HU9800123A2 - Gas-phase polymerization processes - Google Patents

Gas-phase polymerization processes Download PDF

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Publication number
HU9800123A2
HU9800123A2 HU9800123A HU9800123A HU9800123A2 HU 9800123 A2 HU9800123 A2 HU 9800123A2 HU 9800123 A HU9800123 A HU 9800123A HU 9800123 A HU9800123 A HU 9800123A HU 9800123 A2 HU9800123 A2 HU 9800123A2
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Prior art keywords
reactor
vortex
bed
volume
height
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HU9800123A
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Hungarian (hu)
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HU9800123A3 (en
HU9800123D0 (en
Inventor
Daniel Durand
Frederic Robert Marie Michel Morterol
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Bp Chemicals Limited
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Priority to FR9700971A priority Critical patent/FR2758823B1/en
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Publication of HU9800123A2 publication Critical patent/HU9800123A2/en
Publication of HU9800123A3 publication Critical patent/HU9800123A3/en
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    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01JCHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/1872Details of the fluidised bed reactor
    • CCHEMISTRY; METALLURGY
    • C08ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08FMACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
    • C08F10/00Homopolymers and copolymers of unsaturated aliphatic hydrocarbons having only one carbon-to-carbon double bond
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01JCHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/19Details relating to the geometry of the reactor
    • B01J2219/194Details relating to the geometry of the reactor round
    • B01J2219/1941Details relating to the geometry of the reactor round circular or disk-shaped
    • B01J2219/1946Details relating to the geometry of the reactor round circular or disk-shaped conical
    • CCHEMISTRY; METALLURGY
    • C08ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08FMACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
    • C08F210/00Copolymers of unsaturated aliphatic hydrocarbons having only one carbon-to-carbon double bond
    • C08F210/16Copolymers of ethene with alpha-alkenes, e.g. EP rubbers
    • YGENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10STECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S526/00Synthetic resins or natural rubbers -- part of the class 520 series
    • Y10S526/901Monomer polymerized in vapor state in presence of transition metal containing catalyst
    • YGENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10STECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S526/00Synthetic resins or natural rubbers -- part of the class 520 series
    • Y10S526/918Polymerization reactors for addition polymer preparation
    • YGENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10STECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S526/00Synthetic resins or natural rubbers -- part of the class 520 series
    • Y10S526/92Apparatus for use in addition polymerization processes

Abstract

The present invention relates to a gas phase polymerization process, in a vortex reactor having a first cylindrical cross-link, which is provided with a cantilevered cavity, called a separating vessel, from which the vortex bed is at least the first full gate of the reactor. The bristle of the process undergoes one or more dimeric coals, such as ethylene, propylene, 1-ene, 1-pentene, 4-methylpentene, 1-hexene or 1-phenol. ŕ

Description

EXTRACT

Gas Phase Polymerization Process

The present invention relates to a gas phase polymerization process in a vortex reactor having a first cylindrical volume above which a second volume, called a separating vessel, is mounted, wherein the vortex bed occupies at least the entire first volume of the reactor.

In the process, one or more olefin monomers such as ethylene, propylene, 1-butene, 1-pentene, 4-methylpentene, 1-hexene or 1-octene polymerize.

• · · · ·

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PUBLISHED

65 321 / BE

SBG & κ.

International

Gas Phase Polymerization Process

The present invention relates to a polymerization process in a vortex reactor.

It is known to polymerize one or more monomers in a gas phase at atmospheric pressure in a fluidized bed reactor, whereby the resulting polymer particles are kept in a fluidized state by the rising flow of the reaction gas mixture containing the monomer (s) to be polymerized. The powdered polymer thus produced is discharged from the reactor to keep the bed at a more or less constant volume. In a preferred industrial scale process, a fluidizing grid is used to disperse the reaction gas mixture in the bed and act as the bed carrier when the gas flow is interrupted. The reaction at the top of the fluidized bed reactor is fed back to the reactor through a fluidized grid through a compressor-driven external circulation line.

Polymerization of monomers is an exothermic reaction. It is therefore necessary to provide a suitable means for cooling the bed to remove the polymerization heat. A preferred method of polymerizing olefins in a vortex bed is to cool the reaction gas mixture below the polymerization temperature, and then, when this fluidizing gas mixture passes through the bed, it allows for compensation for the excess heat generated by the polymerization.

Thus, when the reaction gas mixture is recycled, it is cooled by at least one heat exchanger in the outer circulation pipe to drain the heat generated in the polymerization process and to maintain the polymerization temperature at the desired value.

In recent years, attempts have been made to optimize the gas phase polymerization process to increase the performance of existing plants. The idea was to increase the rate of polymer production in the sense of increasing the yield of the polymer mass (kg / h / m 3 ) per unit time of the reactor volume unit. It is known that in the above-mentioned type of industrial vortex reactors, the rate of extraction depends directly on the rate of heat transfer in the reactor. For example, the flow rate may be increased by increasing the fluidization gas velocity and / or reducing the fluidizing gas temperature and / or increasing the heat capacity of the fluidizing gas.

For example, International Patent Application WO 94/28032 proposes a process for the gas phase polymerization of olefins in which the recycled gas stream is cooled to a suitable temperature to form a liquid and a gas. By separating the liquid from the gas and introducing the liquid directly into the vortex bed, it is possible to increase the total amount of fluid introduced into the vortex reactor, which allows the bed to be cooled by better evaporation and thus to achieve higher yields.

The vortex reactors of the present invention are generally characterized by a first volume whose boundary is defined by a rotation axis produced by a rotation about a vertical axis known as the axis of rotation of the straight and / or curved segment below. a second volume, usually called a separating vessel, whose boundary is also determined by rotation about the axis known as the axis of rotation of the straight and / or curved segment. According to the definition of the separating vessel, the rectangular cross-section of the second volume (directly above the connection between the two volumes) is larger than the rectangular cross-section of the first volume (at its highest point).

Conventional vortex reactors used for gas phase polymerization of olefins, as shown in Figure 1, generally consist of a vertical axis 3 roller 1 above which a separating vessel 3 is mounted. Figure 1 shows schematically a preferred gas phase polymerization apparatus of the present invention.

The function of the separating vessel is known to slow down the gas stream passing through the vortex bed, which may contain a relatively large amount of solid particles. As a result, the solid particles in the gas stream return to the vortex. Only the finest particles are carried out by the gas stream from the reactor.

In principle, the vortex bed could occupy the entire cylindrical part of the reactor, which extends from the bottom of the vortex, which generally coincides with the fluidizing grid 4, up to a height of H. In practice, the vortex bed occupies a portion of the cylindrical portion of the vortex reactor, resulting in a true height (h) of the yoke 65.321 / BE of 0.95 x H, preferably 0.90 x H, especially 0.85 x H. The height limit for the vortex bed is determined by one of ordinary skill in the art to avoid excessive transfer of polymer particles from the reactor. Fluidization studies showed the formation of bubbles in the vortex bed. Bubbles merge during the bed rises, and when they reach the upper part of the swirl bed they burst. This bursting significantly reduces the release of polymer particles from the reactor. This, of course, prompted the practitioner to limit the height of the vortex bed during the polymerization in a practical manner.

In the framework of its exploration-related research on the gas-phase polymerization of olefins, the Applicant, despite the existing prejudices, succeeded in developing a simple and reliable process that would allow a significant increase in polymer production. In addition, the Applicant has unexpectedly discovered that the use of his new procedure has many advantages as described in the following section of the description.

The present invention therefore relates to a gas phase polymerization process performed in a vortex reactor, wherein the reactor has a first volume whose limit is determined by a rotation axis formed by rotation about at least one vertical axis known as the axis of rotation of the straight and / or curved line, over which a usually called a separating vessel, a second volume, the boundary of which is also determined by rotation around the axis of rotation known as the straight and / or curved segment 65.321 / BE, and characterized in that the vortex bed occupies at least the entire first volume of the reactor. Thus, according to the present invention, the height of the vortex bed (h) is at least equal to the height H of the polymerization reactor. Preferably, the swirl bed occupies at least a portion of the second volume known as the separating vessel.

The Applicant has unexpectedly found that polymer particles do not leave the reactor in large quantities during the process of the present invention. Although we do not wish to be bound by the following explanation, it is believed that this is due, firstly, to the fact that when they reach the separating vessel, the particles slow down and, on the other hand, the size of the bubbles is limited and / or reduced when they enter the separating vessel.

While it is not intended to limit the invention to a single specific type of polymerization, the present invention is particularly suitable for the polymerization reaction of one or more monomers such as olefins, polar vinyl monomers, dienes, acetylenes and aldehydes.

The process of the present invention is preferably used to polymerize one or more olefin monomers such as ethylene, propylene, 1-butene, 1-pentene, 4-methyl-1-pentene, 1-hexene and 1-octene.

According to the present invention, it is possible to determine that the polymerization is carried out temporarily with a bed height according to the invention and a bed height lower than that of the present invention. However, it is preferred that the polymerization be carried out in the constant bed height range of the present invention

65.321 / BE ι

finally .

As mentioned above, the height of the polymerization reactor H is determined by the distance between the bottom of the swirl bed, which generally coincides with the fluidizing grid, and the lower or lower volume, and the second volume called the separating vessel. Thus, in the case of the preferred vertical axis cylinder, the H value is the length of the vertical wall of the cylinder rising above the bottom of the swirl bed.

In a preferred embodiment of the present invention, the height of the vortex (h) is greater than the height of the reactor H, preferably greater than 1.05 χ H, in particular 1.1 χ H.

The separating vessel mounted above the roll containing the vortex bed is, in principle, larger in cross-section than the cylinder. Its shape is a pear-shaped, substantially rotating cylindrical truncated cone whose axis coincides with the axis of the cylinder, the tip of which is pointing downwards at an angle of 10-60 °, its vault being hemispherical. The lower base (bottom) of this truncated cone with the upper end of the cylinder of the reactor and its larger base (top) coincides with the base of the vault. It may also consist of a vertical cylinder attached to a cylindrical cylinder for accommodating a vortex bed with an expanded wire-shaped connecting surface. In this case, the roller has a vertical axis coinciding with the axis of the roller for receiving the vortex bed, and its top is substantially hemispherical.

In a preferred embodiment of the present invention, the height of the vortex (h) is such that the volume of the separating vessel occupied by the vortex bed is equal to the total volume of the vessel.

65 321 / BE

- more than 5%, preferably more than 10%, more preferably more than 15%.

In a preferred embodiment of the present invention, the height of the vortex bed (h) is such that the volume of the separating vessel occupied by the vortex bed is less than 70%, preferably less than 50%, more preferably less than 70% of the total volume of the vessel. 30%.

In the case where the vessel is in the form of a truncated cone having an attached cup tip, the upper limit of the vortex bed is less than the height corresponding to the largest orthogonal section of said vessel. This height limit is a

Figure 2 illustrates the size of L.

The presence of fine particles in the reactor can affect the properties of the polymer by increasing the gel content of the finished product as the films and vessels made of plastic. In addition, agglomerates may form on the inner wall of the reactor, particularly on the wall of the separating vessel during polymerization. Accumulation of fine-grained material and agglomerate on the wall can lead to blockage of the reactor.

In order to prevent the blockage of the reactor, which affects the operation of the polymerization system and the quality of the polymer produced, the reactor is stopped at regular intervals to clean the walls and remove the agglomerates. This can be done under pressure with water or nitrogen. This type of cleaning causes poison to enter the reactor and this automatically results in rinsing and drying the reactor to remove these poisons. This operation is time consuming and not

65.321 / BE, · ·· · · remove these poisons. This operation is time consuming and not very economical.

Unexpectedly, it has been found that the method of the present invention makes it possible to reduce and / or eliminate the problems associated with the blockage of the reactor, particularly with respect to the wall of the separating vessel.

Figure 2 is a schematic diagram of a gas phase olefin polymerization apparatus of the present invention. The equipment consists of:

(i) a vortex reactor 1 comprising a dome 2 and a fluidizing grid 4, consisting of a vertical sidewall cylinder mounted above a damping or separating chamber 3, the top of which forms the dome, (ii) a reaction from a gas mixture feed chamber 9; which is located below the grid 4 and passes through the grid 4 of the cylindrical portion of the reactor 1, and (iii) an outer conduit 5 for circulating the reaction gas mixture, connecting the reactor dome 2 with the gas mixture feed chamber 9; comprising a compressor 8 and at least one heat exchanger 6, 7.

One or more supply lines 10 may be connected to the outer circulation line 5 at one or more locations along it, as one or more olefins, such as ethylene or propylene, or α-olefins having 4 to 10 carbon atoms, one or more, preferably non-conjugated dienes. , hydrogen or one or more carbon monoxide, such as nitrogen or alkane having 1 to 6 carbon atoms, preferably 2 to 5 carbon atoms.

Another object of the present invention is a process for gas phase olefins

65 321 / BE

in a reactor with a chan- nically mixed bed, consisting of a vertical sidewall cylinder and a waveguide or separating chamber 3 mounted thereon, the process being carried out continuously or periodically by feeding the catalyst to the reactor, the reaction through the upstream flow into the gas mixture is continuously olefinized (s) are introduced, the polymerization heat is discharged by cooling the gas mixture of the recycled reaction, the polymer produced is drained, characterized in that the vortex bed fills at least the reactor's vertical wall cylinder. The swirl bed preferably also fills at least partially the said separating vessel.

The process of the invention is particularly suitable for the production of polyolefin powders, including high or low density, for example, linear polyethylene or polypropylene having a relative density of 0.87 to 0.97. In particular, the polymers produced by the present process are D. Geldart: "Gas Fluidization Technology, John-Wiley and Sons." (A Wiley-Interscience Publication, 33-46). (1986) p. The polymers may consist of particles having a weight average diameter of 300-2000, preferably 500-1500 μπ.

The gas phase continuous polymerization of the olefin (s) is carried out in a conventional manner in a fluidized and optionally mechanically mixed bed reactor, wherein the absolute pressure P x may be 0.5-6, preferably 1-4 MPa. The temperature of the vortex bed is lower than the melting point of the polymer, for example from 30 ° C to 130 ° C, preferably from 50 ° C to 110 ° C.

65.321 / BE •. · -W »» «· ·· · · ··· ......

··.:. . · · · »·

- 10 can be held. The reaction mixture is 0.3-1 m / sec, preferably 0.4-0.8 m / sec. passes upwards in the reactor. The reaction is a gas mixture of one or more olefins, especially olefins having 2 to 10 carbon atoms, preferably 2 to 8 carbon atoms, such as ethylene or propylene or a mixture of ethylene and at least one C3-C10, preferably C3-C8, such as ethylene and propylene. butene, 1-hexene, 1-methyl-1-pentene or 1-octene and / or at least one diene such as a non-conjugated diene. It may also contain hydrogen and / or an inert gas such as nitrogen or an alkane, for example pentane having 1 to 6 carbon atoms, preferably 2 to 5 carbon atoms, and / or isopentane. The polymerization process can be carried out in particular according to the method described in PCT 94/28032. Can be carried out in the presence of a catalyst comprising at least one transition metal of groups 4, 5 or 6 of the periodic table of the elements, see FIG. Edited by B. Bruce King, "Encyclopedia of Inorganic Chemistry," by John Wiley & Sons. (1994). In particular, a Ziegler-Natta type catalyst consisting of a solid catalyst comprising a transition metal compound and a co-catalyst of a metal organometallic compound of Group 1, 2 or 3 of the Periodic Table of the elements, such as an organoaluminum compound, may be used. High-activity compounds have been known for many years and are capable of generating a large amount of polymer in a relatively short time, resulting in avoiding the step of removing catalyst residues in the polymer. High-activity catalyst systems are generally from a solid catalyst

65 321 / BE

-lane containing essentially transition metal, magnesium, and halogen atoms. It is also possible to use a high-activity catalyst comprising essentially a heat-activated chromium oxide having a particulate, refractory oxide-based carrier. The polymerization process is very suitable for use with metallocene catalysts such as a titanium or vanadium based metallocene catalyst such as zirconocene, hafnoncene, titanocene or chromocene, or a silica-supported Ziegler catalyst. For example, the metallocene catalyst can be represented by the formula (Cp) m MRxRly wherein Cp is a substituted or unsubstituted cyclopentadienyl ring, M is an element of group IV, V or VI of the periodic table of elements such as zirconium, titanium or hafnium, R and R 1 is the same or different and represents a hydrocarbon radical having from 1 to 20 carbon atoms, halogen or other monovalent ligand, m is from 1 to 3, x is from 0 to 3, and y is from 0 Up to 3, provided that m, x and y are equal to the oxidized state of M. Examples of metallocene-type catalysts can be found in EP 0 129 368, EP 0 206794 and US 5 324 800. The catalyst may also be a mono-cyclopentadienyl heteroatom. Such catalysts are described, for example, in EP 0 416 815 and EP 0 420 436. The Ziegler-Natta type, in particular high-activity catalysts, and more particularly the metallocene-type catalysts, are preferably applied to a porous carrier such as a distillate 65.321 / BE ·· · · · ·

It is used in a state of application to 12 stationary oxides such as silica or alumina.

The above-mentioned catalyst or catalyst system may be used directly in the reactor or may be converted into an olefin prepolymer, in particular during a prepolymerization, when the catalyst or catalyst system is contacted with one or more olefins such as the aforementioned olefin in a liquid or gaseous hydrocarbon medium or phase, for example, in a batch or continuous process outside the vortex polymerization reactor.

In a preferred embodiment, it has been found that the present invention is particularly suitable when the polymer yield is greater than 50 kg / h / m, preferably greater than 60.

3 kg / h / m, more preferably greater than 70 kg / h / m, any catalyst system is used.

The process is particularly suitable for powdered polyolefins such as 0.87-0.97 high density or low density polyethylene or polypropylene or propylene ethylene copolymer and / or

With C4-C8 olefin or elastomer with propylene ethylene or with at least one, e.g., 0.85-0.87, relatively low relative density non-conjugated diene.

The process according to the invention has several advantages. Indeed, the process is not only simple, reliable and easy to operate, but also allows for a significant increase in polymer yield.

The new procedure will allow existing plants to improve performance without changing design.

65 321 / BE

- Increase performance without changing 13 outputs.

In addition, it has been found that the process of the present invention reduces the amount of polymer particles discharged from the reactor. This improvement results in a further advantage of the present process, resulting in a higher upstream flow rate of the reaction gas mixture than was previously possible.

The following examples illustrate the present invention.

Examples

Figure 2 shows a gas-phase copolymerization of ethylene and 1-butene in a schematically illustrated apparatus.

The vortex reactor therefore consists of a vertical wall cylinder mounted on top of a vibration breaker or separation chamber. Features include:

- internal diameter of cylinder 1: 5 m,

- Height of cylinder H: 20 m

- volume of cylinder: 393 m 3 ,

- the inner diameter of the separating chamber 3 at the height of Lp: 8.66 m,

- Lp height: 28.61 m

- height of the separating vessel: 12.94 m,

- the total volume of the separating vessel: 403 m 3 ,

- volume of the separating vessel below Lp height: 338 m 3 ,

- height of the separating vessel above the height of the Lp (dome): 65 m 3 .

At the base, the reactor has a fluidizing grid 4 that is

65.321 / BE κ «» · ·

Over 14, a 0.950 relative density ethylene and 1-butene copolymer bed is fluidized in the form of a powder having an average cross-sectional particle size of 750 microns, with 90% by weight of particles having a diameter of between 900 and 1200. The apparent density of the fluidized powder is 300 kg / m 3 .

The reaction gas mixture flows at an absolute pressure of 2 MPa through the vortex bed at 0.6 m / sec. at 92 ° C. 30% by volume of ethylene, 1% by volume of 1-butene, 25% by volume of hydrogen and 44% by volume of nitrogen.

A Ziegler-Natta type catalyst containing titanium, magnesium and halogens is prepared in the form of a prepolymer in the same manner as Example 1 of French Patent Application No. 2 405 961. The catalyst is periodically fed into the reactor through the feed line 11.

Example C

After a start-up phase, when the bed is gradually raised, the bed is stabilized at a height of 17 m, which corresponds to a swirl bed volume of 334 m 3 .

Under these conditions, 21.5 tons / hour (yield: 64 kg / h / m 3 ethylene (1-butene) copolymer) is produced in the form of a powder having the above characteristics.

The polymer yield is then gradually increased from 21.5

33.2 tons / hour for 8 hours, while maintaining the vortex bed volume and hence the height of the 17m whirlpool. We then observe the appearance of hot spots and the formation of deposits that lead to blockage of the reactor.

65 321 / BE

The only way to form agglomerates is to limit the polymer yield to about 2 tonnes per hour (yield rate: 69 hours per hour).

Example 2

After a start-up phase, when the bed is gradually raised, the bed is stabilized at a height of 20 m, which corresponds to a swirl bed volume of 393 m 3 .

Under these conditions, ethylene-1- (butene) copolymer of 25 tons per hour (yield rate: 64 kg / h / m 3 ) was produced in the form of a powder having the above characteristics.

In spite of the legitimate concerns that may have been caused by the release of the particles from the reactor, there was no jamming problem. It has not even been found that the fine particles in the outer circulation line 5 have accumulated compared to Example C1.

The polymer yield is then increased gradually over a period of 8 hours from 25 to 39 tonnes per hour while maintaining this 20 m bed height constant. Subsequently, the formation of agglomerates is observed, which requires limiting the polymer yield to 29 tonnes per hour (yield rate: 74 kg / hr / m).

Example 3

After a starting phase during which the bed is gradually raised, it is stabilized at a height of 23 m. This means that the swirl bed is 3 m high in the separating vessel, which is

65.321 / BE * Κ ·

- 75 m 3 of the volume of 16 vessels.

Under these conditions, ethylene (1-butene) copolymer of 30 tons per hour (yield rate: 64 kg / h / m 3 ) is produced in the form of a powder having the above-mentioned characteristics.

In spite of the justified concerns that might have arisen with the release of the particles from the reactor, there was no plugging problem. It has not even been found that the fine particles in the outer circulation line 5 have accumulated compared to Example C1. In addition, the subsequent examination of the condition of the heat exchangers 6, 7 mounted in the external circulation 5 showed that these heat exchangers are less plugged in Example 3 than in the other two examples.

The polymer yield is then increased gradually over a period of 8 hours from 30 to 46.5 tonnes / hour (yield rate: 99 kg / hr / m 3 ) while maintaining the vortex bed volume and hence the height of the 23 m whirlpool. This happens without problems. No hotplate formation was observed and this allowed the polymerization to continue under these conditions.

65 321 / BE

- · Vt · ν ·· <"·» · »• ·. ϊ *

.....

Claims (7)

  1. PATIENT INDIVIDUAL POINTS
    1. A gas phase polymerization process in a vortex reactor, the first volume of which is defined by a rotation axis formed by rotation about a vertical axis known as the axis of rotation of the straight and / or curved segment, above which a second volume, usually called a separating vessel, is defined. the boundary of which is also determined, at least in part, by rotation about a vertical axis known as the axis of rotation of a straight or curved segment, contemplating that the vortex bed occupies at least the entire first volume of the reactor.
  2. Method according to claim 1, characterized in that the vortex bed occupies a portion of the volume of the separating vessel.
  3. Process according to one of the preceding claims, characterized in that one or more olefin monomers such as ethylene, propylene, 1-butene, 1-pentene, 4-methyl-1-pentene, 1-hexene or 1-octene are polymerized.
  4. Method according to one of the preceding claims, characterized in that the first volume of the polymerization reactor is a vertical axis cylinder H of H height.
  5. A method according to claim 4, characterized in that
    65.321 / BE ·.
    ··
    - 18 is the height of the vortex (h) greater than the height of the reactor H, preferably greater than 1.05 χ H, especially 1.1 χ H.
  6. A process for continuous gas phase polymerization of olefin (s) in a fluidized bed and optionally a mechanically blended bed comprising a vertical sidewall cylinder and a flotation breaker or separation chamber (3) mounted on said roller at an absolute pressure above the atmospheric pressure of a catalyst. Feeding the reactor continuously or intermittently, continuous feeding of olefins (olefins) into the passing reaction mixture, cooling the gas mixture of the recycled reaction by draining the polymer produced, characterized in that the vortex bed occupies at least the vertical side wall cylinder of the reactor.
  7. Process according to claim 6, characterized in that the polymerization is carried out at a production rate greater than 50 kg / h / m, preferably 60 kg / h / m, more preferably 70 kg / h / m 3 .
    65.321 / BE • ·
    KÖZZÉTÉTEU
    EXAMPLE m, PC> 0tZ3,
    65 321 / BE
    1/2
HU9800123A 1997-01-24 1998-01-23 Gas phase polymerization process HU9800123A3 (en)

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HU9800123A2 true HU9800123A2 (en) 1998-12-28
HU9800123A3 HU9800123A3 (en) 2002-01-28

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