Density polymerization reactor

Density. The density (crystallinity) of catalyticaHy produced PE is primarily determined by the amount of comonomer ( a-olefin) in ethylene copolymer. This amount is easily controlled by varying the relative amounts of ethylene and the comonomer in a polymerization reactor. In contrast, the density of PE produced in free-radical processes is usually controlled by temperature. 

First, in composites with high fiber concentrations, there is little matrix in the system that is not near a fiber surface. Inasmuch as polymerization processes are influenced by the diffusion of free radicals from initiators and from reactive sites, and because free radicals can be deactivated when they are intercepted at solid boundaries, the high interfacial area of a prepolymerized composite represents a radically different environment from a conventional bulk polymerization reactor, where solid boundaries are few and very distant from the regions in which most of the polymerization takes place. The polymer molecular weight distribution and cross-link density produced under such diffusion-controlled conditions will differ appreciably from those in bulk polymerizations. 

An advantage of this approach to model large-scale fluidized bed reactors is that the behavior of bubbles in fluidized beds can be readily incorporated in the force balance of the bubbles. In this respect, one can think of the rise velocity, and the tendency of rising bubbles to be drawn towards the center of the bed, from the mutual interaction of bubbles and from wall effects (Kobayashi et al., 2000). In Fig. 34, two preliminary calculations are shown for an industrial-scale gas-phase polymerization reactor, using the discrete bubble model. The geometry of the fluidized bed was 1.0 x 3.0 x 1.0 m (w x h x d). The emulsion phase has a density of 400kg/m3, and the apparent viscosity was set to 1.0 Pa s. The density of the bubble phase was 25 g/m3. The bubbles were injected via 49 nozzles positioned equally distributed in a square in the middle of the column. 

The basic properties of mPE, such as the average molecular weight, molecular-weight distribution, or density depend mainly on the structure of the metallocene catalyst and its concentration in the polymerization reactor. They also depend strongly on the polymerization temperature and can be varied by incorporation of co-monomers. The influence of the pressure is only small. 

Figure 3.5 Distribution profile of electron density in an argon DC glow discharge in a plasma polymerization reactor.

Kolhapure and Fox, R. (1999), CFD analysis of micromixing effects on polymerization in tubular low-density polyethylene reactors, Chem. Eng. Sci., 54, 3233-3242. 

Fig. 10 Density (d) and melt flow rate (MFR 190/5) as functions of the ethene stream into the polymerization reactor...

The overall conversion in the loop polymerization reactor is very high for a polyolefin manufacturing process, and the conversion per pass is limited by the amount of monomer that is needed to carry the polymer out of the reactor. It is desirable to operate the reactor at as high a slurry density as possible to get the highest throughput and the highest conversion. Typically, loop reactors operate at slurry concentrations of about 45-50 wt% polymer. 

Another problem related to the polymerization reactors is the possibility of multiple responses. The various operating conditions (various feed concentrations, temperatures, pressmes, speed of catalyst addition) may lead to the obtainment of the same type of polymer (the same molecular weight, density, composition), but with different yields. 

Low-density polyethylene (density = 0.915-0.935 g cm ) has long been manufactured by free-radical polymerization using continuous autoclave reactors. The autoclave reactor shown schematically in Fig. 3a is a typical multizone ethylene polymerization reactor. The reactor is typically a vertical cylindrical vessel with a large LID ratio. The reacting fluid is intensely mixed... 

An independent development of a high pressure polymerization technology has led to the use of molten polymer as a medium for catalytic ethylene polymerization. Some reactors previously used for free-radical ethylene polymerization at a high pressure (see Olefin polymers, low density polyethylene) have been converted to accommodate catalytic polymerization, both stirred-tank and tubular autoclaves operating at 30—200 MPa (4,500—30,000 psig) and 170—350°C (57,83,84). CdF Chimie uses a three-zone high pressure autoclave at zone temperatures of 215, 250, and 260°C (85). Residence times in all these reactors are short, typically less than one minute. 

Gas phase olefin polymerizations are becoming important as manufacturing processes for high density polyethylene (HOPE) and polypropylene (PP). An understanding of the kinetics of these gas-powder polymerization reactions using a highly active TiCi s catalyst is vital to the careful operation of these processes. Well-proven models for both the hexane slurry process and the bulk process have been published. This article describes an extension of these models to gas phase polymerization in semibatch and continuous backmix reactors. 

Figure 1. Typical reactor temperature profile for continuous addition polymerization a plug-flow tubular reactor. Kinetic parameters for the initiator 1 = 10 ppm Ea = 32.921 kcal/mol In = 26.492 In sec f = 0.5. Reactor parameter [(4hT r)/ (DpCp)] = 5148.2. [(Cp) = heat capacity of the reaction mixture (p) = density of the reaction mixture (h) = overall heat-transfer coefficient (Tf) = reactor jacket temperature (r) = reactor residence time (D) = reactor diameter].

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