. 1... Cylindrical container, 2... Partition wall, 3... Powder,
4... Flat paddle, 5... Rotating shaft, 6... Opening, 7... Stirrer, 8a, 8b, 8c, 8d... First
．． Second. 3rd゜4th zone, 10... Stirring object supply port, 11... Product extraction port.

Claims (1)

[Scope of Claims] 1. A cylindrical container having a horizontal central axis; an agitator having a rotating shaft aligned with the horizontal central axis; and a stirring device disposed at each end of the cylindrical container. consisting of an object supply port and a product withdrawal port, and two or more partition walls arranged perpendicularly to the rotating shaft and having an opening at the bottom and dividing the inside of the cylindrical container into three or more zones, The three or more zones are connected to two or more independent gas circulation systems for circulating and supplying gas, and the particle layer present in the cylindrical container fills the openings of the partition wall to form a gas phase. - In a horizontal reactor for performing a solid-phase reaction, the stirrer includes a plurality of paddle sets each having one or more flat paddles attached to a predetermined position in the axial direction of a rotating shaft, and in particular, paddle sets that face each other across the partition wall. The two paddle sets constituting the paddle set satisfy the following conditions (i) to (vi) for each pair, and the conditions (vii) to (viii) are satisfied for the relationship between the adjacent pairs. horizontal reactor. (i) 10°≦β≦45° (ii) D/100≦l_1≦D/20 (iii) l_2/l_1≧1 (iv) 1≦S_2/S_1≦3 (v) α≧90° (vi) 1<W_1^n/W_2≦4(1≦n≦N)(
vii) 1≦W_1^n^+^1/W_1^n<1.2
(1≦n≦N-1) (viii) Between all adjacent pairs of paddle groups, l
_1 to each other, l_2 to each other, S_1 to each other, S_2 to each other, W_
The two are each equal to each other. The meanings of the symbols in the above formula are as follows. β: Advance angle of the rotational direction of the paddle on the product extraction side relative to the paddle on the stirring object supply side D: Inner diameter of the cylindrical container l_1: Clearance between the inner wall of the container and the tip of the paddle on the stirring object supply side l_2: The inner wall of the container and the product Clearance between the tip of the paddle on the product extraction side S_1: Clearance between the paddle on the supply side of the object to be stirred and the partition wall S_2: Clearance between the paddle on the product extraction side and the partition wall W_1^n: Counting from the supply port of the object to be stirred Width W_2 of flat paddles on the supply side of the object to be stirred in the pair of paddles that sandwich the n-th partition: Width N of the flat paddles on the product outlet side of the pair of paddles that sandwich the partition: Number of partitions α: Object to be stirred Claim 1, wherein the rotational advance angle of the supply side paddle relative to the product extraction side paddle is 2, and the supply port for the object to be stirred provided at one end of the cylindrical container is a supply port for a catalyst that causes a polymerization reaction. Horizontal reactor as described in section. 3. The gas phase-solid phase reaction is an olefin polymerization reaction, and the gases circulated and supplied to the gas circulation system include raw material gas, hydrogen gas, and liquefied gas as a coolant, as claimed in claim 1 or 2. Horizontal reactor as described in section.