Bubble column reactor

Abstract

A bubble column reactor is provided comprising a reaction zone in which a reaction of gaseous reactants is carried out in a liquid reaction medium, a first separation section arranged above the reaction zone and into which a first effluent stream rising from the reaction zone is introduced, and a condensation zone arranged above the first separation section, wherein the diameter of the condensation zone is smaller than the diameter of the first separation section.

Description

Technical Field

[0001] Cross-reference to related applications

[0002] This application claims priority to Korean Patent Application No. 10-2021-0177022, filed on December 10, 2021, the entire contents of which are incorporated herein by reference for all purposes. Technical Field

[0004] This invention relates to a bubble cap reactor, and more specifically, to an oligomer production apparatus for reducing the amount of solids and liquids entrained in the reactor during oligomer production, thereby improving the stability of the entire process. Background Technology

[0005] Alpha-olefins are widely used commercially as important materials in comonomers, detergents, lubricants, and plasticizers. In particular, 1-hexene and 1-octene have been widely used as comonomers to control the density of polyethylene in the production of linear low-density polyethylene (LLDPE).

[0006] Alpha-olefins are typically prepared by the oligomerization of ethylene. As a reactor type for carrying out ethylene oligomerization, bubble-cap reactors have been used. These reactors use gaseous ethylene as a reactant, and the oligomerization (trimerization or tetramerization) of ethylene occurs through contact with a reaction zone comprising a liquid reaction medium, which includes a catalyst.

[0007] In the case of a bubble cap reactor, the gaseous reactants are mixed with the liquid reaction medium in the reaction zone, existing as a two-phase reaction. As a result of the catalytic reaction, a small amount of polymer is produced as a byproduct, which floats in the liquid reaction medium. At this time, due to the rate at which a large amount of gaseous reactants are introduced into the reaction zone in the form of a large number of bubbles, entrainment of solid polymer and liquid reaction medium inevitably occurs.

[0008] Due to this entrainment, byproduct polymers accumulate not only on the inner walls of the reactor but also on downstream process units such as condensers, pipes, and valves, resulting in scaling. Therefore, scaling occurring in downstream process units leads to equipment degradation and mechanical damage, and in the worst case, may require shutting down the entire process. This results in increased costs associated with the scrubbing process and reduced production due to decreased operating time.

[0009] Therefore, in order to solve the above problems, it is necessary to study how to reduce the entrainment of polymer-containing solids and liquids in bubble cap reactors. Summary of the Invention

[0010] [Technical Issues]

[0011] In order to address the problems mentioned in the background art, one object of the present invention is to provide a bubble cap tower reactor for preventing the entrainment of byproducts, including polymer materials, in addition to the desired product in the reactor, thereby improving the stability of the entire process.

[0012] [Technical Solution]

[0013] In one general aspect, a bubble cap reactor includes: a reaction zone in which gaseous reactants are reacted in a liquid reaction medium; a first separation section disposed above the reaction zone and into which a first effluent stream rising from the reaction zone is introduced; and a condensation zone disposed above the first separation section, wherein the diameter of the condensation zone is smaller than the diameter of the first separation section.

[0014] [Beneficial Effects]

[0015] According to the bubble cap reactor of the present invention, a condensation zone is provided above the reaction zone of the bubble cap reactor, thereby preventing the condenser itself from scaling due to entrainment, compared with the prior art where a separate condenser is provided outside the bubble cap reactor.

[0016] Meanwhile, by making the diameter of the condensation zone above the reaction zone of the bubble cap reactor smaller than that of the separation section, the contact area between the gas stream introduced into the condensation zone and the cooling coils located in the condensation zone can be maximized, thereby improving condensation efficiency. As a result, the solvent and polymer in the gas stream can be effectively condensed and returned to the reaction zone.

[0017] Furthermore, by making the diameter of the condensation zone smaller than that of the separation section, flow changes can be induced in the separation section for the gas stream that has passed through the condensation zone, thereby making the distribution of the gas stream in the separation section uniform and thus improving the sedimentation effect in the separation section.

[0018] Therefore, the stability of the entire process can be improved by reducing the amount of entrained solids and liquids that are not vapors. The reactor's downtime can be effectively increased by fundamentally preventing scaling in downstream process units. Furthermore, energy costs can be reduced by preventing efficiency losses due to scaling in downstream process units. Attached Figure Description

[0019] Figure 1 This is a view illustrating the bubble cap tower reactor and related process flow according to an embodiment of the present invention.

[0020] Figure 2 and Figure 3 This is a schematic diagram showing a bubble cap tower reactor of the prior art. Detailed Implementation

[0021] The terms and words used in the specification and claims of this invention should not be interpreted in their general or dictionary sense, but rather should be interpreted as being based on the principle that the inventors are able to appropriately define the concepts of the terms in order to best describe their own invention, and to satisfy the meaning and concept of the technical ideas of this invention.

[0022] In this invention, the term "stream" can refer to the flow of fluid in the process, or to the fluid itself flowing through a delivery pipeline (pipeline). Specifically, "stream" can refer to both the fluid itself flowing through the pipes connecting the various devices and the flow of fluid. Furthermore, fluid can refer to one or more of gases or liquids.

[0023] In this invention, the term "C#" where "#" is a positive integer refers to all hydrocarbons having # carbon atoms. Therefore, the term "C10" refers to a hydrocarbon compound having 10 carbon atoms. Furthermore, the term "C#+" refers to all hydrocarbon molecules having more than # carbon atoms. Therefore, the term "C10+" refers to a mixture of hydrocarbons having more than 10 carbon atoms.

[0024] In the following text, reference will be made to aid in understanding the invention. Figure 1 The invention will now be described in more detail.

[0025] According to one embodiment of the present invention, a bubble cap reactor 100 may include: a reaction zone 300 in which a reaction of gaseous reactants is carried out in a liquid reaction medium; a first separation section DS1 disposed above the reaction zone 300, and a first effluent stream rising from the reaction zone is introduced into the first separation section; and condensation zones CZ1 and CZ2 disposed above the first separation section, wherein the diameters of the condensation zones CZ1 and CZ2 may be smaller than the diameter of the first separation section DS1.

[0026] According to one embodiment of the present invention, the bubble cap reactor 100 can be used to prepare oligomer products by carrying out an oligomerization reaction of gaseous reactants including monomers in a liquid reaction medium of solvent and catalyst.

[0027] More specifically, the bubble cap reactor 100 may include a reaction zone 300, and a reaction medium may be supplied to the reaction zone 300 via one or more reaction medium supply lines 310 connected to one side of the reaction zone 300. Here, the reaction medium may include a catalyst, a co-catalyst, and a solvent. The catalyst, co-catalyst, and solvent may be supplied separately via individual reaction medium supply lines 310, and two or more reaction medium components may be mixed and supplied to the reaction zone 300 via reaction medium supply lines 310.

[0028] According to one embodiment of the present invention, the monomer may include ethylene monomer. As a specific example, a gaseous reactant containing ethylene monomer may be supplied to the lower chamber 200 of the bubble cap reactor 100 (described later) to generate the desired α-olefin product through an oligomerization reaction.

[0029] The solvent may include one or more selected from n-pentane, n-hexane, n-heptane, cyclohexane, methylcyclohexane, octane, cyclooctane, decane, dodecane, benzene, xylene, 1,3,5-trimethylbenzene, toluene, ethylbenzene, chlorobenzene, dichlorobenzene, and trichlorobenzene.

[0030] The catalyst may include a transition metal source. The transition metal source may be one or more compounds selected from, for example, chromium acetylacetonate (III), chromium tetrahydrofuran chloride (III), chromium 2-ethylhexanoate (III), tris(2,2,6,6-tetramethyl-3,5-heptadecanoate)chromium (III), chromium benzoylpyruvate (III), chromium hexafluoro-2,4-pentanedione (III), chromium acetate (III) hydroxide, chromium acetate (III), chromium butyrate (III), chromium valerate (III), chromium laurate (III), and chromium stearate (III).

[0031] The cocatalyst may include one or more selected from, for example, trimethylaluminum, triethylaluminum, triisopropylaluminum, triisobutylaluminum, ethyl sesquichloride, diethylaluminum chloride, ethyl dialuminum chloride, methylaluminoxane, modified methylaluminoxane, and borate esters.

[0032] Simultaneously, in the reaction zone 300 of the bubble cap reactor 100, oligomerization of monomers can occur in a liquid reaction medium including a catalyst, a co-catalyst, and a solvent. As described above, the region comprised of the reaction medium in which the oligomerization of monomers occurs can be defined as reaction zone 300. Oligomerization can refer to a reaction that causes monomers to oligomerize. Depending on the number of monomers to be polymerized, oligomerization can be called trimerization or tetramerization, collectively referred to as polymerization.

[0033] Alpha-olefins are widely used commercially as important materials in comonomers, detergents, lubricants, plasticizers, and more. In particular, 1-hexene and 1-octene are commonly used as comonomers to control the density of polyethylene in the production of linear low-density polyethylene (LLDPE). Alpha-olefins such as 1-hexene and 1-octene can be prepared by trimerizing or tetramerizing, for example, ethylene.

[0034] The bubble cap reactor 100 may include a product discharge line 320 connected to the reaction zone 300 and located on the other side of the reaction medium supply line, through which products including α-olefins, which are oligomerization products, can be discharged. That is, the product discharge stream 320 may include oligomer products and solvents generated by the oligomerization reaction, and the oligomer products and solvents may be separated by an additional separation device. The separated solvent can be reused during the oligomer production process. Furthermore, for example, when ethylene monomer is used as the monomer for the oligomerization reaction, the oligomer products may include 1-hexene and 1-octene. The supply of the reaction medium to the reaction zone 300 and the discharge of products from the reaction zone 300 can be carried out continuously.

[0035] Meanwhile, the gaseous reactants, including monomers, used for the oligomerization reaction can be supplied through the gaseous reactant supply line 210 to the lower chamber 200 located at the bottom of the bubble cap reactor 100, and then supplied through the dispersion plate 350 to the reaction zone 300 containing the liquid reaction medium.

[0036] That is, the dispersion plate 350 can be disposed between the lower chamber 200 and the reaction zone 300, and gaseous reactants (e.g., monomers) can be uniformly distributed and supplied to the reaction zone 300, which includes the reaction medium, from the lower chamber 200 through through holes formed at equal intervals along the center and circumference of the dispersion plate 350.

[0037] Gaseous reactants flowing into the reaction zone 300, which contains a liquid reaction medium, are introduced into the reaction zone 300 through the dispersion plate 350 and simultaneously dispersed. The force of the dispersed gas generates turbulence, allowing the liquid reaction medium and gaseous reactants to mix naturally. At this time, the dispersion force of the gaseous reactants flowing into the reaction zone 300 through the dispersion plate 350 can be maintained greater than the head pressure acting downward from the liquid reaction medium, allowing the liquid reaction medium to remain in the reaction zone 300.

[0038] Meanwhile, as described above, the gaseous reactants supplied to the reaction zone 300 of the bubble cap reactor 100 can be catalyzed in a liquid reaction medium containing a solvent and a catalyst; specifically, the catalytic reaction can be an oligomerization reaction. In this case, the gaseous reactants and the reaction medium in the reaction zone 300 are mixed together, existing as two phases. Simultaneously, in the reaction zone 300, as a result of the catalytic reaction of the gaseous reactants, a small amount of polymer can be generated as a byproduct, which floats in the liquid reaction medium. At this time, due to the rate at which a large amount of gaseous reactants are introduced into the reaction zone 300 in the form of a large number of bubbles, entrainment of solid polymers and liquid reaction medium may occur. That is, when unreacted gaseous reactants move upward through the reaction zone 300, not only the unreacted gaseous reactants but also the polymers and solvents as byproducts move upward together. In this case, the entrained polymers deposit in the downstream process unit of the bubble cap reactor 100 due to polymer adhesion, resulting in scaling that hinders fluid flow.

[0039] Therefore, the bubble cap reactor 100 according to one embodiment of the present invention may include a separation section DS and a condensation section CZ disposed above the reaction zone 300, thereby preventing polymer-containing byproducts from being entrained, thereby preventing scaling in downstream process units and improving the stability of the entire process.

[0040] More specifically, refer to Figure 1 The gaseous first effluent stream from reaction zone 300 can be introduced into the first separation section DS1. In addition to unreacted gaseous reactants, the first effluent stream may also include non-vapor components, such as entrained polymers and solvents. The passage of the first effluent stream through the first separation section DS1 reduces its upward velocity, and some of the non-vapor components, such as entrained polymers and solvents, particularly some polymer non-vapor components (which are solid materials with a relatively high density), can preferentially precipitate into reaction zone 300. For example, approximately 10% of the vaporized solvent and non-vapor components contained in the first effluent stream can be precipitated by the first separation section DS1.

[0041] Subsequently, the first effluent stream from the first separation section DS1 can be introduced into the condensation zone CZ. Condensation zones CZ1 and CZ2 may include cooling coils, to which refrigerant can be supplied. The first effluent stream from the first separation section DS1 can be passed through the condensation zones CZ1 and CZ2, which are formed with low temperatures, thereby allowing a large amount of vaporized solvent and entrained polymer to precipitate. Specifically, the vaporized solvent can be liquefied through condensation, and the liquefied solvent can be precipitated and returned to the reaction zone.

[0042] Meanwhile, referring to the bubble cap tower reactor shown in the prior art Figure 2The bubble cap reactor sequentially comprises a lower chamber, a reaction zone, and a separation section therein, but does not include a condensation zone as described in this invention. That is, unreacted vapors discharged to the top of the bubble cap reactor are condensed by an external heat exchanger, and then the condensed components, such as solvents and unreacted gaseous reactants, are separated by a separation device (e.g., a flash tank). In this case, entrained polymer components may be discharged unaffected to the top of the bubble cap reactor, and polymer components may deposit in the heat exchanger, flash tank, and connecting pipes, leading to frequent scaling.

[0043] In other words, according to one embodiment of the present invention, since the condensation zones CZ1 and CZ2 are located inside the bubble cap reactor 100, rapid condensation and precipitation of the mixed gas can be achieved even without separate equipment (such as pipes), compared to the case where a separate condenser is provided outside the bubble cap reactor. Furthermore, it fundamentally solves the scaling problem in the pipes between the bubble cap reactor and the external condenser, or the scaling problem of the condenser itself, caused by polymer entrainment.

[0044] According to one embodiment of the present invention, condensation zones CZ1 and CZ2 may include a first condensation zone CZ1 and a second condensation zone CZ2, and a second separation section DS2 may be provided between the first condensation zone CZ1 and the second condensation zone CZ2. That is, the bubble cap reactor 100 may sequentially include a first separation section DS1, a first condensation zone CZ1, a second separation section DS2, and a second condensation zone CZ2 above the reaction zone 300.

[0045] Specifically, the first effluent stream, which has passed through the first separation section DS1, passes through the first condensation zone CZ1 and is introduced into the second separation section DS2. The stream discharged to the upper part of the second separation section DS2 can be used as the second effluent stream through the second condensation zone CZ2. In this process, the vaporized solvent and entrained polymer in the first effluent stream rising from the reaction zone 300 can be almost completely removed, and the gaseous effluent stream 550 containing unreacted monomer components can be discharged to the upper part of the bubble cap reactor 100.

[0046] Furthermore, according to one embodiment of the present invention, the bubble cap reactor 100 can be cylindrical with a circular cross-section, and the reaction zone 300, condensation zones CZ1 and CZ2, and separation sections DS1 and DS2 can also have circular cross-sections. The first and second condensation zones CZ1 and CZ2 can have the same diameter, the first and second separation sections DS1 and DS2 can have the same diameter, and the diameters of the first and second condensation zones CZ1 and CZ2 can be smaller than the diameters of the first and second separation sections DS1 and DS2. Here, the diameters of the first and second condensation zones CZ1 and CZ2 specifically refer to the diameters of their cross-sections, and the diameters of the first and second separation sections DS1 and DS2 specifically refer to the diameters of their cross-sections.

[0047] That is, the condensation of the vaporized solvent and entrained non-vapor in condensation zones CZ1 and CZ2 occurs through the low temperature inside condensation zones CZ1 and CZ2. If the diameters of condensation zones CZ1 and CZ2 are too large, the temperature within them may be uneven. In this case, condensation may occur near the cooling coil, but relatively less at points far from the cooling coil, leading to an increase in the non-contact zone (dead zone). Therefore, by making the diameters of condensation zones CZ1 and CZ2 smaller than the diameters of the first and second separation sections DS1 and DS2, for example, the non-contact zone between the cooling coil and the mixed gas can be reduced, such as by wrapping the hollow portion of the cooling coil, thereby improving the condensation efficiency and precipitation efficiency in the condensation zones.

[0048] Therefore, the diameter of the condensation zone can be 35% to 70% of the diameter of the separation section. Specifically, the diameters of the first and second condensation zones CZ1 and CZ2 can be 35% to 70% of the diameters of the first and second separation sections DS1 and DS2. When the ratio of the diameters of the first and second condensation zones CZ1 and CZ2 to the diameters of the first and second separation sections DS1 and DS2 is greater than 35%, the rising gas flow through the first and second condensation zones CZ1 and CZ2 can be smoothly formed. When the diameter ratio is less than 70%, the non-contact area between the cooling coil and the mixed gas can be reduced, making the temperature distribution in the condensation zone more uniform.

[0049] As the first effluent stream, having passed through the first separation section DS1, passes through the first condensation zone CZ1, the vaporized solvent and entrained polymer in the first effluent stream are condensed and precipitated. Specifically, the vaporized solvent can be liquefied through condensation, and the liquefied solvent can be precipitated for return to the reaction zone. In this process, for example, via passing through the first condensation zone CZ1, approximately 40% of the vaporized solvent and non-vaporized components contained in the first effluent stream can be precipitated.

[0050] Meanwhile, according to one embodiment of the present invention, a second separation section DS2 with a diameter larger than that of the first condensation zone CZ1 and the second condensation zone CZ2 can be disposed between the first condensation zone CZ1 and the second condensation zone CZ2. That is, the first outflow gas stream from the first condensation zone CZ1 is introduced into the second separation section DS2. Due to the larger diameter of the second separation section DS2, eddies exist in the introduced gas stream, causing changes in flow velocity and direction. As a result, the mixed gas can be uniformly mixed in the second separation section DS2, thus improving the precipitation efficiency of the mixed gas. Furthermore, the condensation efficiency in the second condensation zone CZ2 can be improved because the gas stream is uniformly mixed again in the second separation section DS2 before being introduced into the second condensation zone CZ2. For example, when the gas stream passes through the second separation section DS2, approximately 10% of the vaporized solvent and non-vapor contained in the first outflow stream can be further precipitated.

[0051] Furthermore, the gas stream from the upper part of the second separation section DS2, including some unreacted monomers and mixed gases, can be discharged as the second effluent stream and introduced into the second condensation zone CZ2. In the second condensation zone CZ2, non-vapor components (e.g., vaporized solvents and polymers) in the second effluent stream can be condensed and precipitated again, and in the upper part of the second condensation zone CZ2, unreacted monomers, such as a gaseous effluent stream 550 including gaseous ethylene, can be discharged to the upper part of the bubble cap reactor 100. Approximately 40% of the vaporized solvents and non-vapor components contained in the first effluent stream can be further precipitated.

[0052] According to one embodiment of the present invention, condensing zones CZ1 and CZ2 may include cooling coils, and refrigerant may be supplied to the cooling coils. Specifically, the cooling coils are provided in the form of pipes through which refrigerant can flow. The cooling coils are wound from top to bottom of condensing zones CZ1 and CZ2, and refrigerant may be introduced into inlets 510 and 530 of the cooling coils located at the top of condensing zones CZ1 and CZ2, and may be discharged through outlets 520 and 540 of the cooling coils located at the bottom of condensing zones CZ1 and CZ2.

[0053] Specifically, when condensing zones CZ1 and CZ2 include a first condensing zone CZ1 and a second condensing zone CZ2, refrigerant can be introduced into the inlet 510 of the cooling coil located at the top of the second condensing zone CZ2, and refrigerant can be discharged to the outlet 520 of the cooling coil located at the bottom of the second condensing zone CZ2. Here, the temperature of the refrigerant supplied to the inlet of the cooling coil formed in the second condensing zone CZ2 can be in the range of -10°C to -5°C, and the temperature of the refrigerant discharged to the outlet of the cooling coil formed in the second condensing zone CZ2 can be in the range of -5°C to 0°C.

[0054] The significance of the refrigerant temperature in the second condensation zone CZ2 is that, based on thermodynamic relationships, the temperature of the gas effluent stream 550 discharged from the bubble column reactor 100 can be controlled at the desired level.

[0055] Similarly, refrigerant can be introduced into the inlet 530 of the cooling coil located at the top of the first condensing zone CZ1, and the refrigerant can be discharged through the outlet 540 of the cooling coil located at the bottom of the first condensing zone CZ1. The temperature of the refrigerant supplied to the inlet of the cooling coil formed in the first condensing zone CZ1 can be in the range of -5°C to -0°C, and the temperature of the refrigerant discharged to the outlet of the cooling coil formed in the first condensing zone CZ1 can be in the range of 0°C to 5°C.

[0056] When condensing zones CZ1 and CZ2 comprise a first condensing zone CZ1 and a second condensing zone CZ2, the refrigerant required for each of condensing zones CZ1 and CZ2 can be supplied to each inlet of condensing zones CZ1 and CZ2 respectively. However, the refrigerant supplied to the inlet 510 of the cooling coil formed in the second condensing zone CZ2 and discharged to the outlet 520 can be discharged through a refrigerant circulation pipe outside the bubble cap reactor 100, and then supplied to the inlet 530 of the cooling coil formed in the first condensing zone CZ1 to cool the first condensing zone CZ1, and then discharged to the outlet 540 of the cooling coil of the first condensing zone CZ1. In this case, the cooling coils of the first and second condensing zones CZ1 and CZ2 and the refrigerant circulation pipe located outside the bubble cap reactor 100 can be installed as a single pipe. Therefore, the flow meters, control valves, etc. used for flow control can be simplified, which is advantageous in terms of installation and maintenance costs.

[0057] Furthermore, according to one embodiment of the present invention, the height of the second condensing zone CZ2 can be 0.5 to 1 times the height of the first condensing zone CZ1. As described above, the temperature of the refrigerant supplied to the cooling coil of the second condensing zone CZ2 is lower than the temperature of the refrigerant supplied to the first condensing zone CZ1; therefore, the temperature within the second condensing zone CZ2 is lower than the temperature of the first condensing zone CZ1. Therefore, even when the height of the second condensing zone CZ2 is less than the height of the first condensing zone CZ1, the desired condensation efficiency can be achieved in terms of non-vapor removal and condensation efficiency per unit volume, and this allows for a reduction in the overall height of the bubble cap tower reactor 100.

[0058] According to one embodiment of the present invention, the sum of the heights of the first condensing zone CZ1 and the second condensing zone CZ2 can be one to two times the height of the second separation section DS2. That is, the total height of the bubble cap reactor 100 can be reduced by setting the height of the second separation section DS2 to a level that achieves uniform gas mixing through vortex generation.

[0059] The bubble cap tower reactor according to the invention has been described and illustrated above. However, the description and illustrations are only for essential purposes of understanding the invention, and processes and apparatuses not separately described and illustrated in the drawings may also be suitably applied and used to implement reactor cleaning devices and methods, in addition to the processes and equipment described and illustrated in the drawings.

Claims

1. A bubble column reactor comprising: a reaction zone in which a reaction of a gaseous reactant is carried out in a liquid reaction medium; a first separation section disposed above the reaction zone and into which a first effluent stream rising from the reaction zone is introduced; and a condensation zone disposed above the first separation section, wherein the condensation zone comprises first and second condensation zones and a second separation section is disposed between the first and second condensation zones, wherein the diameters of the first and second condensation zones are less than the diameters of the first and second separation sections.

2. The bubble column reactor according to claim 1, wherein, the diameters of the first and second condensation zones are between 35% and 70% of the diameter of the first separation section.

3. The bubble column reactor of claim 1 wherein, the first and second condensation zones comprise cooling coils and refrigerant is supplied into the cooling coils.

4. The bubble column reactor of claim 1 wherein, the diameters of the first and second condensation zones are between 35% and 70% of the diameters of the first and second separation sections.

5. The bubble column reactor of claim 1, wherein, the first condensation zone and the second condensation zone each comprise cooling coils, and the refrigerant supplied to the inlet of the cooling coils formed in the second condensation zone and discharged to the outlet of the cooling coils is supplied to the inlet of the cooling coils formed in the first condensation zone and discharged to the outlet of the cooling coils.

6. The bubble column reactor of claim 5, wherein, the temperature of the refrigerant supplied to the inlet of the cooling coils formed in the second condensation zone is -10°C to -5°C, and the temperature of the refrigerant supplied to the inlet of the cooling coils formed in the first condensation zone is -5°C to 0°C.

7. The bubble column reactor according to claim 1, wherein, the height of the second condensation zone is 0.5 to 1 times the height of the first condensation zone.

8. The bubble column reactor according to claim 1, wherein, the sum of the heights of the first and second condensation zones is 1 to 2 times the height of the second separation section.

9. The bubble column reactor according to claim 1, wherein, the gaseous reactant comprises ethylene monomer.

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