U.S. patent application number 10/016843 was filed with the patent office on 2002-05-23 for process and apparatus for the gas-phase polymerization of alpha-olefins.
This patent application is currently assigned to MONTELL TECHNOLOGY COMPANY bv.. Invention is credited to Covezzi, Massimo, Galli, Paolo, Govoni, Gabriele, Rinaldi, Roberto.
Application Number | 20020061264 10/016843 |
Document ID | / |
Family ID | 11372011 |
Filed Date | 2002-05-23 |
United States Patent
Application |
20020061264 |
Kind Code |
A1 |
Govoni, Gabriele ; et
al. |
May 23, 2002 |
Process and apparatus for the gas-phase polymerization of
alpha-olefins
Abstract
Process for gas-phase polymerization carried out in two
interconnected polymerization zones, to which one or more
.alpha.-olefins CH.sub.2=CHR are fed in the presence of catalyst
under reaction conditions and from which the polymer product is
discharged. The process is characterized in that the growing
polymer flows through a first polymerization zone under fast
fluidization conditions, leaves said first zone and enters a second
polymerization zone through which it flows in a densified form
under the action of gravity, leaves said second zone and is
reintroduced into the first polymerization zone, thus establishing
a circulation of polymer around the two polymerization zones. The
novel process allows olefins to be polymerized in the gas phase
with high productivity per unit volume of the reactor without
incurring the problems of the fluidized-bed technologies of the
known state of the art.
Inventors: |
Govoni, Gabriele; (Renazzo,
IT) ; Rinaldi, Roberto; (Mantova, IT) ;
Covezzi, Massimo; (Ferrara, IT) ; Galli, Paolo;
(Ferrara, IT) |
Correspondence
Address: |
Maurice B. Stiefel, Esq.
BRYAN CAVE LLP
245 Park Avenue
New York
NY
10167-0034
US
|
Assignee: |
MONTELL TECHNOLOGY COMPANY
bv.
|
Family ID: |
11372011 |
Appl. No.: |
10/016843 |
Filed: |
December 14, 2001 |
Related U.S. Patent Documents
|
|
|
|
|
|
Application
Number |
Filing Date |
Patent Number |
|
|
10016843 |
Dec 14, 2001 |
|
|
|
08943748 |
Oct 3, 1997 |
|
|
|
08943748 |
Oct 3, 1997 |
|
|
|
08684411 |
Jul 19, 1996 |
|
|
|
Current U.S.
Class: |
422/131 ;
422/132 |
Current CPC
Class: |
C08F 110/06 20130101;
B01J 8/1863 20130101; B01J 19/2435 20130101; C08F 210/16 20130101;
C08F 10/00 20130101; Y10S 526/901 20130101; B01J 8/388 20130101;
C08F 10/00 20130101; C08F 2/001 20130101; C08F 10/00 20130101; C08F
2/34 20130101; C08F 110/06 20130101; C08F 2500/18 20130101; C08F
210/16 20130101; C08F 210/14 20130101; C08F 2500/12 20130101; C08F
2500/08 20130101 |
Class at
Publication: |
422/131 ;
422/132 |
International
Class: |
B01J 008/00 |
Foreign Application Data
Date |
Code |
Application Number |
Jul 20, 1995 |
IT |
MI95A001562 |
Claims
Claims
1. Process for the gas-phase polymerization of .alpha.-olefins
CH.sub.2=CHR, where R is hydrogen or a hydrocarbon radical having
1-12 carbon atoms, carried out in a first and in a second
interconnected polymerization zones, to which one or more of said
.alpha.-olefins are fed in the presence of a catalyst under
reaction conditions and from which the polymer product is
discharged, wherein the growing polymer particles flow through the
first of said polymerization zones under fast fluidization
conditions, leave said first polymerization zone and enter the
second of said polymerization zones through which they flow in a
densified form under the action of gravity, leave said second
polymerization zone and are reintroduced into said first
polymerization zone, thus establishing a circulation of polymer
between the two polymerization zones.
2. Process according to claim 1, wherein said fast fluidization
conditions are established by feeding a gaseous mixture comprising
one or more of said .alpha.-olefins CH.sub.2=CHR to said first
polymerization zone.
3. Process according to claim 2, wherein said gaseous mixture is
fed to said first polymerization zone in a region below the point
of reintroduction of the polymer into said first polymerization
zone.
4. Process according to claim 3, wherein the feeding of said
gaseous mixture is carried out by means of gas distributor
means.
5. Process according to claim 2, wherein the polymer and the
gaseous mixture leaving said first polymerization zone are conveyed
to a solid/gas separation zone and the polymer leaving said
solid/gas separation zone enters said second polymerization
zone.
6. Process according to claim 1, wherein the control of the polymer
circulating between the said two polymerization zones is effected
by metering the quantity of polymer leaving said second
polymerization zone.
7. Process according to claim 1, wherein the polymer produced is
withdrawn continuously from said second polymerization zone.
8. Process according to claim 1, wherein the catalyst components
are fed to said first polymerization zone.
9. Process according to claim 1, wherein any of the reaction zones
is fed with a catalyst in a prepolymerized form.
10. Process according to claim 1, wherein any of the reaction zones
is fed with a catalyst dispersed in a polymer slurry.
11. Process according to claim 1, wherein any of the reaction zones
is fed with a catalyst dispersed in a dry polymer.
12. Process according to claim 5, wherein the gaseous mixture
leaving said solid/gas separation is compressed, cooled and
transferred, if appropriate with addition of make-up monomers, to
said first polymerization zone.
13. Process according to claim 5, wherein part of the gaseous
mixture leaving the solid/gas separation zone is used for
transferring the polymer from said second zone to said first
polymerization zone.
14. Process according to claim 5, wherein part of the gaseous
mixture leaving said solid/gas separation zone is compressed and
transferred to said second polymerization zone in the vicinity of
the region where the polymer leaves said second zone.
15. Process according to claim 12, wherein the gaseous mixture
leaving said solid/gas separation zone is cooled to temperatures
below the dew point.
16. Process according to claim 1, wherein said first polymerization
zone is cooled by external cooling means.
17. Process according to claim 1, wherein the make-up monomer or
monomers are fed in an at least partially condensed form to said
first polymerization zone.
18. Process according to claim 2, wherein the velocity of the
fluidizing gas into said first polymerization zone is between 2 and
15 M/s, preferably between 3 and 8 m/s.
19. Process according to claim 1, wherein the polymer is in the
form of spheroidal particles having mean dimensions of between 0.2
and 5 mm, preferably between 0.5 and 3 mm.
20. Process according to claim 1, wherein the working pressure is
between 0.5 and 10 MPa, preferably between 1.5 and 6 MPa.
21. Process according to claim 1, wherein one or more inert gases
are present in said polymerization zones at partial pressures of
between 5 and 80% of the total pressure of the gases.
22. Process according to claim 21, wherein the inert gas is
nitrogen or an aliphatic hydrocarbon having 2-6 carbon atoms,
preferably propane.
23. Process according to claim 1, wherein an intermediate
polymerization zone, operating with a fluid bed, is interposed
between said first and said second polymerization zones.
24. Apparatus for the gas-phase polymerization of .alpha.-olefins,
comprising: a first vertical cylindrical reactor (20) equipped with
a catalyst feedline (34); and a second vertical cylindrical reactor
(30) equipped with a polymer discharge system (23); the upper
region of said first reactor (20) being connected by a first line
(21) to a solid/gas separator (22) which is in turn connected to
the upper region of said second reactor (30); the lower region of
said second reactor (30) being connected by a second line (31) to
the lower region of said first reactor (20); and said solid/gas
separator (22) being connected by means of a recirculation line for
the gaseous mixture (36) to said first reactor (20) in a region
(37) at the bottom of said first reactor (20) below the point of
entry of said second line (31).
25. Apparatus according to claim 24, wherein said first reactor
(20) is equipped with gas distributor means (33) located between
the point of entry of said second line (31) and said region (37) at
the bottom of said first reactor (20).
26. Apparatus according to claim 24, wherein a first control valve
(24) for controlling the polymer flow rate is interposed between
said second reactor (30) and said second line (31).
27. Apparatus according to claim 26, wherein said first valve (24)
is a mechanical valve.
28. Apparatus according to claim 26, wherein said first valve (24)
is a non-mechanical valve.
29. Apparatus according to claim 25, wherein said catalyst feedline
(34) is connected via a third line (32) to said first reactor (20)
at a point above said gas distributor means (33).
30. Apparatus according to claim 24, wherein said recirculation
line for the gaseous mixture (36) is equipped with a compressor
(26), a cooling system (27) and systems for introducing monomers
(28) and molecular weight regulator (29).
31. Apparatus according to claim 24, wherein said first line (21)
leaves the upper region of said first reactor (20) laterally.
32. Apparatus according to claim 24, wherein the upper region of
said first reactor is of frustoconical geometry with the broad end
uppermost.
33. Apparatus according to claim 30, wherein said recirculation
line for the gaseous mixture (36) is connected, at a point
downstream of said compressor (26), via a line (25) to said second
line (31).
34. Apparatus according to claim 24, wherein said first reactor
(20) is equipped with external cooling means (35).
Description
[0001] The present invention relates to a process for the gas-phase
polymerization of olefins carried out in two interconnected
polymerization zones, to which one or more .alpha.-olefins
CH.sub.2=CHR are fed in the presence of a catalyst under
polymerization conditions and from which the produced polymer is
discharged. In the process of the present invention the growing
polymer particles flow through a first polymerization zone under
fast fluidization conditions, leave said first zone and enter a
second polymerization zone through which they flow in a densified
form under the action of gravity, leave said second zone and are
reintroduced into the first polymerization zone, thus establishing
a circulation of polymer between the two polymerization zones.
[0002] The development of catalysts with high activity and
selectivity of the Ziegler-Natta type and, in more and more
applications, of the metallocene type, has led to the widespread
use on an industrial scale of processes, in which the
polymerization of the olefins is carried out in a gaseous medium in
the presence of a solid catalyst. Compared with the more
conventional technology in liquid suspension (of monomer or of
monomer/solvent mixtures), this technology has the following
advantages:
[0003] a) operational flexibility: the reaction parameters can be
optimized on the basis of the characteristics of the catalyst and
of the product and are not limited by the physico-chemical
properties of the liquid mixtures of the reaction components
(generally including hydrogen as a chain transfer agent);
[0004] b) widening of the product range: the effects of swelling of
the growing polymer particle and of solubilization of polymer
fractions in a liquid medium greatly reduce the range of production
of all the kinds of copolymers;
[0005] c) minimization of the operations downstream of the
polymerization: the polymer is obtained directly from the reactor
in the form of dry solid and requires simple operations for
removing dissolved monomers and deactivating the catalyst.
[0006] All the technologies devised hitherto for the gas-phase
polymerization of .alpha.-olefins provide for maintaining a bed of
polymer, through which the reaction gases flow; this bed is
maintained in suspension either by mechanical stirring (stirred-bed
reactor) or by fluidization obtained by recycling the reaction
gases themselves (fluidized-bed reactor). In both the reactor
types, the monomer composition around the polymer particle in the
reaction is maintained sufficiently constant owing to the induced
stirring. Said reactors approximate very closely the ideal
behaviour of the "continuous stirred-tank reactor" (CSTR), making
it relatively easy to control the reaction and thereby ensuring
consistency of quality of the product when operating under
steady-state conditions.
[0007] What is by now the most widely established industrial
technology is that of the fluidized reactor operating under
"bubbling" conditions. The polymer is confined in a vertical
cylindrical zone. The reaction gases exiting the reactor are taken
up by a centrifugal compressor, cooled and sent back, together with
make-up monomers and appropriate quantities of hydrogen, to the
bottom of the bed thorough a distributor. Entrainment of solid in
the gas is limited by an appropriate dimensioning of the upper part
of the reactor (freeboard, i.e. the space between the bed surface
and the gas offtake), where the gas velocity is reduced, and, in
some designs, by the interposition of cyclones in the exit gas
line.
[0008] The flow rate of the circulating gas is set so as to assure
a fluidization velocity within an adequate range above the minimum
fluidization velocity and below the "transport velocity". The heat
of reaction is removed exclusively by cooling the circulating gas.
The catalyst components are fed in continuously. The composition of
the gas-phase controls the composition of the polymer. The reactor
is operated at constant pressure, normally in the range 1-3 MPa.
The reaction kinetics are controlled by the addition of inert
gases.
[0009] A significant contribution to the reliability of the
fluidized-bed reactor technology in the polymerization of
.alpha.-olefins was made by the introduction of suitably pretreated
spheroidal catalyst of controlled dimensions and by the use of
propane as diluent (see WO 92/21706).
[0010] Fluidized-bed technology has limits, some of which are
discussed in detail below.
[0011] A) Removal of the heat of reaction.
[0012] The maximum fluidization velocity is subject to quite narrow
limits (which already entail reactor volumes for disengagement
which are equal to or greater than those filled by the fluidized
bed). Depending on the heat of the reaction, the polymer dimensions
and the gas density, a limit to the productivity of the reactor
(expressed as hourly output per unit reactor cross-section) is
inevitably reached, where operation with gas inlet temperatures
higher than the dew point of the mixture of the gases is desired.
This limit can lead to reductions in the plant output, in
particular in the copolymerization of ethylene with higher
.alpha.-olefins (hexene, octene), which is carried out with
conventional Ziegler-Natta catalysts, requiring gas compositions
rich in such olefins.
[0013] Many ways of overcoming the limits, in terms of heat
removal, of the traditional technology have been proposed, based on
partial condensation of the circulating gases and on the use of the
latent heat of evaporation of the condensates for controlling the
temperature in the interior of the reactor (see EP-89691, U.S. Pat.
No. 5,352,749, WO 94/28032). Although technically worthy of
consideration, all the systems proposed for implementing the
principle render the operation of the fluidized reactors
critical.
[0014] In particular (and apart from problems associated with the
distribution of wet solids in the plenum below the distribution
grid), the technology used in patents EP-89691 and U.S. Pat. No.
5,352,749 relies on the turbulence generated by the grid to
distribute the liquid over the polymer. Possible coalescence
phenomena in the plenum can give rise to uncontrollable phenomena
of poor distribution of liquid with formation of agglomerates which
can not be redispersed, in particular in the case of polymers which
have a tendency to stick. The discrimination criterion given in
U.S. Pat. No. 5,352,749 reflects situations under steady-state
conditions, but offers no feasible guide for situations of even a
transient "reaction runaway", which can lead to irreversible loss
of fluidization, with a consequent collapse of the reactor.
[0015] The method described in patent WO 94/28032 involves
separation of the condensates and their distribution above the grid
by means of special, suitably located nozzles. In fact, the
condensates inevitably contain solids in reactive conditions, whose
concentration can become very high at low condensate amounts.
Moreover, the inherent difficulty of uniformly distributing a
suspension over a number of nozzles can compromise the operability
of some of them and a blocking in one nozzle adversely affects the
distribution of the liquid evaporating in the relevant section of
the reactor. It is also clear that the efficiency of the operation
depends upon a vigorous circulation of solids in the reactor and,
below the injection points, this is reduced by an unbalancing of
the gas flow rates caused by large quantities of condensates.
Furthermore, any need for maintenance on one nozzle requires a
complete shut-down of the reactor.
[0016] B) Molecular weight distribution
[0017] As already stated, a fluidized bed shows a behaviour
directly comparable with an ideally mixed reactor (CSTR). It is
generally known that, in the continuous polymerization of
.alpha.-olefins in a single stirred stage (which also involves
steady composition of the monomers and of the chain transfer agent,
normally hydrogen) with Ti catalysts of the Ziegler-Natta type,
polyolefins having a relatively narrow molecular weight
distribution are obtained. This characteristic is even more
emphasized when metallocene catalysts are used. The breadth of the
molecular weight distribution has an influence both on the
Theological behaviour of the polymer (and hence the processability
of the melt) and on the final mechanical properties of the product,
and is a property which is particularly important for the
(co)polymers of ethylene.
[0018] For the purpose of broadening the molecular weight
distribution, processes based on several reactors in series, in
each of which it becomes possible to operate at least at different
hydrogen concentrations, have gained industrial importance. A
problem typically encountered also with these processes, when a
very broad molecular weight distribution is required, is an
insufficient homogeneity of the product. Particularly critical is
the homogeneity of the material in blow-moulding processes and in
the production of thin films, in which the presence of even small
quantities of inhomogeneous material brings about the presence of
unfused particles in the film ("fish eyes"). In patent application
EP-574,821, a system of two reactors is proposed which operate at
different polymerization conditions with mutual recirculation of
polymer between the two. Even if the concept is suitable for
solving the problem of the homogeneity of the product, as shown by
the experimental results, such a system involves investment costs
and a certain operational complexity.
[0019] In other cases, polymers of broad molecular weight
distribution are obtained by the use of mixtures of different
Ziegler-Natta catalysts in a single reactor, each catalyst being
prepared so as to give a different response to hydrogen. It is
clear that a mixture of granules each with its own individuality
are obtained at the exit from the reactor. It is difficult to
obtain homogeneity of the product by this route.
[0020] C) Discharge of the product
[0021] The technology of polymerizing .alpha.-olefins in gas-phase
reactors has rapidly developed in the last years, and the range of
polymers obtainable in this way has widened greatly. In particular,
besides homopolymers of ethylene and propylene, a wide range of
copolymers can be produced industrially, for example:
[0022] random copolymers of propylene/ethylene,
propylene/ethylene/higher .alpha.-olefins and propylene/higher
.alpha.-olefins;
[0023] polyethylenes of low and very low density (LLDPE, VLDPE),
modified with higher .alpha.-olefins containing 4 to 8 carbon
atoms;
[0024] heterophasic copolymers of high impact strength, obtained by
growth on the active centres of the catalyst, in successive stages,
of one or more of the polymers listed above and of
ethylene/propylene or ethylene/butene rubbers; and
[0025] EPR and EPDM rubbers.
[0026] In short, in the polymers producible in the gas phase, the
modulus of flexibility varies from 2300 MPa to values lower than
100 MPa, and the xylene-soluble fraction varies from 1% to 80%. The
flowability, compactability and sticking properties turn out to be
extremely variable as a function of the degree of crystallinity, of
the molecular weight and of the composition of the various polymer
phases. Many of these products remain granular and flowable (and
hence processible) as long as they are maintained in a fluidized
state or in flux, which are conditions under which the static
forces between the individual solid particles have no effect. They
tend more or less rapidly to clump together and to form aggregates
if they are allowed to settle or to be compacted in stagnant zones;
this phenomenon is particularly enhanced under reaction conditions
where, due to the combined action of the temperature and the large
quantity of dissolved hydrocarbons, the polymer is particularly
soft, compressible and compactable, and sticky. The
characterization of soft and sticky polymers is efficaciously
described in EP-348,907 or U.S. Pat. No. 4,958,006.
[0027] The most direct solution for the discharge of the polymer
from the reactor consists of a direct discharge from the fluidized
bed through a controlled valve. This type of discharge combines
simplicity with the advantage of not producing stagnant zones.
Where a sufficiently low pressure (in the range 0.5 - 3 bar gauge)
is maintained downstream of the discharge valve, the reaction is
virtually stopped either by the temperature reduction due to the
evaporation of the monomers dissolved in the polymer or due to the
low partial pressure of the monomers in the gas: in this way, any
risk in the receiver equipment downstream of the reactor is
avoided.
[0028] Nevertheless, it is known that the amount of gas discharged
with the polymer from a fluidized bed through an orifice reaches
very high values as a function of the reactor pressure, of the
fluidization velocity, of the density of the solids in the bed,
etc. (see, for example: Massimilla, "Flow properties of the
fluidized dense phase", in "Fluidization", p. 651-676, eds.
Davidson & Harrison, Academic, New York, 1971). High amounts of
gas discharged with the polymer represent both investment costs and
operating costs, it being necessary to recompress this gas in order
to get back to the reactor pressure from the receiver pressure. In
many industrial applications, discontinuous discharge systems have
thus been installed, with interposition of at least two hoppers in
alternating operation. For example, U.S. Pat. No. 4,621,952
describes a discharge system in which the polymer is transferred
intermittently and at high differential pressures from the reactor
to a settling tank. The momentum of the polymer which, during the
filling phase, impinges first on the walls of the settling tank and
then on the bed of polymer compacts the material which loses its
flowability properties. During the filling phase the pressure in
the settling tank rises rapidly to the value of the reactor
pressure and the temperature does not change significantly. The
reaction proceeds adiabatically at high kinetics. With soft and
sticky products, this easily leads to the formation of agglomerates
which cannot be granulated, with consequent difficulties with the
discharge to the receiving tank below. Analogous observations apply
to U.S. Pat. No. 4,703,094.
[0029] The limits of the intermittent system are clearly revealed
by the proposal for complicated continuous systems. Japanese patent
JP-A-58 032,634 provides for the installation of an internal screw
in the reactor for compacting the polymer towards the discharge;
U.S. Pat. No. 4,958,006 proposes the installation of an extruder,
the screws of which are fed directly in the interior of the
fluidized-bed reactor. Apart from the complication and the
difficulty of industrial application, the systems proposed are in
any case altogether inadequate for feeding the polymer to a
subsequent reaction stage.
[0030] A novel polymerization process has now been found, and this
represents a first aspect of the present invention, which allows
olefins to be polymerized in the gas phase with high hourly output
per unit reactor volume without incurring the problems of the
fluidized-bed technologies of the known state of the art. A second
aspect of the present invention relates to an apparatus for
carrying out this process.
[0031] The gas-phase polymerization process of the present
invention is carried out in a first and in a second interconnected
polymerization zones to which one or more .alpha.-olefins
CH.sub.2=CHR, where R is hydrogen or a hydrocarbon radical having
1-12 carbon atoms, are fed in the presence of catalyst under
reaction conditions and from which the polymer produced is
discharged.
[0032] The process is characterized in that the growing polymer
particles flow through the first of said polymerization zones under
fast fluidization conditions, leave said first polymerization zone
and enter the second of said polymerization zones through which
they flow in a densified form under the action of gravity, leave
said second polymerization zone and are reintroduced into said
first polymerization zone, thus establishing a circulation of
polymer between the two polymerization zones.
[0033] As is known, the state of fast fluidization is obtained when
the velocity of the fluidizing gas is higher than the transport
velocity, and it is characterized in that the pressure gradient
along the direction of transport is a monotonic function of the
quantity of injected solid, for equal flow rate and density of the
fluidizing gas. Contrary to the present invention, in the
fluidized-bed technology of the known state of the art, the
fluidizing-gas velocity is maintained well below the transport
velocity, in order to avoid phenomena of solids entrainment and
particle carryover. The terms transport velocity and fast
fluidization state are well known in the art; for a definition
thereof, see, for example, "D. Geldart, Gas Fluidization
Technology, page 155 et seqq., J. Wiley & Sons Ltd., 1986".
[0034] In the second polymerization zone, where the polymer flows
in a densified form under the action of gravity, high values of
density of the solid are reached (density of the solid=kg of
polymer per m.sup.3 of reactor occupied by polymer), which approach
the bulk density of the polymer; a positive gain in pressure can
thus be obtained along the direction of flow, so that it becomes
possible to reintroduce the polymer into the first reaction zone
without the help of special mechanical means. In this way, a "loop"
circulation is set up, which is defined by the balance of pressures
between the two polymerization zones and by the head loss
introduced into the system.
[0035] The invention is described with reference to the attached
figures, which are given for illustrative purposes without limiting
the invention, in which:
[0036] FIG. 1 is a diagrammatic representation of the process
according to the invention,
[0037] FIG. 2 is a diagrammatic representation of a first
embodiment of the process according to the invention, and
[0038] FIG. 3 is a diagrammatic representation of a second
embodiment of the process according to the invention.
[0039] Referring to FIG.1, the growing polymer flows through the
first polymerization zone 1 under fast fluidization conditions
along the direction of the arrow 14; in the second polymerization
zone 2, the growing polymer flows in a densified form under the
action of gravity along the direction of the arrow 14'. The two
polymerization zones 1 and 2 are appropriately interconnected by
the sections 3 and 5. The material balance is maintained by feeding
in monomers and catalysts and discharging polymer.
[0040] Generally, the condition of fast fluidization in the first
polymerization zone 1 is established by feeding a gas mixture
comprising one or more .alpha.-olefins CH.sub.2=CHR (line 10) to
said zone 1; preferably, the feeding of the gas mixture is effected
below the point of reintroduction of the polymer into said first
zone 1 by the use, where appropriate, of gas distributor means,
such as, for example, a distributor grid.
[0041] The velocity of the transport gas into the first
polymerization zone is higher than the transport velocity under the
operating conditions and is preferably between 2 and 15 m/s, more
preferably between 3 and 8 m/s.
[0042] The control of the polymer circulating between the two
polymerization zones can be effected by metering the amount of
polymer leaving the second polymerization zone 2, using means
suitable for controlling the flow of solids, such as, for example,
mechanical valves (slide valve, V-ball valve, etc.) or
non-mechanical valves (L valve, J valve, reverse seal, etc.).
[0043] Generally, the polymer and the gaseous mixture leaving the
first polymerization zone 1 are conveyed to a solid/gas separation
zone 4. The solid/gas separation can be effected by using
conventional separation means such as, for example, a separator of
the inertial type or preferably centrifugal type, or a combination
of the two. The centrifugal separator (cyclone) can be of the
axial, spiral, helical or tangential type.
[0044] From the separation zone 4, the polymer enters the second
polymerization zone 2. The gaseous mixture leaving the separation
zone 4 is compressed, cooled and transferred, if appropriate with
addition of make-up monomers and/or molecular weight regulators, to
the first polymerization zone 1. This transfer can be effected by
means of a recycle line 6 for the gaseous mixture, equipped with
means for the compression 7 and cooling 8 and means for feeding in
the monomers and the molecular weight regulator 13.
[0045] A part of the gaseous mixture leaving the separation zone 4
can be transferred, after having been compressed, to the connection
zone 5 via the line 9, in order to facilitate the transfer of
polymer from the second to the first polymerization zone.
[0046] Preferably, the various catalyst components are fed to the
first polymerization zone 1, at any point of said first
polymerization zone 1. However, they can also be fed at any point
of said second polymerization zone 2. Any type of catalyst used in
the polymerization of olefins can be used in the process of the
present invention, since it is not important for it to be in any
particular physical state, and catalysts in either solid or liquid
form can be used, because, in contrast to the gas-phase processes
of the known state of the art, the process of the present invention
does not necessarily require the use of catalysts in which at least
one component is in a granular form, but can be carried out with
catalysts in which the various components are in solution. For
example, catalysts based on titanium, chromium, vanadium or
zirconium can be used either in supported or unsupported form.
Examples of catalysts which can be used are described in the
patents U.S. Pat. No. 4,748,272, U.S. Pat. No. 4,302,566, U.S. Pat.
No. 4,472,520 and U.S. Pat. No. 4,218,339.
[0047] Particularly suitable are the catalysts of controlled
morphology, which are described in the patents U.S. Pat. No.
4,399,054, U.S. Pat. No. 5,139,985, EP-395,083, EP-553,805,
EP-553,806 and EP-601,525, and in general catalysts capable of
giving polymers in the form of spheroidal particles having a mean
dimension between 0.2 and 5 mm, preferably between 0.5 and 3 mm.
The process of the present invention is moreover particularly
suitable for the use of metallocene catalysts, either in solution
or supported. The various catalyst components can be introduced at
the same point or at different points of the first polymerization
zone.
[0048] The catalyst can be fed in without prior treatment or in a
prepolymerized form. Where other polymerization stages are situated
upstream, it is also possible to feed the polymerization zones with
a catalyst dispersed in a polymer suspension coming from an
upstream bulk reactor, or a catalyst dispersed in a dry polymer
coming from an upstream gas-phase reactor.
[0049] The polymer concentration in the reactive zones can be
monitored by the usual methods known in the state of the art, for
example by measuring the differential pressure between two suitable
points along the axis of the polymerization zones or measuring the
density by nuclear detectors (for example .gamma.-rays).
[0050] The operating parameters such as, for example, the
temperature are those that are usual in gas-phase olefin
polymerization processes, for example between 50.degree. C. and
120.degree. C.
[0051] The process according to the present invention has many
advantages. The loop configuration allows the adoption of
relatively simple reactor geometries. In practice, each reaction
zone can be designed as a cylindrical reactor of high aspect ratio
(height/diameter ratio). From the point of view of construction,
this particular reactor geometry allows the adoption of high
operating pressures, which are not economical in conventional
fluidized-bed reactors. The process according to the present
invention can thus be carried out under operating pressures of
between 0.5 and 10 MPa, preferably between 1.5 and 6 MPa. The
consequent high gas density favours both the heat exchange on a
single particle and the overall removal of the heat of reaction. It
is therefore possible to choose operating conditions which enhance
the reaction kinetics. Moreover, the reactor through which the
polymer flows under fast fluidization conditions (first
polymerization zone) can run completely full at polymer
concentrations which can reach or exceed 200 kg/m.sup.3. With the
contribution of the second polymerization zone and taking account
of the more favourable kinetic conditions which can be established,
the process of the present invention makes it possible to obtain
specific productivities (hourly output per unit volume of the
reactor) which are much higher than the levels obtainable with
conventional fluidized-bed technology. It is thus possible to equal
or even to exceed the catalytic yields of conventional gas-phase
processes, using polymerization equipment of much more limited
dimensions, with a significant saving in the construction cost of
the plant.
[0052] In the process according to the present invention, the
entrainment of solids in the gas recycle line at the exit from the
solid/gas separation zone and the possible presence of liquids
exiting the cooler on the same line do not limit the efficiency of
the first polymerization zone. Even when using gas distributor
means such as, for example, a grid, the transport gas velocities in
the plenum below the grid are still high and such as to ensure the
entrainment of droplets of even considerable dimensions and of
wetted polymer, without stagnant points. Given that the transport
gas comes into contact with the stream of hot polymer arriving from
the second polymerization zone, the vaporization of any liquid is
virtually instantaneous. It is therefore possible to cool the
gaseous mixture leaving the solid/gas separation zone to
temperatures below the dew point in order to condense part of the
gases. The gas/liquid mixture which forms is then fed to the first
polymerization zone where it contributes to heat removal without
encountering the problems and limits of the known state of the art
and without requiring the use of the complicated devices proposed
to avoid them. In addition to and/or in replacement of the partial
condensation of the recirculating gases, the process of the
invention opens a new way to the removal of the heat of reaction.
The characteristic geometry (high surface/volume ratio) of the
polymerization zone with fast fluidization makes a significant
external surface area available for direct heat exchange on this
zone (and hence with maximum heat transfer between cooling liquid
and reaction system). Where convenient, additional or alternative
heat exchange surfaces can be present in the interior of the
reactor. The first polymerization zone can thus be advantageously
cooled with external cooling means. The high turbulence connected
with the fast fluidization conditions and a high gas density assure
in every case a very high heat transfer coefficient. Any
condensation on the internal walls is continuously removed by the
strong radial and axial mixing of the polymer due to the fast
fluidization conditions. Moreover, this characteristic makes the
proposed technology suitable for operation as a second stage fed
directly from an upstream bulk reactor. It is also possible to feed
part of the make-up monomers in a condensed form without any
difficulty. As far as the removal of the heat of reaction is
concerned, the capacities offered by the process of the invention
are superior to those of the known state of the art and the
difficulties inherent in the prior technologies are overcome.
Moreover, the volumetric rates of the circulating gas are not
necessarily dependent upon the requirements of heat exchange.
[0053] Advantageously, one or more inert gases are maintained in
the polymerization zones, in such quantities that the sum of the
partial pressures of the inert gases is preferably between 5 and
80% of the total pressure of the gases. The inert gas can be
nitrogen or an aliphatic hydrocarbon having 2-6 carbon atoms,
preferably propane. The presence of the inert gas has numerous
advantages, for it makes it possible to moderate the reaction
kinetics while at the same time maintaining total reaction
pressures which are sufficient to keep low the head of the
circulation compressor and to assure an adequate mass flow rate for
the heat exchange on the particle in the bed and, through the
cooler on the circulating gaseous mixture, for the removal of the
heat of reaction which has not been removed by the surfaces.
[0054] In the process of the present invention, the presence of the
inert gas has further advantages, inasmuch as it makes it possible
to limit the temperature increase in the second polymerization
zone, which runs in an essentially adiabatic mode, and also makes
it possible to control the breadth of the molecular weight
distribution of the polymer, particularly in the polymerization of
ethylene. This is because, as already stated, the polymer flows
vertically down through the second polymerization zone in plug flow
(packed flow mode), surrounded by limited quantities of entrained
gas. As is known, the molecular weight of the polymer in ethylene
polymerization is controlled by the hydrogen/ethylene ratio in the
gas phase and, to a lesser extent, by the temperature. In the
presence of inerts, given that the reaction consumes ethylene but
hydrogen only to a marginal extent, the ethylene/hydrogen ratio
decreases along the axis of the polymer flow in the direction of
movement, causing growth of polymeric fractions on the same
particle with decreasing molecular weights. The temperature rise
due to the reaction adds to this effect. It is therefore possible,
by means of an appropriate balancing of the gas composition and the
residence times in the two polymerization zones, to control in an
effective manner the broadening of the molecular weight
distribution of the polymers while at the same time maintaining
maximum homogeneity of the product.
[0055] Conversely, if it is desired to produce polymers with a
narrow molecular weight distribution, the mechanism described above
can be restricted or avoided by proper selection of the reaction
conditions, for example by limiting the amount of inert gas or
feeding an appropriate quantity of reaction gas and/or make-up
monomer(s) at suitable positions in the second polymerization zone.
Advantageously, the gas to be fed to the second polymerization zone
can be taken from the gaseous mixture leaving the solid/gas
separation zone, after this has been compressed. The quantity of
gas introduced is preferably fixed within values such that the
relative velocity of the injected gas with respect to the flowing
solid velocity, is kept below the minimum fluidization velocity
characteristic of the solid/gas system present in said second
polymerization zone. Under these conditions, the downward flow of
polymer is substantially not disturbed. The operational flexibility
of the process of the invention is therefore total, the production
of polymers of different molecular weight distribution being
controllable by the gas composition and, if needed, by simple
closing or opening of a valve on a gas line.
[0056] Advantageously, the polymer can be discharged from zones
where the solids density is higher, for example from suitable
points in the second polymerization zone where large amounts of
densified flowing polymer are available, in order to minimise the
quantity of entrained gas. By inserting a controlled valve at a
suitable point upstream of the exit region of the polymer from the
second polymerization zone, it becomes possible continuously to
control the withdrawal of the polymer produced. The amount of gas
accompanying the polymer is extremely small and only slightly
greater than can be achieved by the device of interposing a series
of hoppers in alternating intermittent operation. In this way, all
the limitations of the discharge systems of the known state of the
art are overcome, with respect to both the quantity of entrained
gas and the nature of the discharged products.
[0057] As already stated, the process of the present invention can
be combined with the conventional technologies in a sequential
multi-stage process in which, upstream or downstream of a
polymerization section operated according to the present invention,
there are one or more polymerization stages using conventional
technologies (in bulk or in the gas phase, either in a fluidized
bed or a stirred bed). Multi-stage processes, wherein two or more
stages are carried out with the procedure of the present invention,
are also possible.
[0058] It is moreover possible to combine the process according to
the present invention with the conventional fluidized-bed gas-phase
technologies by interposing, between the two polymerization zones
as defined in the present invention, a polymerization zone using a
fluid bubble bed, i.e. with fluidization gas velocities higher than
the minimum fluidization velocity and lower than the transport
velocity, while always maintaining the loop circulation
characteristic of the process of the present invention. For
example, one possible embodiment provides that the second
polymerization zone consists of a first and a second section. In
the first (with respect to the downward flow of the polymer) of
said sections a fluidized bed is maintained by appropriately
feeding and distributing gases; in the second section,
appropriately connected to the first one, the polymer flows in
densified form by gravity. From the second section the polymer is
reintroduced into the first polymerization zone, maintaining the
loop circulation. With an appropriate dimensioning of the various
zones, it becomes possible to achieve a braodening of the molecular
weight distribution of the polymer, while retaining all the
advantages described above. The above example is only one of the
possible embodiments of the process of the invention, which, in its
general definition, comprises at least a fast fluidization zone
interconnected with a zone where the polymer flows in densified
form by gravity.
[0059] The process of the present invention is applicable to the
preparation of a large number of olefin polymers without the
disadvantages described above. Examples of polymers which can be
obtained are:
[0060] high-density polyethylenes (HDPEs having relative densities
higher than 0.940) including ethylene homopolymers and ethylene
copolymers with .alpha.-olefins having 3 to 12 carbon atoms;
[0061] linear polyethylenes of low density (LLDPEs having relative
densities lower than 0.940) and of very low density and ultra low
density (VLDPEs and ULDPEs having relative densities lower than
0.920 down to 0.880) consisting of ethylene copolymers with one or
more .alpha.-olefins having 3 to 12 carbon atoms;
[0062] elastomeric terpolymers of ethylene and propylene with minor
proportions of diene or elastomeric copolymers of ethylene and
propylene with a content of units derived from ethylene of between
about 30 and 70% by weight;
[0063] isotactic polypropylene and crystalline copolymers of
propylene and ethylene and/or other .alpha.-olefins having a
content of units derived from propylene of more than 85% by
weight;
[0064] heterophasic propylene polymers obtained by sequential
polymerization of propylene and mixtures of propylene with ethylene
and/or other .alpha.-olefins;
[0065] atactic polypropylene and amorphous copolymers of propylene
and ethylene and/or other .alpha.-olefins containing more than 70%
by weight of units derived from propylene;
[0066] poly-.alpha.-olefins, such as, e.g., poly-1-butene,
poly-4-methyl-1-pentene;
[0067] polybutadiene and other polydiene rubbers.
[0068] A further aspect of the present invention relates to an
apparatus for the gas-phase polymerization of .alpha.-olefins. The
apparatus of the invention comprises a first vertical cylindrical
reactor 20 equipped with a catalyst feedline 34, and a second
vertical cylindrical reactor 30 equipped with a polymer discharge
system 23, and is characterized in that: the upper region of the
first reactor 20 is connected by a first line 21 to a solid/gas
separator 22 which in turn is connected to the upper region of the
second reactor 30; the lower region of the second reactor 30 is
connected by a, second line 31 to the lower region of the first
reactor 20; and the solid/gas separator 22 is connected by means of
a recycle line for the gaseous mixture 36 to the first reactor 20
in a region 37 at the bottom of said first reactor 20 below the
point of entry of the second line 31.
[0069] Preferably, the first reactor 20 is equipped with gas
distributor means 33, for example a grid, located between the point
of entry of the second line 31 and the region 37 at the bottom of
this reactor. As an alternative, with reference to Fig. 3, the gas
distributor means in the first reactor 60 can be replaced by a
cylindrical line 65, through which the gas flows at high velocity
and which is connected to the reactor 60 by a frustoconical section
62 whose angle of inclination to the vertical is preferably smaller
than 45.degree. and more preferably between 30 and 10.degree..
Advantageously both the catalyst (thorough line 66) and the polymer
coming from the second reactor 70 through the line 77 can be
conveyed through this frustoconical connection.
[0070] A first valve 24 for controlling the polymer flow rate is
generally inserted between the second reactor 30 and the second
line 31. This valve 24 can be either of the mechanical or of the
non-mechanical type.
[0071] In the case where gas distributor means 33 are present, some
or all the components of the catalyst can advantageously be
injected via a third line 32 into said first reactor 20 at a point
above the gas distributor means.
[0072] Advantageously, the recycle line for the gaseous mixture 36
is equipped with a compressor 26, a cooling system 27 and systems
for introducing, together or separated, monomers 28 and molecular
weight regulator 29. Two cooling systems, one upstream and one
downstream the compressor, can be present.
[0073] Preferably, the first line 21 leaves the upper region of the
first reactor laterally, it having been observed that a lateral
exit of the solid/gas mixture from the first reactor 20 contributes
in a substantial way to the dynamic stability of the entire
reaction system.
[0074] The upper region of the first reactor 20 can have a
cylindrical shape with a diameter equal to that of the reactor or
preferably can be of frustoconical geometry with the broad end
uppermost.
[0075] The first line 21 can be horizontal or have a slope in the
direction of gravity in order to facilitate discharge of polymer
(see the configuration of the line 71 in FIG. 3). The second line
31 can appropriately be inclined downwards and can be connected (at
a point immediately downstream of the first valve 24) via a line 25
to the gas recirculation line 36 at a point downstream of the
compressor 26. In this way, the flow of polymer is assisted by the
stream of gas under pressure coming from the recycle line, avoiding
stagnant zones of polymer in the line itself and at the point of
introduction into the reactor 20.
[0076] The system of connection between the lower regions of the
reactors can also be of the type described in FIG. 3, in which the
circulation of the polymer is obtained by a pneumatic L valve 74
operated by the gas taken from the recycle line through the line
75. The L valve is connected to a line 77 which leads into the
first reactor 60, said line 77 being connected via the line 76 to
the recycle line 81. Through this line, the polymer is carried back
to the interior of the reactor 60 by an appropriate stream of gas
coming from the line 76.
[0077] The first reactor 20 can advantageously be equipped with
external cooling means 35, such as wall heat exchangers.
[0078] Two possible embodiments of the invention are illustrated in
FIG. 2 and in FIG. 3. These embodiments have a purely illustrative
purpose and do not limit the invention.
[0079] With reference to FIG. 2, 20 represents the first reactor
operating under fast fluidization conditions and 30 represents the
second reactor through which the polymer flows in a densified form
under the action of gravity; 21 and 31 are lines connecting the
upper and lower regions of the two reactors; 34 is the catalyst
feedline; 22 is a solid/gas separator; 23 is a polymer discharge
system; 36 is the recycle line for the gaseous mixture which
connects said separator to a region 37 at the bottom of the first
reactor; 24 is a control valve for controlling the polymer flow
rate; 33 is a gas distributor device; 32 is a line for feeding the
catalyst; 26 is a compressor and 27 is a cooling system for the
recycling gas mixture; 28 and 29 are systems for feeding monomers
and molecular weight regulator; 25 is a line which connects the
recycle line 36 to the line 31; 35 is the external cooling system
of the first reactor 20.
[0080] With reference to FIG. 3, 60 represents the first reactor
operating under fast fluidization conditions and 70 represents the
second reactor through which the polymer flows in a densified form
under the action of gravity; 71 and 77 are lines connecting the
upper and lower regions of the two reactors; 66 is the catalyst
feedline; 72 is a solid/gas separator; 73 is the polymer discharge
system; 81 is the recycle line for the gaseous mixture, which
connects said separator 72 to a line 65 connected to the base of
the first reactor 60 by a frustoconical section 62; 74 is an L
valve for controlling the polymer flow rate; 79 is a compressor and
80 is a cooling system for the gaseous recycle mixture; 63 and 64
are feed systems for monomers and molecular weight regulator; 75 is
a line which connects the recycle line 81 to the L valve 74; 76 is
a line which connects the recycle line 81 to the line 77; 78 is a
line which connects the recycle line 81 to a region at the bottom
of the second reactor 70; 61 is the external cooling system for the
first reactor 20.
[0081] The following examples will further illustrate the present
invention without limiting its scope.
EXAMPLES
General Polymerization Conditions.
[0082] Polymerizations were carried out in continuous in a plant
which comprised a precontacting section, where the various catalyst
component were premixed, a prepolymerization section, and a
gas-phase polymerization section carried out in a reactor of the
type described in FIG. 2.
[0083] A solid catalyst component prepared according to the
procedure described in Example 3 of EP-A-395083, triethylaluminum
(TEAL) and a silane compound were precontacted in hexane at
10.degree. C. for 10 minutes in the precontacting vessel. The
activated catalyst was fed to the prepolymerization section were
propylene was polymerized in slurry using propane as dispersing
medium. Monomer feed and residence time were adjusted so as to
obtain the desired prepolymerization yields, in terms of g of
polymer per g of solid catalyst component.
[0084] The prepolymer was continuously fed to the gas phase
polymerization apparatus. The apparatus, which is described with
reference to FIG. 2, consisted of two cylindrical reactors 20 and
30, connected by pipes 21 and 31. Reactor 20 was equipped with a
heat exchanger 35. Fast fluidization in the reactor 20 was achieved
by recycling gas from the gas/solid separator 22 to the bottom of
the reactor 20, via the gas-recycle line 36. No gas-distribution
means were used, the recycle gases being directly fed to a region
37 at the bottom of the reactor 20, below the point of entry of
pipe 31. The gas-recycle line was equipped with a compressor 26 and
a heat exchanger 27. The prepolymer slurry reactor was fed to the
reactor 20 at a point immediately above the point of entry of pipe
31. Circulation of polymer was controlled via a L valve 24 operated
by a stream of gas 25 taken from the recycle line 36. Make-up
monomers were fed to the recycle line 36. The polymer produced was
continuously discharged from the reactor 30, via pipe 23. Total
volume of the apparatus (i.e. reactors 20 and 30 plus connection
zones 21 and 31) was 250 1.
EXAMPLE 1
[0085] Polypropylene was prepared using a catalyst comprising
dicyclopentyl-dimethoxy-silane (DCPMS) as silane compound. In the
gas-phase polymerization step, propane was used as inert gas.
1 Main operating condition. Precontacting step. TEAL/solid
component (wt.) 8 TEAL/DCPMS (wt.) 3 Prepolymerization step. Yield
(g/g) 100 Gas-Phase Polymerization. Temperature (.degree. C.) 85
Pressure (barg) 25 Propylene (% mol) 91 Propane (% mol) 8 Hydrogen
(% mol) 1 Specific productivity (Kg/h .multidot. m.sup.3) 140
Product Characteristics. Bulk Density (kg/l) 0.45
EXAMPLE 2
[0086] Hexene-modified LLDPE was prepared using a catalyst
comprising cyclohexyl-methyl-dimethoxy-silane (CMMS) as silane
compound. In the gas-phase polymerization step, propane was used as
inert gas.
2 Main operating condition. Precontacting step. TEAL/Ti (wt.) 120
TEAL/CMMS (wt.) 20 Prepolymerization step. Yield (g/g) 400
Gas-Phase Polymerization. Temperature (.degree. C.) 75 Pressure
(barg) 24 Ethylene (% mol) 15 1-Hexene (% mol) 1.5 Hydrogen (% mol)
3 Propane (% mol) 80.5 Specific productivity (Kg/h .multidot.
m.sup.3) 80 Product Characteristics. Melt Index E (g/10 min) 1.4
Density (g/cm.sup.3) 0.908
[0087] The above reported temperature was measured at top of the
reactor 30. The dew point of the gaseous mixture at the operating
pressure is 66.degree. C. Cooling fluid was circulated in the heat
exchanger 35 in such a way to obtain a temperature of 63.degree. C.
on the surface of reactor 20. Under these conditions, the gaseous
mixture partially condensed on the wall of the reactor, thus
contributing to remove the heat of reaction. No problems of fouling
occurred during operation.
* * * * *