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Publication numberUS2568400 A
Publication typeGrant
Publication dateSep 18, 1951
Filing dateSep 18, 1946
Priority dateSep 18, 1946
Publication numberUS 2568400 A, US 2568400A, US-A-2568400, US2568400 A, US2568400A
InventorsKenneth K Kearby
Original AssigneeStandard Oil Dev Co
Export CitationBiBTeX, EndNote, RefMan
External Links: USPTO, USPTO Assignment, Espacenet
Process for subdividing solid particles
US 2568400 A
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Description  (OCR text may contain errors)

Patented Sept. 18, 1951 PROCESS FOR SUBDIVIDING SOLID PARTICLES Kenneth K. Kearby, Cranl'ord, N. J., assignor to Standard Oil Development Company, a corporation of Delaware Application September 1a, 1946, Serial No. 697,810

3 Claims.

The present invention is concerned with'an improved process for subdividing solid particles. The invention more particularly relates to an improved process for finely dividing or pulverizing carbonaceous solid particles, as for example coal, which pulverized particles are subsequently handled to produce gaseous products, as for example gaseous fuels, feed gases suitable for hydrocarbon synthesis reactions, and the like. In accordance with my invention, I employ a standpipe arrangement which is of sufficient height to secure the desired fluid head necessary to inject the particles to be finely divided into a high pressure fluid stream. The fluid stream containing the solid particles to be pulverized is then passed through a jet pulverizing means.

It is known in the art to pulverize or finely divide solid materials, for example, carbonaceous materials, such as coal and the like, by passing a stream of the material through a jet arrangement in which the pressure is reduced resulting in the pulverization of the material. How ver one disadvantage of these processes is that no satisfactory continuous method of introducing the solid particles into the fluid stream such as steam or air, has been obtained. Various suggestions have been made and attempts directed toward overcoming this problem and securing a satisfactory method of continuously introducing the carbonaceous particles into the fluid stream. These efforts have not however been very successful.

I have now discovered a method of incorporating solid material into the fluid stream which is entirely satisfactory and which may be operated in .a continuous manner. In accordance with my invention I employ a fluidized zone of sufllcient height to secure thedesired fluid head. From the bottom of my standpipe arrangement, I introduce suspended fluid solid particles into the fluid stream as for example steam, and then pass this high pressure stream through a jet arrangement in which the pressure is substantially reduced resulting in the pulverization of the solid material.

The process of my invention may be readily understood by reference to the attached drawing illustrating a modification of the same. For the purpose of illustration the operation described with respect to the drawing is assumed to be a coal pulverization process. Referring specifically to the drawing carbonaceous solid material, as for example coal, is introduced into hopper arrangement III by means of conveyor line or equivalent means I. The feed coal falls downwardly in zone It and contacts upflowlng suspending gases which are introduced into zone ID by means of line 2 and distributed throughout the zone by distributing means 3. The velocity of the upflowing gases is sufllcient to maintain the solid particles in a fluid ebullient state, the upper level of which is at point A. The velocity of upfiowing gases is generally in the range from about 0.5 to 2.0 ft./sec. Although the size of the solid particles introduced into zone l0 may vary considerably, for the purpose of illustration, it is assumed that these particles have a, particle size in the range from about 20 to mesh. Additional suspending gases may be introduced if necessary at points i. The suspending gases pass upwardly through zone l0 and are withdrawn by means of line 5 after passing through a cyclone or equivalent separating means '6. Entrained solid. particles separated in cyclone separator t are returned to the bed by means of line I. Larger particles which are not suspended fall past distributing means 3 and are removed from zone I0 by means of line '8. These particles may be passed through mechanical crushing means 9 and recycled to the top of zone it by means of line H. These larger particles may also be withdrawn from the system by means of line l2.

In accordance with my process, I withdraw fluidized particles from zone It through standpipe arrangement it which is shown as a broken conduit to indicate that its length may vary appreciably. The suspended coal particles having a fluid head proportional to the size of th particles, the density of the particles per cubic foot, and the length of the standpipe itself are introduced into line It through which gaseous fluids are passed. For the purpose of illustration, the gaseous fluid passed through line I comprises steam. The steam containing the fluidized coal particles is passed through jet arrangement l5 positioned in pulverizing zone 20. As the gases pass through jet arrangement 15 the pressure on the gases and on the coal is substantially reduced resulting in the pulverization of the coal. The suspending gases and the pulverized coal pass upwardly through cyclone separator or equivalent means l6 positioned in the upper section of zone 20. The steam and the finely divided coal particles are withdrawn from zone 20 by means of line H and may be handled in any manner desirable. Larger particles removed from the suspending gases in cyclone separator [6 are withdrawn by means of line It and preferably recycled to the top of zone In by any suitable conveying means. Larger particles which are not pulverized as they pass through jet arrangement I! are collected in the bottom 01' zone 20 and removed by means of line I 9. These particles are likewise recycled to the top of zone Hi.

My process may be applied to any operation wherein it is desired to flnely divide solid pargreater than the pressure within the line into a which the fluidized solids are being fed. This, as pointed out previously, will depend upon the particular solids being fluidized, the pounds per cubic foot, and the height of the standpipe itself. In a process designed for the pulverizatioh of coal it is preferred that the pressure in the steam line be in the range from about 60 to 100 pounds per sq. inch, and that pressures in the expansion zone after the jet be about atmospheric pressure. Under these conditions the height of the standpipe will be in the range from about l'to 200 it.

If the particles introduced into zone are relatively large it may be necessary to introduce flner particles in order to secure adequate particle size distribution. These finer particles may be secured from an external source and introduced by means of line '21, but are preferably 7 secured by segregating a portion of the particles withdrawn from zone 20 and introducing these pulverized particles into zone I0 by means of line 22.

It is to be understood that the apparatus may be modified. For example, line l3 may be lowered within zone 10 so that coarse material would be allowed to fall downwardly through the bed in zone l0, be withdrawn from the bottom of zone III by means of line l3 and passed through jet arrangement as described. It is also within the concept of my invention to employ a downwardly moving bed in zone In of larger nonfluidized particles with fluidized solid particles interspersing between the interstices of the larger particles. In other words, the bed within zone l0 would comprise nonfiuidized solid particles and fluidized solid particles in which all particles were moving downwardly. The only requirement is that no particles would be too large so that it could not pass through the jet. It is also within the scope of m invention to pass the solids to be pulverized directly to jet means 15.

The process or my invention is not to .be limited by any theory as to mode of operation, but only in and by the iollowing claims in which it is desired to claim all novelty insofar as the prior art permits.

Y I claim:

1. Process for dividing solid particles whic h comprises introducing said particles into a hopper zone, maintaining said particles in said hopper zone in a fluidized state, whereby the larger of said particles segregate at the bottom or said hopper zone, withdrawing said larger particles from the bottom of said hopper zone, mechanically breaking the same and returning the same to an upp r point or said hopper zone, withdrawing fluidized particles from an intermediate point in said hopper zone, introducing said particles into a fluid stream, maintaining said fluid stream under pressure, passing said fluid stream and said introduced solid particles through a jet positioned in a pulverizing zone under conditions to substantially reduce the pressure on said fluid stream whereby said solid particles are subdivided.

2. Process as defined by claim 1 wherein said particles are carbonaceous particles.

3. Process as defined by claim 1 wherein said particles comprise coal particles, and wherein said fluid stream comprises steam.

rcamwrn x. KEARBY.

REFERENCES CITED The following references are 01. record in the file of this patent:

UNITED STATES PATENTS Number Name Date 1,539,401 Neuburger May 26, 1925 1,616,547 Pontoppidan Feb. 8, 1927 1,875,531 Walton Sept. 6, 1932 1,922,313 Mason Aug. 15, 1933 2,032,827 Andrews Mar. 3, 1936 2,237,091 Stephanofl Apr. 1, 1941 2,272,564 Kuever Feb. 10, 1942 2,311,564 Munday Feb. 16, 1943 2,327,175 Conn Aug. 17, 1943 2,341,193 Scheineman Feb. 8, 1944 2,379,027 Monro June 26, 1945 2,392,866 Stephanofi Jan. 15, 1946 FOREIGN PATENTS Number Country Date 216,476 Switzerland Dec. 1, 1941 546,088 Great Britain June 26, 1942 591,921 Great Britain Sept. 2, 1947

Patent Citations
Cited PatentFiling datePublication dateApplicantTitle
US1539401 *Feb 21, 1925May 26, 1925Jacob NeuburgerPulverizing machine
US1616547 *Apr 3, 1926Feb 8, 1927Smidth & Co As F LHandling dry pulverulent materials
US1875531 *Mar 1, 1930Sep 6, 1932 Pboduction of abrasive floubs
US1922313 *Jun 27, 1931Aug 15, 1933Masonite CorpProcess and apparatus for disintegration of material
US2032827 *May 28, 1935Mar 3, 1936Internat Pulverizing CorpMethod of and apparatus for providing material in finely divided form
US2237091 *May 29, 1937Apr 1, 1941Thermo Plastics CorpPulverizing apparatus
US2272564 *Jan 28, 1941Feb 10, 1942Blaine Rhoades FDry cement conveyer
US2311564 *Nov 2, 1940Feb 16, 1943Standard Oil Dev CoHandling finely divided materials
US2327175 *Oct 31, 1941Aug 17, 1943Standard Oil CoCatalyst control in hydrocarbon conversion
US2341193 *Jul 3, 1941Feb 8, 1944Standard Oil CoCatalytic hydrocarbon conversion system
US2379027 *Dec 31, 1940Jun 26, 1945Standard Oil CoCatalytic conversion system
US2392866 *Feb 28, 1940Jan 15, 1946Thermo Plastics CorpMethod and apparatus for comminuting or drying materials
CH216476A * Title not available
GB546088A * Title not available
GB591921A * Title not available
Referenced by
Citing PatentFiling datePublication dateApplicantTitle
US2668669 *Sep 18, 1947Feb 9, 1954Kellogg M W CoApparatus for the explosive pulverization of coal
US2738263 *May 29, 1950Mar 13, 1956Du PontCoal partial combustion with pure oxygen
US2763434 *May 1, 1952Sep 18, 1956Texas CoProcess for pulverizing solids in fluid suspension
US2764531 *Aug 1, 1952Sep 25, 1956Exxon Research Engineering CoProcess and apparatus for retorting oil shale
US2768938 *May 24, 1954Oct 30, 1956Exxon Research Engineering CoMethod of coking and grinding coke
US2785050 *Aug 21, 1952Mar 12, 1957Allied Chem & Dye CorpTwo-stage fluid-suspension roasting of iron sulfide ore
US2830769 *May 18, 1953Apr 15, 1958Texaco Development CorpMethod and apparatus for treating a solid material
US2835561 *Oct 12, 1953May 20, 1958Benz Cyril CSeparation of molten sulfur from a slurry of its ore constituents
US3168989 *May 2, 1962Feb 9, 1965Allis Chalmers Mfg CoProcess and equipment for the production of granulated material
US3863846 *Aug 22, 1972Feb 4, 1975Chemical Comminutions InternatApplication for the benefaction of coal utilizing high volatile liquids as chemical comminutants
US4313737 *Mar 6, 1980Feb 2, 1982Consolidated Natural Gas ServiceMethod for separating undesired components from coal by an explosion type comminution process
US4377392 *Aug 24, 1981Mar 22, 1983Cng Research CompanyParticles from explosive comminution
U.S. Classification241/1, 48/DIG.400, 241/39, 241/62, 241/52
International ClassificationB02C19/00
Cooperative ClassificationY10S48/04, B02C19/00
European ClassificationB02C19/00