Source: http://www.google.com/patents/US7993591?dq=oakley+5,387,949
Timestamp: 2016-05-04 09:13:27
Document Index: 514892684

Matched Legal Cases: ['Application No. 200809160', 'Application No. 200809157', 'Application No. 200809158', 'Application No. 200809159', 'Application No. 2008709161', 'Application No. 201004966', 'Application No. 200809157', 'Application No. 200809158', 'Application No. 200809159', 'Application No. 200809161']

Patent US7993591 - Spouted bed device and polyolefin production process using the same - Google PatentsSearch Images Maps Play YouTube News Gmail Drive More »Sign inPatentsA spouted bed device of the present invention includes a cylinder which extends vertically; a closing plate which closes a top end of the cylinder; a decreasing diameter member which is formed at a bottom end of the cylinder, has an inside diameter that decreases progressively downward, and has a gas...http://www.google.com/patents/US7993591?utm_source=gb-gplus-sharePatent US7993591 - Spouted bed device and polyolefin production process using the sameAdvanced Patent SearchPublication numberUS7993591 B2Publication typeGrantApplication numberUS 12/332,102Publication dateAug 9, 2011Filing dateDec 10, 2008Priority dateDec 11, 2007Fee statusPaidAlso published asCN101455954A, CN101455954B, DE102008061427A1, US20090149620Publication number12332102, 332102, US 7993591 B2, US 7993591B2, US-B2-7993591, US7993591 B2, US7993591B2InventorsHideki Sato, Hiroyuki OgawaOriginal AssigneeSumitomo Chemical Company, LimitedExport CitationBiBTeX, EndNote, RefManPatent Citations (84), Non-Patent Citations (33), Referenced by (1), Classifications (27), Legal Events (2) External Links: USPTO, USPTO Assignment, EspacenetSpouted bed device and polyolefin production process using the same
US 7993591 B2Abstract
Spouted bed devices which employ a spouted bed have the advantage that all the particles, even relatively large particles several millimeters in size that require an excessively high gas velocity for fluidization in a fluidized bed, circulate and are thoroughly mixed. As used herein, “spouted bed” refers to a state characterized by the circulatory movement of particles wherein, under the action of a gas introduced at a high velocity from a gas inlet orifice provided at the bottom end of a cylindrical vessel, there forms a spout (sometimes referred to below as the “spout portion”) which has a dilute particle concentration near the center axis of the particle bed held within the vessel and in which particles flow upward together with the gas, and there also forms at the periphery of the spout an annular particle bed where particles fall in a moving bed state under the influence of gravity.
It is known that there remains room for improvement in spouted bed devices from the standpoint of the solid-gas contact efficiency between the particles and the gas. One means for enhancing the solid-gas contacting efficiency between the particles and the gas while maintaining the excellent mixing properties of a spouted bed, described by K. Takeda and H. Hattori in “Spouted bed device provided with gas outlet in sidewall” (Kagaku Kogaku Ronbunshu 1, No. 2, 149-154 (Kagaku Kogaku Kyokai, 1975), involves providing a gas outlet in the sidewall of the cylindrical vessel in which the spouted bed is formed.
However, because the gas outlet in the spouted bed device described by K. Takeda et al. was formed in the sidewall of a region where the annular particle bed portion of the spouted bed is formed, many particles ended up being discharged from this discharge outlet together with the gas. Hence, there arose a need to install an auxiliary apparatus of substantial size such as a filtration unit to prevent the discharge of particles or a recovery unit for recovering discharged particles.
The polyolefin production process of the present invention entails carrying out olefin polymerization by using either of the inventive spouted bed devices described above to form a spouted bed of polyolefin particles within the treatment zone. In particular, when the above-described multistage-type spouted bed device is used, it is preferable to carry out olefin polymerization by feeding to at least one treatment zone a second type of gas that differs from a first type of gas fed to the other treatment zones. By employing such a method, it is possible, for example, to efficiently produce multistage-polymerized propylene-based copolymers which have crystalline propylene-based polymer segments and amorphous propylene-based polymer segment, are called “high-impact polypropylene” (in Japan, also customarily called “polypropylene block copolymers”).
FIG. 1 is a schematic view of a first embodiment of the spouted bed device according to the present invention;
The deflector 20 and the tubular baffle 30 are each attached to the cylinder 12A by supports (not shown). The supports have substantially no influence on gas flow and polyolefin flow. The cylinder 12A, deflectors 20 and tubular baffles 30 may be made of, for example, carbon steels and stainless steels such as “SUS 304” and “SUS 316L”. As used herein, “SUS” refers to a stainless specification standardized by Japanese Industrial Standards (JIS). It is preferable to use “SUS 316L” when a catalyst which are high in corrosive ingredient (e.g., a halogen such as chlorine) is to be employed.
Accordingly, in the present embodiment, a polymerization step which uses two reactors—i.e., an olefin prepolymerization reactor 5 and an olefin polymerization reactor 10A—is achieved. In this way, the olefin prepolymerization reactor 5 effects the polymerization and growth of polyolefin particles, creating relatively large polyolefin particles having a particle size of preferably at least 500 μm, more preferably at least 700 μm, and even more preferably at least 850 μm, thereby enabling the formation of a more stable spouted bed. However, it is also possible to have the polymerization step be one which uses only a single reactor and does not include an olefin prepolymerization reactor 5. In this case, an olefin polymerization catalyst or prepolymerization catalyst is fed directly to the olefin polymerization reactor 10A, and olefin polymerization is carried out. Alternatively, one or more additional olefin polymerization reactor, such as an olefin prepolymerization reactor 5 or an olefin polymerization reactor 10A, may be provided subsequent to the olefin polymerization reactor 10A so as to achieve a polymerization step having three or more stages.
In the olefin polymerization reactors and polyolefin production methods according to the present embodiment, polyolefin—i.e., olefin polymer (olefin homopolymer, olefin copolymer)—production is carried out by the polymerization of one or more olefin (homopolymerization or copolymerization). Examples of olefins that may be used in the present embodiment include ethylene, propylene, 1-butene, 1-pentene, 4-methyl-1-pentene, 5-methyl-1-hexene, 1-hexene, 1-heptene and 1-octene.
Examples of such polymers include propylene-propylene/ethylene polymers, propylene-propylene/ethylene-propylene/ethylene polymers, propylene/ethylene-propylene/ethylene polymers and propylene-propylene/ethylene/1-butene polymers. Here, a dash (“-”) indicates the boundary between polymers, and a slash (“/”) indicates that two or more olefins are copolymerized within the polymer. Of these, the production of multistage-polymerized propylene-based copolymers which are polymers having propylene-based monomer units, are called “high-impact polypropylene” (in Japan, also customarily called “polypropylene block copolymers”), and have crystalline propylene-based polymer segments and amorphous propylene-based polymer segments, is preferred. A multistage-type polymerized propylene-based copolymer can be prepared by the continuous multistage polymerization, in any order, of crystalline homopolypropylene segments or random copolymer segments obtained by copolymerizing a small amount of an olefin other than propylene, with amorphous rubber segments copolymerized from ethylene, propylene and, as an optional ingredient, an olefin other than ethylene and propylene, in the presence of the respective polymers. Such a copolymer has an intrinsic viscosity, as measured in 1,2,3,4-tetrahydronaphthalene at 135� C., which is preferably in a range of from 0.1 to 100 dl/g. This multistage polymerized polypropylene-based copolymer has excellent heat resistance, rigidity and impact resistance, and can therefore be used in automotive components such as bumpers and door trim, and in various packaging containers such as retortable food packaging containers.
The olefin polymerization catalyst used in the present embodiment may be a known addition polymerization catalyst used in olefin polymerization. Illustrative examples include Ziegler-type solid catalysts formed by contacting a solid catalyst component containing titanium, magnesium, a halogen and an electron donor (referred to below as “catalyst component A”) with an organoaluminum compound component and an electron donor component; and metallocene-type solid catalysts prepared by supporting a metallocene compound and a cocatalyst component on a granular carrier. Combinations of these catalysts may also be used.
The polyolefin production system 100B according to a second embodiment of the invention, aside from employing an olefin polymerization reactor 10B which forms a plurality of spouted beds 8 instead of the olefin polymerization reaction 10A which forms a single spouted bed 8, has a construction similar to that of the polyolefin production system 100A according to the first embodiment of the invention. The following explanation of the second embodiment deals principally with those features that differ from those in the above-described first embodiment.
Examples 1 to 4 and Comparative Examples 1 to 4 were carried out so as to evaluate the solid-gas contacting efficiency between particles and gases in the annular particle bed portion of the spouted bed that is formed within the treatment zone. Evaluation of the solid-gas contacting efficiency between particles and gases was carried out by comparing the ratio Ua/Umf obtained by dividing the gas flow rate within the annular particle bed (Ua) by the minimum fluidization velocity of the particles (Umf).
A cylindrical cold model reactor made of transparent vinyl chloride resin and capable of forming a single spouted bed in the cylinder (height, 1,100 mm) was furnished. This reactor had, disposed within the cylinder, a single tubular baffle of inverted conical shape with a gas inlet orifice therein and, paired with the baffle, a single deflector of conical shape. The cylinder was closed at the top end with a closing plate, and a plurality of gas introducing nozzles were formed at the top, enabling gases to be discharged laterally from these gas discharge nozzles. More specifically, the cylinder had four gas discharge nozzles, each with an inside diameter of 100 mm, located at positions 100 mm below the top of the cylinder. These gas discharge nozzles were disposed at substantially equal intervals in the circumferential direction of the cylinder.
Aside from setting the flow rate of the gas introduced into the unit to 4.0 m3/min instead of 3.3 m3/min, the same procedure was carried out as in Example 1 and the gas flow velocity in the annular particle bed of the spouted bed was calculated. As a result, the gas flow velocity in the annular particle bed of the spouted bed was 0.15 m/s, which was 0.75 as high as the minimum fluidization velocity.
Aside from setting the flow rate of the gas introduced into the unit to 4.7 m3/min instead of 3.3 m3/min, the same procedure was carried out as in Example 1 and the gas flow velocity in the annular particle bed of the spouted bed was calculated. As a result, the gas flow velocity in the annular particle bed of the spouted bed was 0.16 m/s, which was 0.80 as high as the minimum fluidization velocity.
Aside from setting the flow rate of the gas introduced into the unit to 5.4 m3/min instead of 3.3 m3/min, the same procedure was carried out as in Example 1 and the gas flow velocity in the annular particle bed of the spouted bed was calculated. As a result, the gas flow velocity in the annular particle bed of the spouted bed was 0.16 m/s, which was 0.80 as high as the minimum fluidization velocity.
Instead of discharging gases laterally from four gas discharge nozzles formed in the cylinder, all the gas discharge nozzles were blocked, in addition to which a closing plate was not used and the top of the cylinder was opened up so as to discharge gas upward. Aside from these changes, the same procedure was carried out as in Example 1 and the gas flow velocity in the annular particle bed of the spouted bed was calculated. As a result, the gas flow velocity in the annular particle bed of the spouted bed was 0.13 m/s, which was lower than the value obtained in Example 1 and 0.65 as high as the minimum fluidization velocity.
Instead of discharging gases laterally from four gas discharge nozzles formed in the cylinder, all the gas discharge nozzles were blocked, in addition to which a closing plate was not used and the top of the cylinder was opened up so as to discharge gas upward. Aside from these changes, the same procedure was carried out as in Example 2 and the gas flow velocity in the annular particle bed of the spouted bed was calculated. As a result, the gas flow velocity in the annular particle bed of the spouted bed was 0.11 nm/s, which was lower than the value obtained in Example 2 and 0.55 as high as the minimum fluidization velocity.
Instead of discharging gases laterally from four gas discharge nozzles formed in the cylinder, all the gas discharge nozzles were blocked, in addition to which a closing plate was not used and the top of the cylinder was opened up so as to discharge gas upward. Aside from these changes, the same procedure was carried out as in Example 3 and the gas flow velocity in the annular particle bed of the spouted bed was calculated. As a result, the gas flow velocity in the annular particle bed of the spouted bed was 0.12 m/s, which was lower than the value obtained in Example 3 and 0.60 as high as the minimum fluidization velocity.
Instead of discharging gases laterally from four gas discharge nozzles formed in the cylinder, all the gas discharge nozzles were blocked, in addition to which a closing plate was not used and the top of the cylinder was opened up so as to discharge gas upward. Aside from these changes, the same procedure was carried out as in Example 4 and the gas flow velocity in the annular particle bed of the spouted bed was calculated. As a result, the gas flow velocity in the annular particle bed of the spouted bed was 0.12 m/s, which was lower than the value obtained in Example 4 and 0.60 as high as the minimum fluidization velocity.
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No. 12/332,055.32Weickert et al., "New Reactor Concepts for the Gas-Phase Polymerization of Olefins," Chemie lngenieur Technik, vol. 77, No. 8, 2005, pp. 977-978.33Yokokawa, "Fluidizing characteristics of fluidized bed, and spouted bed, and their application", Journal of the Society of Powder Technology, vol. 21, No. 11, Nov. 1984, pp. 715-723.Referenced byCiting PatentFiling datePublication dateApplicantTitleUS9278314Sep 19, 2013Mar 8, 2016ADA-ES, Inc.Method and system to reclaim functional sites on a sorbent contaminated by heat stable saltsClassifications U.S. Classification422/129, 526/348, 526/65, 422/141, 422/139, 422/140, 422/142International ClassificationB01J10/00, C08F210/00, B01J8/18, C08F2/00Cooperative ClassificationB01J8/1827, B01J8/1872, C08F10/00, B01J8/245, B01J8/0045, B01J8/388, B01J2208/00274, B01J2208/0084, B01J8/28European ClassificationB01J8/38D4, B01J8/00F12, B01J8/28, B01J8/24B, B01J8/18G2, B01J8/18L, C08F10/00Legal EventsDateCodeEventDescriptionFeb 18, 2009ASAssignmentOwner name: SUMITOMO CHEMICAL COMPANY, LIMITED, JAPANFree format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNORS:SATO, HIDEKI;OGAWA, HIROYUKI;REEL/FRAME:022274/0515Effective date: 20081209Jan 21, 2015FPAYFee paymentYear of fee payment: 4RotateOriginal ImageGoogle Home - Sitemap - USPTO Bulk Downloads - Privacy Policy - Terms of Service - About Google Patents - Send FeedbackData provided by IFI CLAIMS Patent Services