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Publication numberUS3643875 A
Publication typeGrant
Publication dateFeb 22, 1972
Filing dateJun 27, 1969
Priority dateJun 27, 1969
Publication numberUS 3643875 A, US 3643875A, US-A-3643875, US3643875 A, US3643875A
InventorsDille Roger M, Schlinger Warren G
Original AssigneeTexaco Inc
Export CitationBiBTeX, EndNote, RefMan
External Links: USPTO, USPTO Assignment, Espacenet
Fluid energy grinding method and system
US 3643875 A
A fluid energy grinding system wherein a stream of a dispersion of solid particles suspended in gas or vapor is accelerated to supersonic velocity in a nozzle having a divergent discharge section sufficient to produce a standing shock wave along the path of flow of solid particles effecting size reduction of particles.
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Description  (OCR text may contain errors)

United States Patent Dille et al. 1 Feb. 22, 197 2 [54] FLUID ENERGY GRINDING METHOD 2,889,242 6/1959 Teichmann ..241/39 UX AND SYSTEM 2,916,213 12/1959 Paull ..241/5 2,846,150 8/1958 Work ..241/39 X [72] Inventors: Roger M. Dille, La Habra; Warren G. Schg Pasadena, both of Calif- Primary ExaminerJames L. Jones, Jr. [73] Assignee: Texaco Inc" New York NY. Attorney-K. E. Kavanagh and Thomas H. Whaley [22] Filed: June 27, 1969 A fluid energy grinding system wherein a stream of a disper- [52] US. Cl ..24l/5, 241/39 sion of solid particles suspended in gas or vapor is accelerated Cl 19/06 to supersonic velocity in a nozzle having a divergent discharge [58] Fleld of Search ..24 H5, 39 tion sufficient to produce a standing shock wave along the path of flow of solid particles effecting size reduction of parti- [56] References Cited cles.

UNITED STATES PATENTS 7 Claims, 4 Drawing Figures 3,257,080 6/1966 Snyder ..24l/5 2,914,391 11/1959 Stratford ..241/5 X 1 36 Z/r/y Z04 34 r d /2 1 /4 JU'HH" e //6' //ea/er 36 Oduc/ PATENTEDFEBZZ I972 3.643 .875

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Ill/[111m FLUID ENERGY GRINDING METHOD AND SYSTEM BACKGROUND OF THE INVENTION The present invention relates to a novel method and a system in which fluid energy grinding is performed by-employing an improved type nozzle therein.

It has been proposed in the past to grind solid particles of material such as coal, talc, ban'te, aluminum, magnesium, clay and oyster shells by suspending'them in a gas and passing the resulting dispersion at high velocity through opposed nozzles.

In a commonly assigned US. Pat. No. 2,846,150 issued to L.T. Work on Aug. 5, 1958, which patent is herewith incorporated by this reference, solid particles are dispersed in a gas stream, and ejected as a plurality of intersecting. streams affecting particle size reduction by impinging them against one another.

The present invention relates to an improved method and apparatus for fluid energy grinding with nozzles.

SUMMARY OF THE INVENTION The present invention relates to a method for reducing the size of relatively coarse particles of a frangible solid material by passing a stream of .such particles dispersed in an elastic fluid, e.g., gas or vapor, through a divergent nozzle wherein the fluid is accelerated to supersonic velocity and expanded to form a standing shock wave which results in disintegration or size reduction of the solid particles. In one specific embodiment of the process of this invention a flowable mixture or slurry of relatively coarse particles of a frangible solid material in a vaporizable liquid is made up, the mixture is passed through a tubular heating zone providing sufficient heat to substantially completely vaporize the liquid and form ,a stream of solid particles suspended in vapor and the stream of coarse particles suspended in vapor expanded through a divergent nozzle in which the velocity of the stream is increased to supersonic velocity and rapidly decelerated to subsonic, thereby creating a standing shock wave near the downstream end of the noule. The solid particles in the stream pass through the standing shock valve wherein they are subjectedto high shearing forces which break up the particles to form smaller size particles. A converging-diverging nozzle is preferred as described in greater detail hereinafter.

The terms pulverization and"grinding, as used herein are to be understood to mean reduction in the size of solid particles as produced in the process described herein.

An object of thepresent invention is to provide an improved process of fluid energy grinding.

Another object of the present invention is to provide an improved process for fluid energy grinding wherein the energy dissipated in a shock wave is utilized for grinding or size reduction of solid particles.

A further object of this invention is to provide apparatus for carrying out the process of this invention.

Other objects and advantages of this invention will become apparent by reference to the accompanying drawings forming a part of this application and illustrating a preferred as well as alternate embodiments of the invention.

BRIEF DESCRIPTION OF THE DRAWING FIG. 1 is a schematic diagram of a system wherein the apparatus of the present invention is used;

FIG. 2 is a longitudinal cross section of the apparatus for performing the herein disclosed novel method;

FIG. 3 is a plan view, partly in cross section, of a. portion of the system showing an alternate apparatus of the present invention; and

FIG. 4 is a longitudinal cross section of another embodiment of the apparatus for performing the herein disclosed novel method.

DESCRIPTION OF THE PREFERRED EMBODIMENTS As illustrated in FIG. 1, solid particles to be ground are blended intimately with a vaporizable liquid to form a flowable mixture in a slurry tank 10, which may include an agitator, such as a motor-driven paddle. The concentration of solid material in this flowable mixture or slurry can be up to 70 percent by weight depending upon the characteristics of the solid material and liquid employed in the process.

From slurry tank 10, the slurry is passed by a pump 12 at a pressure of above about 200 p.s.i.g. through a heated conduit 14 within a heater 16, such as an oil or gas-fired furnace. The heater 16 provides heat to the flowable mixture in the conduit The conduit 14 can be arranged in any desired way within the heater [6 to secure space economy while assuring that the material in conduit 14 is heated to a temperature sufficient to vaporize the liquid in the slurry to forma flowing dispersion. The conduit length and diameter are such that sufficient heat transfer surface is provided for vaporization of the liquid in the slurry. Approximately 1 square. foot of surface area for each 10 pounds of slurry passing through the conduit in a 1- hour period of time is generally required. Typically the tubular heating zone comprises from 1,000 to 1,500 feet of A inches to 2 inches diameter iron pipearranged as a nested coil, but other arrangements also can be used, such as straight pipe sections connected by return bends.

For convenience, only one heater 16 is shown. However,for greater efiiciency a plurality of cascaded heaters can be incorporated in the system, each successive heater being at a higher temperature.

Many vaporizable liquids can be used as the slurry liquid such as water, kerosene, mineral oil or such liquefied gases as propane, butane and air. Selection of the slurry liquid depends mainly on the nature of the material being ground. Water can be used for relatively stable materials such as coal, coke, talc, barite and oyster shells. Kerosene or oil should be used with metals, which may react with steam.

Within the heater 16, the slurry in conduit 14 is heated abovethe vaporization temperature of the slurry liquid so that part way through the conduit there is formed a flowing dispe'rsion of the solid particles in a vapor gas. The term vapor" as used herein does not preclude super-heated gases as the carrier of the flowing dispersion. This dispersion flows the rest of the way through the conduit 14 at a relatively high velocity,

for example, 10 to feet per second, which is sufficient to carry the particles with a minimum erosive effect. Some preliminary grinding of the particles may occur as the particles impinge against one another while flowing through the heater tubes.

The dispersion in conduit 14 can be split into two streams as illustrated in FIG. 3 in which the streams passthrough a pair of ducts l8 and 20 to a pair of discharge nozzles 22 and 24, respectively, projecting from opposite sides of a relatively large diameter reaction chamber 26 to the interior thereof.

The nozzles 22 and 24 have passages 28 and 30, respectively, therethrough of circular cross section which are axially aligned with one another and are shown with their outlet orifices diametrically opposed to one another at an angle of ,However, all that is required in the method of the present invention is a single discharge nozzle 22 which is directly coupled to the conduit 14 so that the dispersion passes through the discharge nozzle 22 into the interior of the reaction chamber 26. For simplicity, since the method of this invention can be practised with a single nozzle, the method will be described by reference to nozzle 22 and nozzle passage 28 when the embodiment of FIG. 3 is not specifically being described. With a single discharge nozzle 22, the reaction chamber 26 must be of sufficient size that the particles leaving the nozzle 22 can dissipate their kinetic energy without eroding any portion of the reaction chamber 26 in the paths of the particles.

Nozzle passage 28 for at least part of its length, has a flared discharge opening, diverging outwardly with respect to the flow of the dispersion therethrough. The nozzle can be flared as shown in FIG. 2, or convergent-divergent as shown in FIG. 4. lt is important however that the nozzle be such that the supersonic velocity is developed in the fluid passing therethrough and that a standing shock wave is developed in the nozzle. An included angle of about 45 for nozzle 22 is satisfactory, but smaller or larger angles from 15 to 90 can also be used. Preferably the included angle of the divergent section is within the range of 15 to 60.

The volume of reaction chamber 26 is large enough to reduce the velocity of the solidsto a value low enough to prevent undue erosion downstream of the nozzle and permit operation of the nozzle as described. For example, reaction chamber 26 may be located in a pipe Tee having legs of about 4 to 12 inches inside diameter. The ratio of the upstream pressure to the downstream pressure relative to the nozzle, necessary for supersonic velocity in the nozzle is at least four. As the pressure ratio is increased, the extent of grinding of the solid particles is increased.

From reaction chamber 26, the low-velocity dispersion of particles in vapor passes through conduit 32 into cyclone separator 34, solids passing off the bottom from product outlet 36 and vapor passing off the top through a valve-controlled conduit 38. Valve 40 regulates the back pressure on the system. A conventional separator can be employed, such as one of the cyclone type. It is to be understood that for greater separation of the powder from the gas additional stages of cascaded separators can be added to separator 34 as well as a scrubber for a final separation.

While the exact mechanism by which the improvement results is not understood, the following is offered as a possible explanation of the mechanisms involved. A standing shock wave is set up in the noule 22 near the exit of the divergent section of the noule and this shock wave is largely responsible for grinding the relatively coarse particles of solid material. Upon passage through this shock wave, the solid particles are subjected to extreme shearing forces which result in grinding of the particles. In shock wave there is a rapid adiabatic compression and conversion of the kinetic energy to a pressure as the velocity decreases to a subsonic value.

The following example indicates comparative results when a similar dispersion is ground according to the prior art with two opposing straight nozzles and according to the present invention with diverging nozzles.

EXAMPLE A slurry containing 40 percent by weight of Tale of which 0.03 percent is retained on a Tyler size 325 mesh, (44 microns), in distilled water was passed into 750 feet of heated half inch iron pipe at a pressure of 1,600 p.s.i.g. and at a rate of 1,800 pounds per hour. The slurry was heated to a maximum temperature of 770 F. at the heater pipe outlet where the discharge pressure was 1,130 p.s.i.g. The resulting dispersion was then passed through opposed flared nozzles having a /32-inch inside inlet diameter and a 15/32-inch outside inlet diameter. The outlet opening of the nozzles had a 7/ 16-inch diameter discharge orifice and subtended an included angle of 45. Each nozzle had a total axial length of 1% inches and a flared axial length of inch. The dispersion was then discharged into the chamber 26 having an outlet connected to a cascaded pair of cyclone separators by a 4-inch lPS pipe.

A similar resulting dispersion, for comparison, flowed through the same system modified by replacing the flared nozzles with straight nozzles having an inside diameter of 5/32 inch and an axial length of 1% inches.

The following Table compares the results of a Klett Turbidimetric analysis (a well-known measurement) of the particle size of a tale product from both a straight and a flared nozzle and the talc feed:

TABLE 1 Product of- Percent of particles in batch which Flared Straight are smaller than stated size Feed (u) nozzle (p) nozzle ()1) A comparison of the figures in Table I shows that the product of the flared nozzle. is consistently finer than the product of the straight nozzle. For example, percent of the product of the flared nozzle is smaller than 2.2 microns while only 60 percent of the product of the straight nozzle is smaller than 3 microns. Also at the lower end, 20 percent of the product of the straight nozzle is smaller than 0.5 micron, while 40 percent of the product of the flared nozzle is smaller than 0.4 micron.

Table 11 below gives quantitative figures showing the quality of fineness of the product of the flared nozzle in contrast to that of the straight nozzle.

Correlated area (ml/g.)

Hegeman is a known measure of the quality or uniformity of fineness of particulate matter. Reference is made to a booklet issued by Sherwin-Williams Company, entitled Hegeman Grind Gauge Reading Procedure which is stated to be an abstract of their test method 441. Additionally, reference is made to an article in the Paint, Oil and Chemical Review, June 22, 1950, pages 34 through 39 by D. Doubleday and A. Barkman of the Sherwin-Williams Co. entitled Reading the Hegeman Grind Gauge."

The above Table indicates qualitatively, that the flared nozzle product is not only finer than the product of a straight nozzle but that the flared nozzle product is also more uniform as can be seen from a Hegeman Grind Gauge reading of 7V2 compared to a 5 /2 for a straight nozzle. The surface area has also increased along with a decrease in the bulk density.

The present invention encompasses the use of one or more divergent nozzles capable of producing a shock wave with one or more other nozzles not capable of producing a shock wave and having the axes of all the nozzles intersecting one another and having the axes of all the nozzles intersecting one another at a large angle so that the effluent of the nozzles impinge against each other.

Other modifications and variations of the above invention as hereinbefore set forth may be made without departing from the spirit and scope thereof, and therefore, only such limitations should be imposed as are indicated in the appended claims.

We claim:

1. A fluid energy grinding system which comprises a flowing dispersion having relatively coarse particles of a frangible solid material dispersed in an elastic fluid, a convergingdiverging nozzle communicating with said flowing dispersion and having a discharge opening diverging outwardly with respect to said flowing dispersion therethrough, means for imparting supersonic velocity to said flowing dispersion and said converging-diverging nozzle including means for producing a pressure drop of at least 75 percent across said nozzle thus producing a standing shock wave .within said diverging discharge opening, the angle of convergence of the converging section of said nozzle being between 45 and 120 and the angle of divergence of the diverging section of said nozzle being between l5 and 90, said angle of convergence always being greater than said angle of divergence.

g 2. A system as described in claim 1 wherein a pair of said converging-diverging nozzles are positioned with their discharge openings substantially in opposition to each other.

3. A system as defined in claim 1 wherein the angle of divergence of said discharge opening is from to 60.

4. A method for reducing the size of coarse particles of a solid material which comprises the following steps in sequence:

a. forming, as a flowing stream, a dispersion of said coarse particles in a gaseous medium,

b. accelerating said dispersion at superatmospheric pressure to supersonic velocity while introducing said dispersion into a zone of gradually decreasing cross-sectional area,

c. introducing the dispersion into a zone of gradually increasing cross-sectional area while effecting a reduction in the pressure of at least 75 percent thereby forming a standing shock wave in said zone of gradually increasing cross sectional area,

passing said dispersion through said shock wave, and recovering from said zone of gradually increasing crosssectional area a dispersion containing particles of reduced size, the rate of decrease of said decreasing cross-sectional area being greater than the rate of increase of said increasing cross-sectional area.

5. The process of claim 4 in which the standing shock wave is produced by regulating the pressure drop and the velocity drop of said flowing stream.

6. A method as described in claim 4, wherein a plurality of said streams are formed having at least one with said gradually increased cross-sectional area and directed to axially impinge against one another at a large angle.

7. A method as described in claim 6, wherein said streams are diametrically, axially impinged against each other at an angle of 180.

Patent Citations
Cited PatentFiling datePublication dateApplicantTitle
US2846150 *Sep 29, 1955Aug 5, 1958Texaco Development CorpFluid energy grinding
US2889242 *Jun 15, 1955Jun 2, 1959Texaco Development CorpManufacturing of wallboard
US2914391 *Mar 4, 1955Nov 24, 1959Texaco IncTreating solid materials
US2916213 *Mar 3, 1954Dec 8, 1959Texaco Development CorpOre beneficiation process and apparatus
US3257080 *Feb 26, 1965Jun 21, 1966Tredco LtdMethod and apparatus for processing anisotropic solid substances
Referenced by
Citing PatentFiling datePublication dateApplicantTitle
US3876156 *May 25, 1972Apr 8, 1975Bayer AgMethod of and apparatus for the jet-pulverisation of fine grained and powdered solids
US3932194 *Feb 11, 1974Jan 13, 1976Johns-Manville CorporationMilled talc material and milling method
US4452911 *Aug 10, 1983Jun 5, 1984Hri, Inc.Frangible catalyst pretreatment method for use in hydrocarbon hydrodemetallization process
US4546926 *Nov 17, 1982Oct 15, 1985Jouko NiemiPressure-chamber grinder
US5385640 *Jul 9, 1993Jan 31, 1995Microcell, Inc.Process for making microdenominated cellulose
US5487419 *Jul 9, 1993Jan 30, 1996Microcell, Inc.Redispersible microdenominated cellulose
US6482250Feb 28, 2000Nov 19, 2002Barrick Gold CorporationNozzle for low pressure flash tanks for ore slurry
US6530534Sep 13, 2000Mar 11, 2003Lee McGrathPneumatic comminution and drying system
US6691938 *May 21, 2001Feb 17, 2004Hydro-Attrition Scrubbers LlcMethod and apparatus for hydroattrition scrubber
WO1983001915A1 *Nov 17, 1982Jun 9, 1983Jouko NiemiPressure-chamber grinder
WO1984003455A1 *Mar 5, 1984Sep 13, 1984Jouko NiemiPressure chamber grinding equipment
WO2001019521A2 *Sep 13, 2000Mar 22, 2001Mcgrath LeePneumatic comminution and drying system
U.S. Classification241/5, 241/39
International ClassificationB01J2/00, B02C19/06
Cooperative ClassificationB02C19/06, B01J2/00
European ClassificationB02C19/06, B01J2/00