MXPA97005983A

MXPA97005983A - Method and apparatus for the dry milling of soli

Info

Publication number: MXPA97005983A
Application number: MXPA/A/1997/005983A
Authority: MX
Original assignee: Ernest Csendes
Filing date: 1997-08-04
Publication date: 1999-04-06

Abstract

The present invention relates to a method for the dry milling of solids, characterized in that it comprises the steps of: directing solid particles generally upwards to a swirl milling zone, and milling the solid particles directed upwards in the milling zone of swirling by passing a portion of the particles through the swirl milling zone, the swirl milling zone comprising at least one vertically disposed whirling milling step comprising successively passing particles up through the milling zone. at least one of the semipermeable rotating means and an annular space defined by a stationary plate with a flat surface with a circular opening therein and a rotating circular disk without openings in the circular opening

Description

METHOD AND APPARATUS FOR MILLING IN DRY SOLIDS RELATED REQUESTS This application is a continuation request in part of the application S.N. 07 / 907,368 filed on August 1, 1992, and the application of E.U.fl- S.N. 07 / 983,019 filed on November 30, 1992 and pending *.

BACKGROUND OF THE INVENTION The present invention relates to a method and apparatus for the solid grinding of solids. The process of dry milling is practiced today using hammer mills, impact mills, ball mills, cylindrical mills or roller mills equipped with internal classifiers that purify la-; desired fine fractions and return the coarse particles to a grinding chamber. For superfine and ultra M na milling, a similar arrangement is used with vibration mills, impact mills, or jet mills. All the mills, present show poor efficiency in fine grinding, use excessive energy and exhibit very high wear. In conventional mills, dry milling of solids with mechanical irnpactac tion rails suffers from the disadvantage that the fi rst solid fractions formed during the grinding process are fixed by themselves. elect rosta-icamen-t or larger particles that protect the impacts during subsequent collisions and thus, the efficiency of grinding decreases. Although the jet mills do not have the eiectrostatico Lerna prob of the impact mills, because the jet mills use high pressure gases, it has high energy requirements, great maintenance and limited capacity.

BRIEF DESCRIPTION OF THE INVENTION The main objective of the present invention is to eliminate the disadvantages of the prior art systems and to provide a method and apparatus for the dry grinding of solids which render finished products in a safe, energy efficient and environmentally acceptable manner, with low capital and operating costs. The present invention utilizes the controlled swirling action of a fluidised bed for the coarse and fine grinding of solids at low static pressures, followed by gas wear and shear stress of the particles in a vertical or horizontal swirl at high flow pressures for yield fine, superfine and ultra-fine products. In the present invention, limiting the size of the particles of the materials supplied to the grinding zone for fine, superfine and ultra-fine grinding is implemented by subjecting the mixture of particles to gravity separation by means of a centrifugal ejection fan and allowing the stream of gas containing the selected particles to enter a milling area of swirling action. Opposite to conventional mills, the present invention achieves the instant removal of fine particles by a strong draft airflow, whereby dry milling becomes more efficient. In the present invention, this is coupled to an efficient internal recirculation of the oversized particles to the initial coarse grinding stage by semipermeable rotating means. Opposite to the jet mills, the present invention does not use pressurized gases as a source of crushing energy, thereby greatly reducing capital costs, energy requirements and maintenance, while allowing for scale-up on capacity. The present invention utilizes rotors to create a controlled whirling action in a fluidized bed, which grinds primarily by autogenous abrasion and irnpaction, and swirl generators comprising semipermeable rotating means, which generate a vertical whirl and grind primarily by gas wear, and Rotating discs, which generate a horizontal swirl and move mainly by shear stress. The present invention can be used to micronize coal or limestone, and allows to use micronized products of ba or cost for applications in energy raw materials, petrochemicals, environmental cleaning of generating and heating plants for utility and industrial use, transportation of solid substances processed by pipe, manufacturing of construction materials, manufacture of new or improved materials such as insulators soporador <; - weight, manufacture of ceramics and superconductors, and in the production of metals and metallurgy related to the preparation of minerals, including precious metals. Certain definitions related to the size of the product are used in the present invention as follows: Product size llalla (Tyier's mall) j,? Rn Coarse +270 > 5f- Fine 270 Y -270 _ < 5ñ Superfine 500 and -500 j.32 Ultrafine -500 to 4,500 < 32 a < 5 In the course of this request. reference is made to the solids "my cromzados", for example, mineral coal and limestone icronizados. For these purposes, "micronized" is defined as solids in the size scale of 75%, -400 -75% mesh, < 40 pm).

The present invention avoids the costly problems associated with the direct impact of the particles on the internal moving parts of the grinding machinery as well as the impact mills, which result in high energy costs and excessive wear and maintenance of said devices. . The present invention uses fast moving air pads on which the particles are milled by autogenous abrasion and impaction, gas wear and shear stress. The mechanism of grinding in the present invention is designed to avoid collisions of the solid particles with the internal mechanism of the mill. During the generation of a controlled whirling action in a fluidized bed, the rotors of the present invention operate as rotating fans, the rotor blades striking the gas and the gas, in turn, transmitting this emitted energy imparted to the particles. they swirl in the initial coarse grinding zone. Therefore, the present invention can be practiced with internal parts coated / covered with polyurethane or with polyurethane mold to reduce the size of the abrasive minerals and still exhibit wear factors. The foregoing explains the milling efficiency, low energy requirements, low wear and low maintenance costs of the present invention. The present invention is a fluid energy mill, that is, a gas such as air, carbon dioxide, nitrogen or a noble gas acts as the operating fluid and performs the transmission of the energy necessary to accelerate the suspended particles that they undergo size reduction. In conventional fluid energy mills, for example, jet mills, a velocity loading is generated for the particles by high external pressures imparting their initial velocity to the fed particles. However, said speed load decreases after a short path, hence the efficiency and high recirculation ratios, as well as the high wear factors for the jet mills. In contrast, the particles fed in the present invention are only re-accelerated by centrifugal forces, and their speed loading is renewed by air pads energized by the rotating mill rotor assembly. The present invention operates at low speeds. static pressures (up to 38.1 c of water column), but generates very high flow pressures through venting effects that propagate through the internal design of the apparatus. The e-speeds are on the scale of 3,000 to 10,000 revolutions per minute (RPM). The rotors of the grinding chamber of the present invention are the source of the centrifugal forces. The agitation of the fluidized bed of the particles is achieved by the movement of turbulent air generated by the rotors, together with the increasing flow bars mounted vertically on the inner walls of the mill.

The design of the rotor blades is selected to give optimum conditions for the acceleration and controlled turbulence of the air cushions. Adornas, said design ensures a minimum energy consumption and the prevention of collisions of the rotor blades with the particles fed. With fine particles, superfines and ult raf as, collisions are avoided by lifting the Limit layer. The distance between the rotor blades and the wall of the mill cover defines the width of the grinding zone of the fluidized bed. By shortening the rotor arms, the width of the fluidized bed expands and the capacity of the initial coarse grinding zone is improved. The present invention operates on the principle of gas swirl milling as the operating fluid. For its initial reduction in size, it uses the controlled swirling action of a fluidized bed, where the centrifugal forces and the swirling of the swirl are created by a rotor assembly. The fluidized bed is supported by a strong air stream of lifting that also provides instant removal of fine powders. A unique mechanism of internal recirculation achieves, at a cost of energy, the return of coarse or oversized particles that have been brought along with the fine powders by the lifting air stream, to the initial coarse grinding zone to mix them with the incoming feed stream in the whirlpool. For its fine and superfine main milling, the invention uses two novel methods of crushing through milling by swirling --- (i) semipermeable rotary media; and (ia) rotating discs. In its primary milling process, the invention uses a fluidized bed at low static pressures, and its secondary milling proceeds at high flow pressures. In the last phase, the fine powders can be converted into superfines and lth raffins, to the degree of 1/4 to 1/2 of the total fine olvos produced. In this way, the ratio of fine powders to superfines produced is on a scale of 4 to 2 without an appreciable increase in the cost of energy over that of the milling process. If the internal design of the equipment varies, the secondary grinding procedure can be suppressed. The milling system can be operated by recirculating the operating fluid, thus making the system safe and reliable. In addition to its environmental benefits, the milling system of the present invention operates at low noise levels. The controlled swirl action achieved with the present invention allows proper heat dissipation-during coarse grinding in the fluidized bed, and close control of the size reduction process in the initial grinding chamber. Therefore, the present invention overcomes the disadvantages of the prior art, where the mills operate with uncontrolled whirling action which results in an increase in heat with n rollable, the lack of close control of the size reduction process and undesirable alterations in the product. The use of rotary screens for the separation of solids by size is well known. Centrifugal sieves work on this principle and select the size of the ground product, allowing the passage of small particles through the sieve openings and centrifugally rejecting the thick sieved particles remaining on them. The sieves operate at a rotation speed of 30 to 120 RPM. If the speed of the sieve is increased to more than 1,200 RPM, the sieve's rotating sieve becomes clogged, and the separation by size ceases due to sieve clogging. If a sieve with a 100 mesh screen is used in the milling system of the present invention, at a rotation speed of 1,500 to 4,500 RPM, the screen is instantly clogged with fine powders and becomes inoperable. The solid particles which originate from the milling by swirling in the fluidized bed of the initial grinding chamber, and which are carried upwardly by the rising gas stream are in the mesh size scale. 40 to 500. An object of the present invention is the use of semipermeable rotary means, comprising assembly with a rotary sieve of large mesh size which is not hindered by high speed rotation. One use of the semipermeable means is to carry out the recirculation of thick particles or of certain over-suspended particles suspended in a gas medium. This makes it possible to recirculate the oversized particles at low cost from the fast-moving gas stream. The divisions in the fast spin sieve of mesh size from 4 to 10 act as a statistical barrier to slower moving particles. The semipermeable rotary means are not able to recognize the differences in the particle sizes as a centrifugal sieve, so that a mesh particle -0 may not be blocked by a rotating sieve with a 4 mesh screen. The semipermeable rotary means only They are able to recognize differences in particle velocities. The particles carried in ascending form from the grinding zone of the fluted bed reach s? velocity in the laminar gas flow, depending on its Stokes drag, which causes large particles to reach a lower velocity than small particles. In turn, particles that move more slowly are more likely to hit the divisions of the fast-spinning wide-screen sieve contained in the semi-permeable rotary media assembly., and that are rejected by him to fall back into the initial coarse grinding zone. Therefore, the ratio of the speed of the revolving screen to the velocity of the ascending particles, ascending in the gas stream, determines which particles are blocked by the divisions of the wide-screen fast-spinning sieve. By varying the speed of the screen, the size of the particles passing through the fast spinning screen can be controlled. This explains why the size of the particles has no relationship with the mesh size of the rotating screen in the present invention. The semipermeable rotating means can block a particle with a mesh size of 60 to 150, depending on the previous ratio of the velocities of the circularly moving sieve and the particle moving in ascending f-orrna. In turn, the velocity of the particle will depend on the velocity of the rising gas stream and on the particle size that determines its drag. The previous phenomena of the "statistical rejection" of the particles through a system with a fast-spinning sieve of mesh size, due to their different speeds that support the internal recirculation of the coarse or overdrawn particles towards the zone of Initial grinding of the present invention is limited to a system containing solid particles suspended in a fast moving gas stream. The above phenomena do not occur in dense media, that is, in liquids such as water. The permeable means of the present invention operate efficiently at rotation speeds in the range of 1,500 to 10,000 RPM and more preferably in the range of 3,000 to 4,500 RPM. The semipermeable means of the present invention overcome the difficulty experienced with the prior art screens which become clogged and become inoperable when rotating at high speeds. Once out of the initial coarse grinding chamber, the particle sizes will be on the sieve scale from 150 to 500, or smaller, and with such smaller particle sizes, the drag forces will decrease rapidly. Therefore, the choice of the speed of semipermeable rotary media will be negligible to the smallest particle sizes that prevail from the initial coarse grinding chamber. Another use of semipermeable media outside of the initial coarse grinding zone is the grinding of fine solids through the creation of vertically directed swirling. This yields superfine and ultrafine grinding at low cost. The high-velocity gas passing through the semipermeable rotating media is separated into gas bundles by the divisions of the wide mesh sieve, and the bundles are twisted by the impulse of the rapid rotation of the sieve, thus generating a vertical spiral swirl . In the vertical eddy, the particles are crushed by gas wear. The effectiveness of the grinding depends on the speed of the gas in the grinding zone by swirling action, which determines the residence time of the particle in the swirl, and the rotation speed of the permeable media, which determines the speed of the the turbulence that affects the gas bundles that comprise the whirlpool. Outside the initial coarse grinding chamber, the only function of the semi-rotary rotary media is to be an effective swirl generator. Originally, in the present invention, the swirl generators are placed in sorting chambers where the separation by gravity of the thickest particles in the rising gas stream is affected by centrifugal ejection fans. I BS selected particles that remain in the rising gas stream are subjected to the milling by swirling action generated by the semi-leakable media. By repeating this procedure in stages, each stage comprising separation by gravity and milling by swirling action, fine particles can be reduced to ultrafine size. The grinding of fine particles to superfine and thermophanous products by gas swirls created by a rotating screen is unexpected and occurs at a very low energy use. The screen is preferably composed of steel and has a mesh size in the range of 2.5 to 60, more preferably in the range of 4 to 10. The optimum mesh size of the rotating screen and the rotation speed have to be selected experimentally. The generation of the swirl by the semipermeable rotating means is limited to a gaseous medium. In dense media, for example liquids such as water, the swirls created by a rotary sieve are localized and extinguished by friction. Another purpose of the semi-rotary rotating media is the effective removal of solids from a high pressure gas, at high temperature and at high speed, with negligible loss of pressure and temperature drop. The semi-leakable media for this application has a rotating sieve with a mesh size in the range 2.5 to 60, more preferably in the range of 4 to 10, and are composed of a metal or alloy, such as tungsten or steel. , appropriate for the temperature and the speed of rotation to which they will be exposed. The ratio of the sieve speed: rotary and the velocity of the gas stream under pressure to which an adequate differentiation of the velocity of the suspended solid particles occurs, to effect its blocking by the semipermeable rotating means, has to be determined. Additional debugging of 1 <; - gas flow can be effected by separation by gravity with a centrifugal expulsion fan, following the passage of the gas stream through the semipermeable rotating means. Another objective is the use of an annular space defined by a stationary circular opening and a circular rotating disk located in said opening, for the grinding of fine solids in the annular space through the creation of a horizontally directed swirl created by the disk rotary. The annular space has a width of 1.27 crn to 15.24 crn, preferably about 7.62 c, and a height of 1.27 cm to 15.24 crn. The effectiveness of the crushing in the annular space will depend on the residence time of the fine particles in it and the prevailing shear forces. Therefore, the effectiveness of the annular space will be determined by the speed of the rising gas flow and the speed of the rotating disk. The reduction of size to t-tves the annular space occurs at a low and high energy use. In the widely known application of rotating discs to control the particle sizes entering the crushing zone, the width of the annular space (for fine grinding and superfine applications) would have to be on the scale of .3175 ca.508 crn With such a small width of the annular space, the generation of the vortex would become operable to achieve size reduction through shear stress, and the use of energy would increase excessively. Originally, in the present invention, the swirl generator consisting of an annular space is placed in a sorting chamber where the reduced particles leaving the horizontal swirl of the annular space-suffer size separation in a gravity field generated by a fan of centrifugal expulsion. The present invention uses for its superfine and ultrafine milling swirl generators comprising the semipermeable rotary means and the annular space located within a sorting chamber, where this secondary grinding is carried out at a low energy use and a low maintenance cost. . Therefore, the present invention overcomes the disadvantages of the prior art, where impact mills are used - abrasion for superfine and ultrafine grinding which is achieved in the initial grinding chamber through the uncontrolled swirl action in the narrow space between the rotors and the wall tle the cover and through the generation of action of swirl intra-blades and inter-plates (in some cases increased by the generation of ultrasonic waves). Said swirl action and sonic increase of the prior art represent low efficiency procedures for fine grinding, high energy use and high maintenance cost. A further objective is the use of autogenous grinding media and / or arrangements that produce the shear stress or gas wear of suspended solids in the gaseous operating fluid for the purpose of in situ modification of the reactive surfaces of said particles. i «freshly ground with organic or inorganic chemical reagents. The reactivity of freshly ground surfaces and their modification with chemical reagents is well recognized, but modification procedures in prior art milling systems, for example, impact mills-abrasion or jet mills, occur in a non-destructive manner. controlled Therefore, the economy of the surface modification procedure is not favorable due to the excessive use of reagents and the limits thus imposed on the control of the properties of the final products. In the milling system of the present invention, the generation of new surfaces by shear stress in the annular space can be tightly controlled and a partial surface modification can be achieved with economical use of the chemical reagents to yield a modified product. with desirable surface properties. Still another objective is the use of swirl generators comprising a combination of semipermeable rotary means, consisting of an assembly containing a rotating screen and an annular space formed by a rotating disc in a circular stationary opening for the purpose of superfine and ultrafine grinding of solids at low energy use. Ordinarily, said combi ation and swirl generators are used in the present invention within a sorting chamber, where the separation by gravity by a centrifugal ejection fan selects the size of the particles leaving the horizontal swirl of the space annular, before allowing the stream of purified gas with the reduced particles of the desired size to enter the vertical swirl zone generated by the semipermeable rotating means. The repeated use of said combinations in a vertical stack of cameras of 10 classification, it gives rise to the production of ultraf os products. The oversized particles removed in a given sorting chamber are re-circulated externally to the above sorting chamber in the vertical stack for the purpose of still reducing their size by whirling. Still another objective is the use of a milling system consisting of a rotor chamber for the initial coarse and fine grinding of solids in a controlled swirl of a fluidized bed grinding zone with an additional grinding zone available for grinding. the superfine and ultra-fine grinding of said swirl generator solids comprising semipermeable rotating mills and said annular space, wherein a split power pulse is provided which allows a very fast rotation of the screen and the disk to a ba use of energy The sieve with a divided impulse can rotate at more than 10,000 RPM, while the rotor assembly rotates at less than 3,200 RPM, still retaining the characteristics of low energy use and low wear. For the performance of the internal recirculation function within the initial coarse grinding chamber, which comprises the classification of the particles by their different individual velocities in the lifting gas stream, the semi-rotary rotary means have to reach a speed less than 4,500 RPM. Another objective is a system in which the rotor assembly is covered with rubber, polyurethane or other plastic materials, or the rotor assembly is formed by emptying these parts from said materials. Alternatively, the rotor assembly can be coated with ceramic (eg, chromium carbide, tungsten carbide)? aluminum oxide. An additional objective is a system in which the walls of the system and the rotating sieve and disc are covered with rubber, polyurethane, other plastic materials, ceramic or aluminum oxide. These and other objects and advantages of the present invention are achieved in accordance with the present invention by a method for the dry grinding of solids comprising the steps of directing the fine fine particles generally in ascending form in a grinding zone by the action of swirl and grind solid fine particles directed upwards through tje swirl generators located in the milling area by swirling by passing a portion of the particles through the milling area by whirling action, milling by swirling action comprising at least one milling step arranged successively verif ically which comprises passing the particles in ascending form to tr-birds of at least one of the semipermeable rotary means and an annular space defined by a plate stationary with a circular opening in the same and a circular rotary di in the circular opening. The purpose of passing the particles upwardly through said semipermeable rotary means comprises passing the particles through a fast spinning screen. The screen is not thicker than the 2.5 mesh, preferably has a mesh size on the scale of 2.5 to 60, and preferably has a mesh size on the scale tJe 4 to 10 and is rotated at a speed on the scale from 1,500 to 10,000 RPM, and preferably in the range of 3,000 to 4,500 RPM. The step of passing the particles through the annular space comprises passing the particles through an annular space having a width of 1.27 orn to 15.2-pn, preferably about 7.62 crn, and a height of 1.27 crn to 15.24 crn. Preferably, each step comprises passing the particles through the semipermeable rotating means and then through the annular space. To classify the particle sizes that leave the annular space, the rising gas comment with its mixture of suspended particles is subjected to gravity separation by means of a centrifugal ejection fan, and the ascending gas stream with the selected particle sizes is allowed to enter the milling zone by vertical swirling of the semipermeable rotating means. In the initial coarse grinding chamber, the method also comprises internally recirculating, by rotation, said semipermeable media at a sufficient speed to prevent the removal of a portion of the oversized particles through the mills. The method further comprises externally recirculating, by rotation, a centrifugal ejecting fan downstream of the semipermeable rotary means and providing a recirculation channel which receives the particles from the rotating fan and which has a salt below the porous at least one stage of rotation. milling by swirling action. The method also comprises the step of removing the particles above the grinding zone by swirling action. The removal step comprises rotating at least one centrifugal ejection fan below at least one milling step per whirling action. In one embodiment, the method also comprises the step of initially grinding the coarse particles into fine particles before directing the fine particles in the swirl generators containing the grinding zone. The step of injecting my material comprises feeding the solids into a chamber, forming a fluidized bed of the solids in the chamber directing air upwards in the chamber and creating a controlled whirling action in the fluidized bed for the purpose of autogenous grinding. . The external recirculation passage comprises externally recirculating the particles in the fluidized bed.

T? The method may have a plurality of milling steps, containing swirl generators with external recirculation of the overdrawn particles to a previous stage. The separation and removal step is preferably compressed in two stages of removal vertically arranged to separate and remove particles of successively smaller sizes. In another modality, the initial coarse grinding step comprises generating a controlled swirl using the use of rotors. The swirl generators comprising the semipermeable rotary means and the rotating disc can rotate on a common axis. The milling step can be carried out in a non-reactive gas atmosphere in the presence of a chemical reagent to effect controlled surface modification of the solid particles. The present invention is also directed to an apparatus for the dry milling of solids, comprising means forming a milling zone by swirling action that contains swirl generators, including at least one step of milling by swirling action vertically prepared for the grinding of solid fine particles, and means for directing the fine particles solid, generally in an upwardly ascending manner in the milling zone by swirling action. At least this swirling step comprises swirling generators which contain at least one of the semi-permeable rotary means and means forming an annular space comprising a stationary plate having a circular opening therein, and a circular rotating disc in the circular opening and wherein the semipermeable rotating means and the annular space are configured to pass a portion of the small particles directed in ascending fashion through them, and having a size separator. of particles for the products leaving the horizontal swirl zone of the annular space, the overdrawn particles being separated by gravity with a centrifugal expulsion fan. The semipermeable rotary means preferably comprise a rotating screen no thicker than 2.5 mesh, preferably having a mesh size in the range of 2.5 to 60, and more preferably having a mesh size in the range of 4 to 10. The The annular space has a width of 1.27 cm to 15.24 cm, preferably around 7.62 cm, and a height of 1.27 cm to 15.24 cm. Both swirl generators are used to efficiently grind the fine particles in the rising gas stream and reduce these particles to super-fine and ultra-fine products. In one embodiment, each stage comprises the semipermeable rotating means and means forming the annular-downstream space of semipermeable rotating means and having a gravity separator of the oversized particles in the rising gas stream comprising a centrifugal ejection fan. In another embodiment, the apparatus also comprises means for internally recirculating the coarse particles in the initial grinding chamber including means for rotating said semipermeable means at a sufficient speed to prevent the passage of a portion of the particles through the Also, said portion comprising particles exhibiting lower velocity in the rising gas stream. The apparatus also comprises means for externally rotating, comprising a rotatable centrifugal ejector fan downstream of the semipermeable rotary means in the initial coarse grinding chamber and a recirculation channel which receives the particles of the rotating ejector fan, and having an outlet below it, at least one stage of milling by swirl action. The apparatus also has means for removing the particles above the initial coarse grinding zone. In one embodiment, the removal means comprises means for rotating at least one centrifugal fan mentioned below at least one grinding step. . In an additional mode, the apparatus further comprises means for grinding my coarse particles into fine particles before they are directed into the grinding zone containing the swirl generators. The means for grinding micially preferably comprises wheels for feeding solids into a chamber, means for forming a fluidized bed of the solids in the chamber including means for directing air upwards in the chamber and means for creating a swirling action. controlled in the fluidized event will make the autogenous label. External circulation comprises means for externally recirculating the particles in the fluidized bed. In yet another embodiment, the apparatus comprises a plurality of milling stages, each of the steps comprising swirling generators and means for separating through gravity and externally recirculating the oversized particles to a previous stage. The removal means preferably comprise removal means in two stages of vertical removal arranged to separate and remove particles of successively smaller sizes. The means for the initial grinding preferably comprise rotors to generate a controlled swirl. The swirl generators comprising the semipermeable rotatable means and the rotatable disk preferably rotate about a common axis. In another embodiment of the present invention, a method and apparatus for the dry grinding of solids comprises means for feeding solids into a chamber, means forming a fluidized bed of solids in the chamber directing air upwardly in the chamber, and means that create a controlled whirling action in the fluidized bed to effect autogenous grinding. This embodiment also preferably includes means for separating and removing the particles above the fluidized bed, and preferably means for recirculating the particles removed in the fluidized bed. The removal of the particles preferably comprises rotating at least one centrifugal ejection fan downstream of the fluidised bed, and the recirculation preferably comprises spinning a centrifugal ejection fan downstream of the fluidized bed and providing a recirculation channel. which receives the particles of the rotating expulsion fan and which has an outlet in the fluidized bed. The particles can be removed in two stages of vertical removal arranged to separate and remove particles of successively smaller sizes. The creation of a controlled whirlpool action preferably involves rotating rotors, and the milling can be carried out in a non-reactive gaseous atmosphere in the presence of a chemical reagent to effect a controlled surface modification of the soldered particles. A further embodiment of the present invention is directed to a method and apparatus for depuration of particulates from a gas stream, comprising rotating at least semi-permeable rotary media, directing at least one particle gas stream. solids through at least semi-permeable rotatable means, and removing the particles that do not pass through at least semi-permeable rotary means and removing the particles that pass through a rotating expulsion fan, downstream of the rotating means semipermeable. At least one of the semipermeable rotating means preferably comprises an assembly with a rotating screen, preferably a screen no thicker than 2.5 mesh, more preferably a screen having a mesh size in the range of 2.5 to 60, and more preferably a screen having a mesh size on the scale of 4 to 10. These and other objects and advantages of the present invention will be apparent from the following detailed description taken in conjunction with the accompanying drawings, wherein: DESCRIPTION OF THE DRAWINGS Figure 1 is a schematic view of an apparatus in accordance with the present invention for carrying out the method in accordance with the present invention, - Figure 2 is a schematic cross-sectional view of a fluid energy mill shown in FIG. Figure 1; Figure 3 is a schematic view in section 20 cross section of a fluid energy reformer in accordance with the present invention; Figure 4 is a schematic cross-sectional view of an ultrafine fluid energy reformer in accordance with the present invention; Figures 5A and 5B are top and sectional views of the centrifugal lifting fan shown in Figure 2; Figures 6 and 6B are top views of two different coaxial rotors used in Figure 2; Figures 7A and 7B are top and elevational views of the semipermeable rotary means shown in Figure 2; Figures 8ñ and RB are top and elevational views of the rotating disc shown in Figure 2; Figures 9A and 9B are top and top elevations of the turntable shown in Figure 2; Figure LO is a top view of an internal support assembly in the mill of Figure 2; and Figure 11 is a top view of the flow-enhancing bar-ras in the mill of Figure 2.

DETAILED DESCRIPTION OF THE INVENTION Figure 1 is a schematic view of the apparatus in accordance with the present invention and an appendix to carrying out the method of conformity with the present invention. As shown in Figure 1, the grinding unit LO includes a lower fine and coarse grinding zone 11 in the form of a chamber to which solid material is fed through the feed inlet 14 and in which a gas , such as air, is fed from the bottom in the inlet 15. The particles in the lower zone 11 are fed by means of the gas flow in the intermediate grinding zone 12 for further grinding. The intermediate zone 12 is provided with do < - recirculation paths 18 and 19 to recirculate the oversized particles back into the lower zone 11. The particles milled in the intermediate zone 12 are fed by means of the gas flow in the upper separation zone 13. The upper zone-13 works to separate the final product (such as superfine particles), which exit through the line 16 to the cyclone 30 to be isolated from the superfine product, the fine particles are removed from the supepor zone L3 through Line 17 to the cyclone 20 to be isolated from the fine product. The cyclone 20 passes the recirculation gas through the line 23 at the bottom of the lower zone 11, and transfers the particles through the line 24 to the product cylinder 21 for fine particles. The cyclone 30 recirculates its gas through the line 22 at the bottom of the lower zone 11. The superfine particles pass through the line 33 in the product cylinder 31. Alternatively, the cyclone 30 can pass all the gas conveyor, or part of it, to tr-birds of line 40 to a collector tank. Figure 2 shows the grinding unit 10 of figure 1 with further detail. As shown in the present invention, the grinding unit uses the internal ee 51 which is driven by the motor 52 and is located in the support 53, and which is responsible for the rotation of all internal parts 4 to 68 of the milling unit. To stabilize the rotating shaft against vibrations, one or more internal bearings are provided and, as shown in FIG. 10, these bearings are fastened through steel beams 76 to the outer wall of the mill. To operate at speeds in excess of 4,000 RPM, a hole can be used to prevent flagellation of the shaft. The apparatus can be operated with a split shaft, where the axis in zone 11 containing the rotors, it is operated at a lower shaft speed, and the other rotating elements are operated at a higher shaft speed. The lower zone 11 includes a rotating plate 54 which is located below the internal lifting fan 55. The plate 54 protects the fan from turbulence caused by recirculated gas streams entering through the inlets 22 and 23. The fan 55 works to provide a lift airflow throughout the milling unit. The lifting fan 55 is shown in more detail in Figures 5A and 5B. As shown in the present invention, the fan includes a central portion 55, and a plurality of vanes 55B, each of which is twisted at an angle of approximately 15 °, alternating up and down the hub to create an action of rising when they turn. On top of fan 55 are four rows of rotor-is co-axial twins in crossed quilting 56-59. The rotors are preferably round arm or flat plate arm rotors which are wedged in the shaft and hold a coaxial rotor blade in each extrusion. The rotor blades are shown in more detail in figures 6A and faU. Figure 6 shows a flat plunger arm rotor having a flat plate 56 L with rotor blades 562 and 563 at the ends thereof. The rotor blades are disposed at a torsion angle of approximately 70 ° to the horizontal plane of the plate 561. A round-arm rotor including the round arm 564 and the rotor blades 565 is shown in Figure 6B. and 566 at the ends thereof and arranged at a torsion angle tle about 70 ° relative to the arm 564. The fan 55 generates a peripheral curtain of air facilitated by sides (not shown) fixed to the lower end of the incrementing bars of flow 77 which are fixed to the wall 78 as shown in Figure 11. The wall 78 may be covered with a rubber or polyurethane coating and has flow increasing bars 77 fixed thereto, preferably spaced every 7.62 cm at 17.78 crn along the wall. The rotor blades agitate the fluidized bed created by the fan 55. The rotor blades may have different winding or torsional angles against the horizontal plane, different inclination angles, i.e. inclination against the vertical plane, or they may have Oscillating angles with respect to the rotor arms. In addition, the rotors may also have different baffles (not shown) to increase turbulence of the swirl or to lengthen the grinding zones through the deflection of the air streams. Arranged above the rotor 59 at the beginning of the intermediate zone 12, there are semipermeable rotary means 60 which act to facilitate the internal recirculation of the coarse or oversized particles towards the initial grinding zone 11, further promoting fine grinding and additional super fine grinding. through its vertical whirling action on the particles in ascending form within the intermediate zone 12. The structure of the semipermeable gauge means 60 is shown in Figures 7A and 713. As shown in the present invention, the semipermeable rotating means 60 have a frame 50A including the hub 60B that is wedged to the shaft 51. On the lower portion fie the support plate 60A is the sieve 60C. The screen may be in the range of 2.5 to 60 mesh, preferably 4 to 10 mesh. The screen is preferably made of steel. Below the screen is the baffle 60D which prevents the passage of the particles to tr-birds from the center of the 60C screen. The baffle disc can vary in diameter from 10.16 m or 25.4 pn, depending on the quantity and fineness of the desired product. The particles passing through the semi-permeable rotary means must then pass through the annular space 70B between the stationary plate 70 and the rotary disk 61 arranged in the opening 70A of the stationary plate 70. FIGS. 8A and OB show the position of the rotating disc in the central opening of the seasonal plate in more detail, forming the annular space 70E. The annular space 70B is from 1.27 cm to 15.24 ein wide, preferably around 7.62 crn, and has a height of 1.27 crn to 15.24 ein. The distance between the means 60 and the plate 70 is preferably greater than 5.08 crn. The rotary disc 61 and the stationary plate 70 are preferably in the same plane, but the plane of the disc may be up to about 2.54 crn above or below the plane of the plate. The rotating disc and the stationary plate are preferably composed of steel. The intermediate zone 12 includes the centrifugal ejection fan 62 which acts to eject the coarse or oversized particles passing through the semipermeable rotary means 60 and the annular space 70B between the rotating disc 61 and the stationary plate 70. These particles thick or oversized are recirculated through the conduits 18 and 19 to the initial milling zone 11.

Arranged above the fan 62 are semi-permeable rotary means 63 having the same structure as the semi-permeable rotary means 60. The particles that have reached a small size are no longer rejected for recirculation by the semi-permeable rotary means 63 which serve only for the function of the swirl generation. Above the means 63 is the stationary plate 71 having a rotary disk 64 arranged in the opening 71A and forming the annular space 71B. These have the same structure as that of the stationary plate 70 and the rotary disk 61. Arranged above the rotary disk 6 is the centrifugal ejection fan 65 which expels the fine particles through the outlet 17. Arranged above the fan ejection 65 is the turntable 66 which has the same structure as the turntable 54 and which is shown in more detail in Figures 9A and 9B. As shown in the present invention, the turntable has a hub 61 that is wedged to the shaft 1, so that it rotates therewith. The purpose of the plate 66 is to decrease the upward turbulence within the zone 13 and to facilitate the separation by size effected by the centrifugal ejection fans 65 and 68 through the outlets of the receptacle 17 and 16. In the event, it desires a finer separation by size of the fine or superfine particles, and the products of the outputs 17 and 16 can be fed into an elution unit. Arranged above the turntable 66 is the stationary plate 72 having a rotating disk 67 which rotates in the centre aperture 72A and forms the annular space 72B. The structure of this plate is identical to that of the aforementioned stationary plates with rotating discs. Arranged above the rotary disc 67 is the centrifugal ejection fan 68 which ejects the superfine particles through outlet 16. The lower zone 11 it can operate as a closed atmospheric system, in which case input 15 and output 40 are closed. If the wet particulate feed is to be used, an instant dryer should be fixed to the inlet 15 to dry the particles fed at a moisture level of less than 4%, while simultaneously grinding. Fixes have to be made for the steam produced during the drying, creating an exit after the exit of the cyclones, said exits located in the entrances 22 and 23. The entrances 22 and 23 in L < ? Figure 1 serves to transport the recirculated gas from the cyclones. The incoming feed particles from the inlet 14 are driven towards the circumference by the action of the gas bearings generated by the rotors 56 to 59, and form there a fluidized bed of particles, held in suspension by the continuous lifting forces of the gas stream produced by the fan 55. The velocity loading of the particles colliding in the circular fluidized bed is generated by the centrifugal forces of the rotors 56 to 59, and transmitted through the gas operating fluid. Said speed load is renewed with each revolution of the rotors which are fixed to the rotating shaft 51. The stirring of the fluted bed and its control are effected by the rotating rotor blades and through the selection of their torsion and inclination angles . The stirred fluidized bed is modulated by flow-enhancing rods vertically mounted on the inner part of the milling unit 10 which forces the particles into "confined cavities" and exerts a "pumping venturi" action on them, through the fluctuations of the flow pressures. The particles are separated from the fluidized bed by the continuous rising air curtain generated by the fan 55 and reinforced by a helical lift of the gas-operated fluid created by the cross wobble of the rotating pairs 56-59. In terms of the forces exerted on the particles in the lower area, the centrifugal forces created by the rotating rotors will affect the larger particles as much, driving them towards the outer periphery, while the drag forces will keep these particles suspended in the swirling area, provided that the lifting currents are maintained at constant speed . After the particles decrease in size, due to autogenous impact, friction, shear or erosion, they will reach a scale of reduced size, where the effect of centrifugal forces decreases. Therefore, they will move towards the internal perimeter of the whorl. Having reached the smallest particles, the drag decreases to the point where the dynamics of the flow of the lifting current remains and brings said reduced particles towards the semipermeable rotary means 60. The semi-permeable rotary means act by promoting a more effective internal recirculation of overdrawn particles, through "statistical rejection". In addition, they interfere with the passage of the gas stream by separating the gas bundles and winding them, thus producing directed vertical eddy forces that create additional fine powders mainly through gas wear and shear stress. At higher shaft speeds, the effectiveness of semi-permeable gauge media for grinding is considerably increased. The rotating discs 61, 64 and 67 located in the central openings 70A, 71A and 72ñ of the stationary plates 70, 71 and 72 cause ventup effects and high flow pressures. Thus, superfine grinding is mainly due to increased circular shear forces of a swirl acting on the fine particles. For a given feed speed and rotor speed, there exists for a swirling fluidized bed a maximum density of its particle population that optimizes the effects of the energy of the swirling action when applied to the grinding of said suspended particles. In the present invention, this maximum density value can be obtained, and the effect of the controlled swirl action can be maintained by adjusting the internal design and operating variables. Accordingly, the present invention, utilizing a controlled whirling action of the fluidised bed, provides an effective transfer of the incoming energy through a gaseous operating fluid pair to the actual crushing of the aliquoted particles. improve the performance of existing grinding circuits using ball mills, cylindrical mills, roller mills or other impact devices and introducing the ability of fine grinding and improved superfine at a low cost, the tle energy reformer can be used fluid of figure 3. In this figure, equal numbers refer to the same elements. It differs from the mode of Figure 2 in that the lower zone is used mainly to prepare the fed particles and has only two rotors, and the external recirculation of the product occurs from the intermediate milling zone through the lines 18 'and 19' back to the fluidized bed to yield a final product of fine or superfine powders as specified. The fluid energy reformer utilizes the semipermeable rotating methyls 73 in FIG. 3 as a swirling generator instead of the plate 66 in FIG. 2. In the embodiment of FIG. 2, the fluid energy recirculator utilizes the semi-permeable rotary means 60 for a more effective internal recirculation of the overdrawn products in the initial coarse grinding chamber, and the semipermeable rotary means 63 and 73 and the rotating discs 61, 64 and 67 as swirl generators for better grinding fine and superfine. Superfine grinding in the fluid energy reformer can be suppressed or accelerated by selecting the inserts and internal adjustments of the mill. As a retreatment, the fluid power reformer would take the final products from an existing grinding circuit and use them as a material d ~ > food n. The ultra reformer * "-, &nt; n Figure 4 is used as an inexpensive and inexpensive using the capacity,, -----. -.- .. gives fine, superfine, and enhanced ultrafine of the swirl generators comprising the semipermeable rotary means (80, 82, 86, 89, 92 and 95) and the rotating discs (84, 87, 90, 93, 96 and 99) .The effectiveness of this arrangement is due to the use of stages in which the consecutive recirculation of the oversized products in each stage is affected by the gravity separation through the centrifugal ejection fans (81, 85, 88, 91 and 94) and the transportation of oversized products expelled to the next lower stage through recirculation channels (110A-114A and 110B-114B), thus multiplying the effect of the ascending swirl generators, comprising semi-rotary rotating media and rotating discs arranged in a vertical stack. Coarse initial 11, pair sizes The particle size of the solids in the upflow gas stream are sufficiently reduced, so that any internal recirculation effected by the semi-rotary rotary means becomes insignificant. Therefore, in the ascending stages of the ultrafine reformer, the semipermeable rotating means act only as swirl generators. The increase of the ultra fine size reduction through the use of stages and the consecutive recirc? Ltion a? N under low energy useIt is unexpected. The ultrafine reformer of Figure 4 is a low pressure size reduction device that will operate at high shaft speeds with low energy use. The ultra-thin reformer generates high flow pressures at low static pressures, and thus effectively achieves the reduction from a 270 (56 pin) mesh fed material to a final 4,500 (5 um) or lower mesh size, according to is specified. In Figure 4, like numbers refer to like elements. Above the rotors 58 and 59 are the semipermeable rotary means 80 followed by the stationary plate 101. This follows a sequence of five stages consisting of the centrifugal ejection fans 01, 85, 88, 91 and 94, the methyls rotating c-ern? permeable 82, 06, 89, 92 and 95, the stationary plates 102-106 and the rotary discs b, 84, 87, 90, 93 and 96 forming the annular spaces 102B-106B. The stages have recirculation pathways 110A-114A and 110B-114B. At the top are the superfine and ultrafine separators that include the expulsion fans 97 and 100, the gauge plate 98, the rotary disk pq and the staking plate 107 forming the annular space 10711.

The expulsion fans 97 and 100 expel the particles in the outlets 17 and 16. The lower zone is for the entrance tle feed where the particles fed in through 14 are L5 suspended through the lifting forces of the fan-cent rif ugo 55 'and the swirling action of the crossed rotors in staggered 58-59. Then, the particles are subjected to the swirling action of the semipermeable rotary means 80 and are driven in a series of stages. 0 Apart from the gas inlet 15 in the bottom of the chamber of the power inlet, there are inlet ducts 22-23 that return the gas from the cyclones (after passing to tr-poultry from an additional box of pressure, not shown, to increase the pressure, if necessary). 5 The intermediate zone for super fine and ultra fine grinding is divided into five stages. Each of these steps subjects the incoming particles to the consecutive action of swirl generators comprising rotatable serm permeable means, and rotating discs in ascending order. Each stage has a centrifugal expulsion fan associated with it which serves to eject the fraction of the overdrawn product after it leaves the horizontal swirl of the annular space through the recirculation outlet ducts to the next lower stage. Therefore, the separation by gravity selects the solid fractions and limits the size of the particles entering the consecutive grinding zone by swirling action, with the vertical swirl generator comprising the semipermeable rotating means. The upper zone is for sorting, and has centrifugal ejector fans 97 and 100 that eject the final products through the outlet conduits 17 and 16 to the respective cyclones. If a finer separation of the particle sizes is desired, the products of the outputs 17 and 16 can be fed into a removal unit. The ultrafmo reformer can have a diameter of 61 crn and a height of 2,135 m, with a variable power boost, facilitating shaft speeds from 3,000 to 10,500 RPM. The reformer inserts will be coined in the hollow tube shaft 51. The wall of the unit can be covered with rubber and corrugated with incremental bars to flow each .62 ein 17. 78 cm along the circumference.

If there is built-in flexibility in the fluid energy mill of Figure 2, it should be convenient to use said mill to release the particular components of the material fed in the form of coarse concentrates. such an event, the activity of the swirl action and the recirculation of the mill have to be limited. Accordingly, the turntable 66 (Figure 9ñ) is placed immediately above the semipermeable rotating means 60 (Figure 2) to limit s? function towards internal recirculation in the lower initial coarse grinding zone, while the rotary discs 61 and 64 are removed, together with the semi-rotating rotary means 63 and the centrifugal expulsion fan 62, limiting the performance or closing the recirculation ducts. 18 and 19, and increasing the entrance of the mill gas through 15. The thick concentrates will come out in the conduit 17, while the fine fraction will be expelled through the conduit 16. In the ultra one reformer, the particles smaller ones will move in ascending form at relatively low static pressures (up to 38.1 crn in the water column), and will be exposed to vertically directed very rapid spiral cyclones generated by the semi-rotary rotary media and pass through elevated circular areas of stress cutting generated in the annular spaces. The reduction in particle size will occur through shear stress and gas wear. The centrifugal ejection fan, associated with each stage, will provide the separation by gravity and will facilitate the return of the oversized particles to a subsequent lower stage to be further reduced. Thus, a plaque formation is made for the smaller particles, each advance stage being facilitated by the swirling milling areas generated by the semipermeable rotating means and the rotating discs, and located in a substantially superior position in the ultran reformer. The Urafino reformer can be extended by increasing the diameter of the individual stages. The capacity can be increased also by increasing the number of ascending stages of the unit. Due to the finer feed material and the use of rotors mainly for the mixing of the fed particles, the ultrafine reformer of FIG. 4 can operate at speeds much higher than the fluid power mill of FIG. 2, thus increasing its capacity, while still maintaining its low use of energy. The fed material commonly used in fine grinding is 1.27 crn to 3.175 cm in size, and is obtained at low cost with a variety of crushers. Fine mills are generally air-sweeping mills with fixed classifier systems that return the fraction of particles superimposed to the milling circuit for greater conversion into fine particles. Vanos impact mills cover this function - ball mill, flint tube mill, hammer mill, cylindrical mill, roller mill and other impact pulverizers. Primary milling in all these devices occurs by physical impact of the beater parts on the fed particles. The utility of impact mills and their advantages are well recognized - high capacity operation units and effective size reduction. Its disadvantages are also well recognized - great wear, high energy cost and low, capacity for fine grinding. Attempts to extend the useful scale of the impact mills through the generation of the swirling action are well documented. Impact inol «The swirling action or the impact-grinding mills use rotating beaters with radial beater plates and covering discs. The direct mechanical impact of the particles on the beater plates and the abrasion of the particles through collisions with the surfaces of the apparatus are used for fine grinding. The value of the side effects of the whirling action is well appreciated abrasion by particle collision with particle, wear and shear stress by high velocity gas in the vortex. The uncontrolled swirl zones generated in the impact-abrasion mills are located in the narrow space between the rotor and the cover wall, the mtra-bucket 1 or the mfra-plate areas within the rotor assembly. Roll generation can not be increased by corrugation of the roof wall, and is facilitated by ultrasonic vibrations generated by the attachment of vibrating blades or vibrating disks. Lac deficiencies «The impact mills of action« swirl are high energy consumption, excessive wear, large heat accumulation, low capacity and performance in the case of fine powders. As a result, they represent a difficult scale for the larger operating units. The design of the present invention as in Figure 2 overcomes these disadvantages by using, for the primary size reduction, a controlled swirling action of a fluidized bed located on the circumference of the mill, where the particles are irnpacted with each other, They are driven by centrifugal forces initiated by rotors and effectively transmitted by the gaseous operating fluid. The width of the fluidized bed can be increased by retracting the rotor blades (by shortening the rotor arms) and increasing, consequently, the speed of rotation and the speed of the lifting gas stream. The abrasion occurs through the autogenous collision of the particles at preferential angles to maximize the effect of abrasion at high shear velocities. An efficient coarse and fine grinding is achieved by a very effective internal recirculation of the oversized particles towards the initial grinding zone 11 (Figure 1) using the speed selection effect of the semipermeable rotating media rejecting the particles The slower movement, mainly of a larger size, carried in an upward direction with the gaseous current. In contrast to the prior art, the largest part of the fine and superfine grinding is not carried out in the primary grinding zone. In the present invention, most of the fine and superfine grinding is carried out in the grinding zones by whirling action, wherein the semipermeable rotary means and the rotating discs act as swirl generators and increase the fine grinding, superfine and uH ratin by gas wear and shear at high pressures flow. Therefore, the present invention exhibits low energy use, minimal wear and minimal heat accumulation, and is characterized by a very efficient production of fine powders and ult-refines. The ultrafine reformer as in Figure 4 provides a low-cost ultralin grinding using a new design that utilizes the generation of vertical spiral cyclones for the gas wear of the particles, in combination with horizontal circular shear zones that cut the particles at high flow pressures and low static pressures. This swirl generator system uses rotary semipermeable media to generate the vertical spiral swirl zone and rotating discs to generate a horizontal swirl zone, these two swirl generators acting as efficient size reduction devices for the upward movement of fine particles in the gaseous current and carrying out its crushing with an energy expenditure ba o. At each stage, after the particles pass through the horizontal swirl zone, the oversized particle *: are distributed by gravity separation effected by a centrifugal ejection fan. The superheated particles removed are externally recirculated to the next lower swirl mill zone for further size reduction, the fine particles remaining in the rising gas stream, after the size distribution by gravity separation, pass to the Next milling zone «I swirl it for additional size reduction, and in this way the grinding effect is multiplied through ascending stages of the apparition by means of platform action. The ultimate reformer provides ultra high-performance grinding, low energy and low capital cost. Thickly ground limestone has been an important industrial product used in the construction industry, cement manufacturing and agriculture. Finely ground limestone has been used in foods to encourage and treat water. Ultimate limestone is an expensive product used as a paper sizing agent, pigment, an ingredient for industrial compounds and environmental cleaning. Ultrafine and ultra thin limestone at low cost is very valuable in the desulfurization of gases. Chimney and would facilitate the use of mineral coal with high sulfur content of low cost of high calorific values ,. Limestone icronizatla is valuable in the combination of extended carbon fuels. Superfine dolomite and magnesite are valuable as desulfurant additives for vain heating oils, heavy crude materials or petrochemicals. The present invention, when used to produce micronized mineral carbon / accreted limestone, performs the cleaning of SO2 and nitrogen oxides at cost. With the present system, the mixed mineral coal and the upgraded limestone can be introduced simultaneously through burner nozzles into a combustion chamber. At this particle size, combustion will be instantaneous, proceed with speed similar to oil and natural gas as the fuel fed to the burners. To allow the reaction of SO2 to be completed with the limestone, it is required to recirculate the exhaust gases around the boiler tubes. The complete combustion of the carbon, and the very fine size of the ash particles explain the lack of aggregation and adhesion of these particles, and the fouling, wear and corrosion of the conduction and convection surface must be minimized. The complete combustion of heat reduces the heat losses through the chimney emissions and increases the thermal efficiency of the boiler. In addition, it will produce voltaic ash very low in carbon (less than .5%) and favored as a replacement for premium cement and additive in concrete formulations. During the use of mineral coals with low sulfur content, eg, coal from the tiel no Uyorning Powder, the heat content of the mineral coal is lower when compared with mineral coals with a high content of sulfur from the east and from Midwest. Therefore, using the same amount of pulverized sulfur low carbon (size of 75 μ, 200 mesh) eliminates the nominal capacity of the boiler system, due to the low thermal efficiency of the fuel. Burned. Using coal with a low content of sulfur-containing sulfur (size 40 JJ, 400 mesh) the combustion is greatly accelerated and the nominal capacity of the boiler is improved, due to its increased capacity to burn a large amount of water. fuel per hour. The size of the [volatile ash] joints should eliminate damage to the blades and blades of the gas turbine. As an option, hot coinbusting gases could be cleaned of volatile particulate materials, without significant drop in pressure or temperature, by the use of rotary semi-permeable media. Similarly, sulfur absorbers, lime absorbers, and ash modifiers can be added to hot combustion gases and can be cleaned in a similar manner during the use of rotary semipermeable media. Cleaning can be increased by inserting a centrifugal ejection fan after the passage of the combustion gases through the semi-permeable media. In the event that an extended fuel is used (mixtures of mineral coal with natural gas, heating oil, heavy crude material or water) in a chamber of combustion, the preconditioning of fuel with finished limestone should be sufficient, assuming that the mixtures have been established, what the O2 scrubber is available at the combustion site. The use of macronized mineral coal in extended fuels (heating oil, raw materials, alcohol) destined to be used in utility boilers that burn oil and gas, without a substantial capacity eliminator of said capacity "Je boiler, is facilitated by the increased surface area of the tnicronized mineral coal, -the increased volatility and ease of combustion that give rise to a high volumetric heat release. These extended fuels can be burned using burners that adapt a small excess of air thus avoiding or minimizing the formation of nitrogen oxides. For a SO2 cleaning at low pressure, the most economical means is the injection of micronized limestone either to the combustion zone or to the hot flue gases at the outlet. The result of the present invention will allow the combustion of fuels of high sulfur content, cheap - carbon and ligmta, petrocoque, residual oil, heavy crude materials and asphaltene - due to the cleaning of low cost SO2 through the use of limestone / dolomite are processed. The iron oxide rni chronized can be added to the limestone / dolomite as a fluxing agent to accelerate the completion of the reaction. The high sulfur micronized mineral coal prepared in accordance with the present invention can be used for the addition of waste oils and heavy crude oils, prior to the processing of said mixtures by hydrogenation at high pressure (H-carbon-mineral processes). H-oil, flexicoque), to be converted to high-value petroleum liquids (fuel for transportation, naphtha, diesel) while the sulfur impurities are removed and recovered as a sulfur element. The micronized mineral coal for these purposes shows a particle size of not less than 30 microns (525 mesh) and 20% less than 20 microns (075 mesh). These mixtures of mineralized coal-carbon will accommodate up to 50% of the mineral coal. streamlined in the system. The presence of said mineral coal in the mixture, in the hydrogenation process, results in higher yields of petroleum liquids and improved processing economy. The impure ulral mineral coal and desire in certain applications of coal in extended fuels for internal combustion engines (passenger vehicles, trucks or diesel engines for locomotives). For these purposes, the mineral coal must be reduced to -400 mesh (<40u) then subjected to foam flotation to remove the ash material. The beneficiated charcoal will be dried, and will be subjected to size reduction in the fine-to-fine reformer to the size scale up to < lp. A clean, inexpensive, ultrathin carbide mineral is an important substitute fuel for automobiles in itself, or mixed with gasoline, oil, methanol, MTBE (methyl ether-1-methyl ether), or in the form of a fuel suspension of mineral coal - water. The modification of the surface of solid particles reduced in size is of particular interest for their transport through ducts or in their industrial use as fillers, pigments, absorbers, abrasives, cements, fuels of mineral oil suspension for machines with high-pressure injection, or as intermediate starting materials for further processing. The fresh surfaces created in autogenous grinding, through shear stress and gas wear used in the reduction of particle size in the present invention, deploy reactive sites, either in the form of mechanical radicals (ie, reactive sites resulting from the breakdown of chemical bonds within the molecular regions on the surface of the feeding mats) or in the form of residual valences (that is, active sites resulting from the breaking of the crystalline lattice structures on the surface of said feeding materials). These reactive sites usually have a lifespan and are saturated in the ordinary course of the oceans or trio of oxygen or carbon dioxide present in the air or through water molecules of moisture in the environment. The present invention, with an inert atmosphere (e.g., the working fluid in the mill consists of nitrogen or noble gases, and is operated with complete recirculation of the fluid "work"), allows the in situ modification of the surfaces sprayed. milling and reactive with chemical reagents, chemical compounds both organic and inorganic, producing valuable new materials for trade and industry. For the surface modification in the present invention, the chemical reagents are allowed to evaporate, if they are volatile, within the circulating working fluid of the system, or they can be dispersed as aerosols, if they are high boiling point or solid, and they are diluted by the inert gases present in the working fluid of the system. To saturate mechanical radicals, chemical reagents consist of alcohols (eg, methanol to stearyl alcohol), fatty acids (eg, formic acid to stearic acid) or cellular compounds (eg, vimic alcohol, acid). acplico, ¡-.tJ acplonitri, tile vmilo chloride, styrene, butadiene), amines, ammonium salts, carboxarmides, ureas and epoxides (e.g., ethylene oxide, propylene oxide, epichlorohydrin). For residual saturation valences, the chemical reagents consist of salts (eg, alkali metal halides or stearates, alkaline earth metal or basic metal, ammonium salts). Reduced solids with chemically modified surfaces in situ represent new material compositions that show vane-hunect properties, "altered surface and altered surface tension, reduced coherence in re particles, free flow as dry powders, internal dynamic viscosity when they are suspended in hydrocarbons or in aqueous medium. The modification of the chemical surface in situ in the present invention produces new compositions of modified mineral ore which are useful in the formulation of extended fuels (ie suspensions of mineral coal with alcohol, fuel oils, heavy crude oils). or able to be useful as activated intermediaries. Modified coal products exhibit better dispersion, higher viscosity under a high carbon load in suspensions (eg, coal / water suspension fuels or extended fuels), improved storage stability, and less effort cutting and character degastante. Said modification is important to prepare feed materials for the transport of solid solids, which have biological properties satisfying high solids loads and therefore lower transmission costs per ton of solids. . Limestone, chemically modified, and chemically modified at its surface, in the formulation of high sulfur content bushels (heavy crude, residues, fuels, asphaltenes, high sulfur mineral coals, and petrochemicals) to meet environmental requirements satisfactorily. amount are burned. Other products my croni ados modified on its surface comprise metallic minerals and other minerals that supply products "pre-reactivated" for subsequent benefit by several modes of separation in dry (eg, gravity, magnetic or electrostatic) and aqueous separations (gravity, floating «He foam or agglomeration of oils). The surface modification in accordance with the present invention can be used in the grinding of fillers and pigments. In the case of fillers (eg, carbon blacks, silicas, clays, calcium carbonates), the modified compounds show better dispersion and superior reinforcing characteristics in polypic media. In the case of pigments, the compounds mo «l? They show better dispersion and color resistance (ie, t inte values). To prepare the modified feed materials on its surface for heterogeneous chemical reactions at high temperature, the surface modification of "faster reaction" regimes, and improved yields of the final product, resulting in savings in processing costs. In the case of cement and stone, the modification in situ? of the products my cronizados results in improved storage, faster union and better aging properties. The apparatus of the present invention is compact and lightweight and allows such inoinos to be transported to production sites for the rapa "generation of powders. "" fresh mieronizados. In this way, instant cement can be produced from crushed slag or mimescopa. The ** "currently used slag formulations use slow curing formulas to avoid the" setting "of cement when it is stored .. The method of the present invention will avoid the rotting of ground cement by producing fresh cement at construction sites. Similarly, the quick cure formulas for cement slags can be used in the process of the present invention to produce fresh cement that allows for accelerated construction.The ability to produce fresh cement at sites of construction can result in substantial savings in grinding, packaging, storage and transportation costs. The autogenous mold of the present invention results in a more economical release of desirable components of mineral aggregates that can be achieved with impact mills. This is the case because automatic grinding effects the release of said components at particle sizes greater than impact grinding. With impact grinding, a portion of the desired component is lost in the final parts, and grinding energy is wasted, due to the overrun necessary to achieve the release of the desired component. For the above reason, the present invention can be used economically for processes such as the preparation of mineral carbon feedstocks that require low-cost release of pyrites and related inorganic sulfur compounds. The present invention also allows differential grinding to effect the separation of components into mineral aggregates, provided that the grinding rates of the components are sufficiently different, due to the control of the forces of swirl, shear, and wear in the system. For example, precious metal ores could be concentrated by dry differential grinding of alluvial deposit deposits containing high concentrations of clay. Similarly, gold ores could be concentrated by dry differential grinding of black sands containing gold. The dry differential grinding according to the present invention can be used in the refinement and separation of "washing mineral coals" with high clay content after drying said feed materials before introducing them into the mill. The micronization of solid reagents to powders with a size of 80% less than 30 μ (rnalla 535) and 20% -60% of the smaller ones of 5 μ (rnalla 4500) allows the manufacture at low cost of many micromachined chemical compounds including alkalimetal metal carbides, silLoe and heavy metals (e.g., gc, CaC ?, SiC, r-3C2, Fe3C, U2C, N1C2). This procedure is so low cost that it would not only reduce the current manufacturing costs of these carbides, but also allow new applications for the same. The foregoing discussion generally discloses some of the areas in which the present invention has application. The following are detailed examples of specific uses.

EXAMPLES L. - Micronized mineral coal for the production of dust. The mineral coal is milled according to the invention for direct firing in the combustion chamber of a boiler, where the mineral coal is milled to a particle size of 80% less than 32 μ (500 rnalla). The coal is burned with a short bright flame similar to No. 2 fuel oil or natural gas. The burning of the carbon is very fast and ha > 99%, and dry chimney gas loss is < 6%, compared to a burn of 96%, and a loss of dry chimney gas of 9%, for a pulverized mineral coal of? B ~ μ (rnalla 200) that undergoes combustion in a shallow fluidized bed system . 2. - Clean mineral coal fuel for boiler applications. A mechanized mineral coal fuel and a chronically heated limestone removal agent (eg, limestone or a mixture of limestone and a basic oxide) is used according to the invention for direct cooking in the chamber combustion of a boiler where the romeral carbon is milled to a particle size of 90% or 32 μ (500 nm) and the limestone is returned to a particle size of less than 30 μ (rnalla 525) and 15% of the mi less than 5 μ (4500 mesh). The coal is burned as fuel oil 2, the unburnt coal is > 99%, dry chimney gas loss is < 6%, and the limestone removes > 95% of S02 and N0". 3. - Clean mineral coal fuel for applications in gas turbine. A micronized mineral coal fuel and a limestone removing agent my croni ada each are ground separately according to the invention for the direct heating of a gas turbine, where the mineral coal and the limestone are milled. a particle size of 90% less than 30 μ (rnalla 525), 35% faithful less than 10 μ (2000 mesh) and 15% of the same less than 5 μ (rnalla 4500). Coal is burned with fuel oil No. 2, limestone removes > 95% of SO2 and NO *, and the particulate materials of the combustion process do not wear out or soil the blades or blades of the turbine. 4. - Mineral coal fuel for gasification applications. A mechanized mineralized coal fuel and a controlled limestone removing agent are each separated by the invention for oxygen combustion in a high pressure coal gasification chamber to produce a medium BTU gas, wherein the fuel and scavenger are milled to a particle size of 80% by volume of 32 μ (500 mesh) and 25% of less than or equal to 20 μ (875 mesh). The resulting medium BTU gas can be used as fuel for a combustion turbine, can serve or fuel input for a fuel cell, or can be used as an intermediate in the manufacture of liquid fuels (e.g. , methanol, gasoline, diesel) or chemical feedstocks. Compared to thicker mineral coals, mineralized carbon gives faster combustion rates and results in increased gasifier capacity. 5"- Extended clean fuel: mineral coal / gas.

A mixed fuel consisting of natural gas, modified raw coal, and finer-grained limestone has the solid components each ground separately according to the invention at a particle size of 90% less than 32 μ (500 mesh (and 15% The fuel mixture reduces the cost of congeneration and power generation of combined cycle 6. - Extended clean fuel: mineral coal / oil The fuel is less than 5 μ (4500 mesh) Compared to pure natural gas. It contains sulfur as a sulfur-containing liquid fuel, mineralized coal, and a micronized limestone remover. solids each ground separately according to the invention at a particle size of 90% less than 32 μ (500 mesh) and L5% "I read less than 5 μ (alla 450 (1) and has the two solid components The modified surface area of the surface allows for a higher concentration of solids (up to 70%) in the liquid fuel mixture (with acceptable biological properties) than otherwise possible. - Clean liquid fuel: heavy oil A liquid fuel "containing sulfur with a limiting agent" of limestone has the grinder removed according to the invention at a particle size of 90% less than 30 μ (525 mesh) ) and 20% of the same as 5 μ (4500 mesh), and has the surface of the eliminator chemically moiJi ficada m situ when it moves. The mixture allows the use of fuel oil containing low-cost sulfur, fuel, waste oils and heavy crude oils resulting in heat and / or electricity at lower cost from direct heating boilers or power generators. combined cycle while allowing 90% of so2 and N0X to be removed in situ. 8. Clean coal / water suspension fuel. A mineral coal-water suspension fuel has the mineral coal and limestone removing agent each ground separately according to the invention at a particle size of 90% less than 32 μ (500 mesh) and 15% of the minimum less than 5μ (rnalla 4500), and has the surface of fuel component being chemically modified atu when they are ground. This high-carbon coal suspension fuel shows stable flames and shows fast burning speed, is stable to storage and can smell a coal load of up to 80%. The S? 2 and NOx are removed in-situ during the combustion process by the micronized limestone. Due to its high content of mineral coal and ease of use, coal-water suspension fuels can be a useful means of supplying coal through a conduit, river transport vessels or tankers. Said mineral coal-water liquid mineral carbon fuel will show savings in milling, handling and transportation when compared with conventional coal in lumps. In addition, it provides the ability to store tank terminals. This mineral-water suspension fuel can be used as a boiler fuel for utility or as a feed material for high-pressure coal-fired gasifiers. 9. Control of SQ2 / N0K: co-heating with formation of calcium carbide. The mineral coal and the limestone are ground according to the invention for direct combustion in the combustion chamber of a boiler, where the mineral coal and the limestone are each separately ground to a particle size of - O% -90% less than 30 μ (525 mesh) and 20% -70% of the same than 5 μ (450 mesh), uniformly mixed in a molar ratio of mineral coal: limestone = 4: 1, and injected on the combustion chamber of a boiler. Calcium carbide is formed at the flame temperature of the combustion chamber (16O4 ° C to 1843.3 ° C), which is combined with the oxides of sulfur and nitrogen oxide. SO2 is reduced by calcium carbide to calcium sulfide (CaS) and N0? it is reduced to nitrogen (N2) with an elimination effectiveness of 90% -99%. The formed particles that can be collected downstream in a collecting vessel, greatly reduce (or eliminate) the need for wet removal below the outgoing chimney gases. 10. Control dß SQ2 NOX: Co-baking and Recirculation. The elimination of? 2y N0? created in the combustion of sulfur-containing fuel, by Co-firing the fuel with the grinded limestone removing agent milled according to the invention at a particle size of 80% less than 20 μ (875 mesh) and 20% of the less than 10 μ (2000 mesh) and allowing fuel gases to circulate at 871.1 ° C to complete the unit before leaving the dust bag collector. To the sizes «Previous particle, the O2 and the NOx are absorbed > 99% OR . Control of S02 / N0X: Co-cooking and hydration. The elimination of S? 2 and NO * created in the combustion of sulfur-containing fuel, by Co-firing the fuel with the micromotating limestone removing agent according to the invention to a particle size of 80% less than 20 μ (875 mesh) and 20% the same monkeys as 5 μ (4500 mesh) and treating the resulting flue gases with a fine water mist to further activate the natural agents and lower the temperature of the gases «escape a The scale of 760-982.2 before going to the collector of the dust bag. Applying a sprinkling of fine water with compressed air is converted to the burnt lime (calcium oxide, Ca (0H) 2) in the combustion gases to slaked lime (calcium hydroxide, Ca (0H) 2 that removes any residual SO2 and N0X. The previous method- absorbs SO2 and NO * > 99 +%. 12. Control of S? 2 / N0x: absorbent injection. As an alternative to mineral raw material co-eroded with a solidified limestone removing agent, the finished limestone can be used for absorbent injection into hot gases that swirl above the combustion area. For absorbent injection, the nichromated limestone removing agent is milled according to the invention at a particle size of 80% less than 20 JJ. (rnalla 875) and 20% of it less than 10 μ (2000 mesh). For 6 b Improved absorbent action Micro-raised limestone can be activated additionally through the addition of micromised iron oxide or micronized iron oxide. The previous method absorbs SO2 and 0? > 96%. 13. Control: burned. As an alternative to control N0? , the icronized mineral coal up to an amount equal to 20% of the total weight of the fuel used, is milled according to the invention at a particle size of (=% less than 32 μ (500 nm) and is immediately injected by above the combustion zone for "R-burned", which creates a deficient area of oxygen thus eliminating the emission of residual NXX 14. Improved cement slag, cement slag is made, where the cement rocks eg, limestone, clays, stones / stones, iron ore and / or rubber) are milled according to the invention at a particle size of 90% less than 32 μ (500 nm and 15%) of the same or less than 5 μ (4500 mesh), said cement rocks being mixed and cooked in porn has a finished cement slag. The slag made with superfine and ultrafine cement rock components as specified above is of a superior and more consistent quality than the slag made without such preparation or its reactive components. 15. Improved cements. The cement particles have their chemically modified surfaces in situ while they are ground according to the invention. The modification fi? Cement surface or reinforced concrete improves strength and leads to a faster development of final physical properties in concrete formulations. 16. Improved cement preparation. The reduction of size of cement slag, where the cement product is ground according to the invention to a particle size of 90% less than 30 μ (rnalla 525) and 20% of it less than 5 μ. (rnalla 4500) with 10% of the same less than 2 μ. Cement with superfine and ultrafine particles as specified is deployed with greater strength, superior strength and faster cure in concrete formulations. 17. New Concrete Formulations. The volcanic glasses (eg, volcanic pollen, ash, tuff and nolite) can be converted into micronized glasses, eg, poly a is milled according to the invention at a particle size of 80% or 32 μ (mesh). 500) and 20% of it same as LO μ (2000 mesh). Volcanic vanes, when used in cement formulations, produce a concrete with high early strength and are quickly cured to produce compression shafts of 281 kilograms per square centimeter or more. Volatile ash, a byproduct of a power plant, can be icronized according to the present invention and used in high strength concrete formulations in admixture with cement by plant, silica fume and suitable aggres, producing a concrete with an understanding of 1195.1 to 1406 Kg / cm2. The improvement of the volatile ash has a micronized product of first quality should result in a cost of production more ba or par-electrical energy. 18. Concrete Recirculation. The concrete used is converted to a micronized recirculated concrete mixture according to the present invention through dry milling at appropriate particle sizes for use in new concrete formulations in combination with fresh cement or an additional binder. The ability to recirculate concrete recovered in the construction stage results in significant savings in materials such as transportation, labor costs and labor costs. 19.- New construction materials. The reduction in size of granite, quartz, wollastom or other igneous silicates and rocks, where the pulverized products are milled according to the present invention at a particle size of 90% less than 32 μ (500 mesh) and 20 % of it less than 5 microns (rnalla 4500), said products reacting with a binder to produce new construction materials. Products propad from micronized hard rocks that show supepor strength and other physical properties compared to conventional products in the construction industry, such as mixtures, bricks, blocks, tiles and panels. High strength concrete formulations, prepared with the addition of silica fume and volatile ash as ingredients, show high compression, but lack ductility, become brittle and show decreased shear strength. The replacement of the common aggres used in these formulations with hard rock prepared in accordance with the present invention overcomes this deficiency and produces a high strength concrete with high compression and high shear strength. 20. - Novel insulating materials. Foamed cellular concrete made of polychromised polite or other volcanic glass incorporates the closed cell structures that are inherent in these materials due to the treatment of volcanic gas bubbles. These foams show high insulation values and added structural strength (values f- «Je 30 to 40 and compressive strengths up to 140.6 g / cm2). In addition to being completely "fireproof", micronized ceramic-foam concrete formulations are excellent thermal and acoustic insulators as well as impact absorbers. Such low-cost foams can replace expensive polyurethane foam insulation that releases poisonous gases (e.g., hydrogen cyanide) when exposed to fire. Said foams can also reduce the requirements for steel reinforcement in high lifting structures, can be used for the erection of insulated warehouses of ba or cost, and can serve as foundations for road beds, thus producing maintenance costs associated with damage to roads caused by fluctuations in temperature. 21. - Production of sponge iron carbides.

For the purpose of converting iron ore M to iron carbide powder, the dry iron ore is milled according to the invention to a finished product which has a particle size of 90% less than 32 μ (500 rnayia) and 15% of the same less than 5 μ (4500 mesh). The mineralized iron is mixed with mineralized mineralized iron having a particle size of 90% less than 30 μ (525 mesh) and 15% less than 5 μ (4500 mesh) and the mixture is processed through a reducing furnace to produce fiery carbide The conversion of iron ore to iron carbide at the source of its mining results in a product with a higher iron content (Fß2? 3 with 93.22% vs. F 2? 3 with 69. 94% of Fe), reducing transport costs to the market. Iron carbide is directly usable in the steelmaking electric furnace process, serving as a replacement for waste iron in steel mills, thus allowing the diversion of the costly step of reducing iron ore in pellets in blast furnaces. . For the purpose of converting iron ore to sponge iron, the dry iron ore is milled according to the invention to a finished product having a particle size of 60% less than 32 μ (500 mesh). The micronized iron ore is processed through a reduction furnace with gasified coal prepared from mineralized carbon and oxygen. The resulting sponge iron is a synthetic waste iron useful in the replacement of waste iron for the production of steel in electric furnaces of mills. 22. Micronized mineral coal for blast furnaces. The ground-dried mineral coal milled according to the invention at a particle size of 80% less than 32 μ (500 rnale) can be used directly in conventional blast furnaces for L < -reduction of iron ore by introducing said micronized mineral coal in the nozzles of said ore. Up to 40% of the coke and all the natural gas used as fuel to assist said process can be replaced by high-content, low sulfur mineralized coal, the sulfur originating from said coal being purified to blast furnace slag. . Int roducientJ mined coal L and oxygen to the blast furnace process, up to 90% of the coke can be replaced by high-content sulfur-containing mineral ore prepared in accordance with the present invention and results in a lower cost of production of steel. 23. Recovery of strategic metals. The availability of low-cost mineralized minerals with the present invention and low-cost hydrogen from the gasification of macronised mineral coals with high sulfur content allows the recovery of strategic metals (manganese, nickel, cobalt , tin, titanium, chromium, rnolibdene, tungsten and vanadium) from these lower quality minerals. The lower grade strategic metal ores are milled according to the invention at a particle size of 90% less than 30 μ (alla 525). These chromed powders are processed with hydrogen in a reducing furnace thus releasing the strategic metal particles that can be separated by gravity from the undesirable ore gangue. 24. Dry Separation of Precious Metals. The reduction in size according to the invention can be used in the separation of precious metals from alluvial deposits containing a high amount of clay, black sands or their concentrates and in the recovery of those metals from their refractory minerals. . As an eco-processing, it represents savings in water use and water recirculation and therefore results in a reduction in processing costs for the recovery of precious metals, par- ticularly with deposits located in regions of weather I walk. 25. Release of gold and platinum from minerals. The reduction in size according to the invention can be used to release gold element from hard quartz or silicate minerals., and release platinum element from encapsulating magnetite nodules. Released gold can be benefited by concentrating or by chemical leaching and platinum can be improved by wet magnetic separation. 26. Hydrogen production. The mineral coal and the limestone are each separately ground according to the invention for combustion with oxygen in the presence of water in a high-pressure gasifier to produce a mixture of carbon monoxide (CO) or hydrogen ( H2), where the mineral carbon is milled to a particle size of 80% less than 32 μ (500 mesh) and the limestone is ground to a particle size of 80% less than 30 μ (525 mesh) and 25% of it less than 5 μ. The use of micronized mineral carbon reduces the reaction time and allows for better control of the reaction, thus reducing the cost of hydrogen production below the cost of using higher carbon feed material. The above represents one of the lowest cost methods of hydrogen production. 27. Cleaning of combustion gas for turbines heated with direct coal. The combustion gases of a turbine heated with direct mineral coal that burn 75 μm mineral coal (rnalla 200) pass horizontally through rotary semipermeable means according to the present invention. The semipermeable means are an assembly with a rotating screen placed between the islet of the combustion chamber and the gas turbine, with a trap below the rotating sieve. Most of the hot-melted ash particles from the coal are removed from the gas stream with negligible pressure loss and reduction in temperature, and the remaining salt in the gas stream is reduced in size in such a way that Do not damage the blades or blades of the turbine. Similarly, rotary semi-permeable media can be used to perform hot-gas cleaning when the sulfur absorbers, alkali absorbers or ash modifiers are injected into the hot gas stream to prevent wear and corrosion of the turbine. gas and to comply with the standards «broadcast to the environment. The effectiveness of the cleaning can be increased by the additional use of a centrifugal fan after the passage of hot gases through the rotating semi-permeable media. 28. Cleaning of flue gas for PFBC. The combustion gases that leave a combustion chamber of the fluidized bed under pressure contain ash and alkali particles are cleaned allowing the hot gases to pass through an arrangement containing rotatable semi-rotary media in accordance with the present invention, before entering the gas turbine, thus eliminating the need for costly and fragile ceramic cross-flow filters. The cleaning effectiveness can be increased by using a centrifugal ejection fan below the semipermeable rotating media to remove residual solids in the hot gas stream. 29. Cleaning of combustion gas for boilers heated with mineral coal. Rotary semi-permeable means in accordance with the present invention are made tungsten and are placed horizontally in the combustion chamber within the zone "the tubes" the boiler "a boiler heated by mineral oil that burns off the Bon mineral 75 μ (200 mesh). Large embers are rejected by the rotary semi-permeable means and retained within the combustion chamber long enough to transport additional heat to the boiler tubes so that the carbon burn increases to 99% and the loss of the Dry chimney gas is reduced below 8%. 30. Manufacture of calcium carbide. Limestone and mineral coal are ground separately according to the invention, each at a particle size of 80% less than 30 μ (525 mesh) and 20% ~ 60% thereof less than 5 μ (4500 mesh) ). A rhino chromed coal mineral flame is initiated in a cyclonic combustion chamber and its temperature is maintained at a scale of 1, 593 ° C ~ 1, 843 ° C. The micronized limestone and the mixed mineral coal are uniformly mixed in a molecular ratio of limestone: coal = 1: 4, and the mixture is blown into the combustion zone where calcium carbide is formed. The calcium carbide formed in this way is removed by a stream of air through an assembly in which the reaction products are cooled to 148.8 ° C, after which the calcium carbide powder will be heated to a temperature of 70 ° C. separates from the 7ñ Current of incoming gas in a cyclone. The above description describes, by way of illustration but not limitation, preferred embodiments of the invention. Equivalent variations of mo < The described methods could be done by those skilled in the art. Said variations, modifications and equivalents are within the scope of the invention as indicated with greater part iculapity. The following claims, when interpreted to obtain the benefits of all equivalents to which the invention relates.

Claims

NOVELTY OF THE INVENTION CLAIMS 1. - A method for the dry grinding of solids, which includes the steps of: directing solid particles generally upwards to a grinding zone "ie swirl; and milling the solid particles directed upward in the swirl milling zone by passing a portion of the particles through the swirl milling zone, the millstone. Finally, a swirling milling stage disposed in a successive manner comprises passing particles upwardly to trirds of at least one of the rotary semipermeable means and a defined annular space or a stationary plate with a flat surface with a circular aperture in it. the same and a disk with openings does not circulate rotating in the circular opening.
2. The method of conformity with area 1, further characterized in that the step of passing parcels upwards through said semipermeable rotating means comprises passing particles through an assembly which has a rotating screen.
3. The method according to claim 2, further characterized in that the step of passing particles through said rotary screen comprises passing particles to tr-birds of a screen no thicker than 2.5 mesh.
4. The method according to claim 3, further characterized in that the tarniz has a mesh size in the range of 2.5 to 60"5. The method according to claim 4, characterized by" Jemas por-que the sieve has a mesh size on the scale of 4 to 10 »6.- The method« conformed «with the re? v? n« J? cation L, also characterized by the step of passing through- the particles through the annular space comprises pass-through The particles through an annular space that has a width of 1.27 to 15.24 centimeters. 7. The method according to claim 1, further characterized in that each step comprises passing the particles through rotary semipermeable means and subsequently through the annular space. 8. The method according to claim 1, further comprising the step of making an external recirculation recirculated by rotation of a centrifugal ejection fan downstream of the rotary semi-permeable means and providing a recirculation channel. Receptive particle of the rotating ejector fan and having a low exit from at least one stage of a rotating ejection. 9. The method according to claim L, also characterized because it comprises the step of removing particles above the grinding zone. 10. The method according to claim 9, further characterized in that the removal step comprises rotating at least one centrifugal ejection fan downstream of the milling step (at least one). Ll.- The method of compliance with the claim 1, further characterized in that it comprises the step of initially injecting coarse particles into fine particles before directing the fine particles to the grinding zone. 12.- The method according to the rei indication L, also characterized because it comprises the step of micronally molding coarse and fine particles feeding solids to the chamber, forming KÁI? fluidized bed of solids in the chamber directing upwards into the chamber and creating a controlled trawl in the grinding zones of the fluidized bed to effect autogenous grinding. 13. The method according to claim 12, further characterized by comprising the recirculation step internally incertando half rotary semi-rotary media in the initial coarse grinding zone, and rotate dLchos semipermeable media at a sufficient speed to prevent the passage of a portion of the particles overdrawn through it and internally recirculate said particles to the initial grinding zone of coarse particles. 14. The method according to claim 12, further characterized in that it comprises the step of externally recirculating particles to the fluidized bed. 15. The method of conformity with claim 1, comprising a plurality of stages of swirl milling and further comprising the step of recirculating externarnente particles to a previous stage. 16. The method according to claim 9, further characterized in that the removal step compresses and removes in two stages of vertical removal, ready to remove particles of small size successively. 17. The method according to claim 12, further characterized in that the step of creating a controlled trailer comprises the use of rotors. 18. The method according to claim 7, further characterized in that it comprises rotating semi-rotary half-rotary means and rotary disk on a common arrow. 19. The method according to claim 1, characterized by "lernas" because the grinding step is carried out in a non-reactive atmosphere in the presence of a chemical reagent to effect controlled surface modification. 20.- A procedure to treat combustion gases for the removal "Je S0? and N0X in it, I understood in Jo the steps of: grinding coal and limestone at particle sizes of 70% -90% under 30 μ and 20% -70% of them under 5 JJ; introducing said ground mineral coal and ground limestone into a molecular ratio of at least 4: 1 to a chamber at a temperature of 1.565 ° C and 1, 843 ° C in order to form CaC2; and mix the aC2 formed with combustion gases to remove SO? and NO * of the combustion zones by the formation of CaS and 2. 21. An apparatus for the dry milling of solids comprising: means for forming a swirl mill zone that includes at least one milling stage e Removed vertically or in a successive way to grind solid particles; and means for directing solid particles generally upwards to the swirl milling zone; wherein said swirl milling step (at least one) comprises at least one of the rotary semipermeable means and means for forming an annular space comprising a flat surface stationary plate having a circular opening therein and a disk without circular openings rottopo in the circular opening and where the medie-. rotary semipermeable and annular space are configured to pass a portion of the particles directed upwards through the same; and wherein said swirl milling step contains a rotating fan-ejector below the rotating medium to distribute the size of the particles directed upwards. 22. The apparatus according to claim 21, further characterized in that the semipermeable means 02 The rottopes comprise an assembly that contains a rotating screen. 23. The apparatus according to claim 22, further characterized in that the rotating tarniz comprises a tarniz no thicker than maL La 2.5. 24. The device "Je co or mu" Jad with claim 21, further characterized in that the device has a size in the scale of 2.5 to 60. The device according to claim 23, further characterized. because the tarniz has a size on the scale from 4 to 10. 26.- The apparition according to claim 21, further characterized because the annular space has a width of 1.27 to 15.24 centimeters. 27.- The device in accordance with the claim 21, further characterized in that each stage comprises semipermeable means and means forming the annular space and the centrifugal elimination fan downstream of the serniperrneab means Le. 28.- The apparatus in accordance with the claim 21, further characterized in that I comprise internal recirculation means including means for rotating said rotary semipermeable means at a speed sufficient to prevent passage of a portion of the particles therethrough. 29. The apparatus according to claim 28, further characterized in that it comprises an external recirculation device "comprising a centrifugal ejection fan downstream of the rotary semi-permeable means and a recirculation channel for the particles of the ventilator. rotating ejection and having an outlet below of at least one swirl milling stage. 30.- The apparatus according to claim 21, further characterized in that it comprises means for removing particles above the grinding zone »31.- The apparatus in accordance with the claim 30, further characterized in that the removal means comprises rotating at least one centrifugal ejection fan downstream of the swirl milling stage (at least one). 32.- The device in accordance with the rei indication 21, characterized in that it comprises means for grinding my cialrnent coarse particles into fine particles before directing the fine particles towards the milling zone of rernol no. 33.- The device in accordance with the rei indication 31, further characterized in that it comprises means for massively circulating means for feeding solids to a chamber, means for forming a fluidized bed of the solids in the chamber including means for dipping air upwards into the chamber and means for create a controlled swirl in the fluidized bed to perform autogenous grinding. 34. - The apparatus according to claim 33, further characterized in that it comprises means for internally recirculating particles to the fluidized bed. 35. The apparatus according to claim 21, further characterized in that it comprises a plurality of grinding stages and means for externally recirculating particles to a previous stage "36.- The apparatus in accordance with the claim 30, further characterized by the fact that the removal methods comprise means to remove in two stages of vertical removal arranged to remove particles of varying sizes as small as possible. 37. - The conformity apparatus with claim 33, further characterized because the means to create remo1 Lno controlled comprise the use of rotors. 38.- The apparatus in accordance with the claim 27, further characterized in that it comprises means for rotating the rotary semipermeable means, the rotary disk and the centrifugal elimination fan on a cornun arrow. 39.- A method for the dry milling of solids, comprising the steps of feeding solids to a chamber, -forming a fluidized bed of solids in the chamber directing air upwards in the chamber and creating air movement towards The centrifugal forces through the chamber to cause the solids to move to the periphery of the chamber, said bed being formed into a ring of wide floating solids at the periphery of the chamber.; and creating and controlled swirling in the fluidized bed to carry out automatic grinding of the solids while avoiding the direct impact of the mill machinery on the solids in the grinding zone «Jel wide free floating ring. 40.- The method of compliance with the claim 39, further characterized by the fact that it comprises the passage of reyver particles above the fluvial bed. 41.- The method for the dry grinding of solids, which includes the steps to feed solids to a chamber; forming a fluidized bed of solids in the chamber directing air upwards in the chamber; create a controlled whirlpool in the fl uid bed «Jo to carry out autogenous grinding, remove the particles by arpba from the fluidized bed and recirulate the particles removed in the fluidized bed» 42.- The method of complying with the claim 40, characterized by the fact that the removal step comprises at least one centrifugal ejection fan running downstream of the fluidized bed. 43.- The method of compliance with the claim 41, further characterized in that the recirculation passage comprises spinning a centrifugal ejection fan downstream of the fluidized bed and providing a recirculation channel for particles of the rotating fan and having an outlet to the fluidized bed. 44.- A method for the dry milling of solids, comprising the steps of feeding solids to a chamber; forming a fluidized bed of solids in the chamber by directing air upwards into the chamber; create a controlled swirl in the fluidized bed to effect grinding; and removing particles above the fluidized bed in two stages of removal verfically arranged to remove particles of successively smaller sizes, 45.- The method of compliance with the claim 39, further characterized by the fact that grinding is carried out in a non-reactive atmosphere in the presence of a chemical reagent to perform a controlled surface modification. 46.- A method for dry grinding "Je solí" Jos that includes: rne «J? O to form a chamber; rne «J? o to feed solids to the chamber; means to form a fluvial bed «J? za < of the solids in the chamber including means for «Jipgir air up in the chamber; means for creating centrifugal forces to generate air movement towards the sides in the chamber to force the solids to move towards the periphery of the chamber to form the fluidized bed in a large free floating ring; and means to create a controlled swirl in the chamber to perform autogenous grinding of the solids while avoiding the direct impact of the mill machinery on the solids in the large free floating ring of the mol zone in "Ja . 47. - The apparatus according to claim 46 further characterized in that it comprises means for retracting particles above the fluidised bed. 48.- An apparatus for dry milling "Solid solids comprising: means for forming a chamber; means to feed solids to the carnara; means for forming a fluidized bed of the solids in the chamber including means for directing air upwards in the chamber and means for creating a contoured swirl in the fluidized bed for autogenous grinding; means for removing particles above the fluidized bed; and means for recirculating the removed particles in the fluidised bed. 49.- The apparatus in accordance with the claim 47, further characterized in that the removal means comprise at least one centrifugal centrifugal fan below the fluidized bed. 50.- The apparatus of confrm «Jad with the rei indication 48, further characterized in that the recirculation means comprises a rotary centrifugal ejection fan downstream of the fluidized bed and a rotary fan particle receiving recirculation channel and having an outlet to the fluidized bed. 51.- An apparatus for the dry milling of solids comprising: means for forming a chamber; means for feeding solids to the camera; means for forming a fluidized bed of the solids in the carcase including means for directing air upwards in the chamber and means for creating a controlled swirl in the fluidized bed to effect autogenous grinding; and means for removing * particles above the fluidized bed comprising means for feeding vertically disposed removal steps to remove particles of successively smaller sizes. 52. - The apparatus according to the rei indication 46, also characterized in that the means to create a contoured swirl comprise rotors gpablos. 53.- A method for cleaning "particles of a stream" comprising the steps of: spinning at least half permeable means; directing at least one gas stream with solid particles through rotating permeable media (at least one); and remove particles that go through the rotating semipermeable media (at least one). 54, - The method of conmi ad with the rei indication 53, furthermore, because the step of directing a stream of gas with particles through said rotary semi-permeable means (at least) comprises directing the gas and particle stream through an assembly containing a rotating sieve. . 55.- The method of compliance with the claim 54, further characterized in that the step of directing a gas stream with particles through said rotating screen comprises directing a stream of gas with particles through a no thicker screen than 2.5. 56.- The method according to claim 55, further characterized in that the sieve has a scale size in the range of 2.5 to 60 »57.- The method in accordance with the claim 55, further characterized in that the tarniz has a mesh size in the scale of 4 to 10 »58.- An apparatus for cleaning particles of a gas stream comprising: at least one rotatable semipermeable medium; edios to direct a gas stream with solid particles through rotating permeable serm media (at least one); means for removing particles that do not pass through the semi-permeable rotary media (at least one); and means for removing particles which pass through the rotating, serine means by directing said gas stream through a "vent". The "centrifugal" ejection. 59. - The device «Je trust in the claim 58, further characterized in that the rotatable semipermeable means (at least one) comprises an assembly containing a garat or rao screen. 60.- The apparatus of form with the reiviication 59, further characterized in that the rotatable screen comprises a tarniz not larger than 2.5 mesh. 61.- The apparatus according to claim 60, further characterized in that the screen has a mesh size in the range of 2.5 to 60. 62. - The apparatus according to claim 60, further characterized in that the screen has a size "Je rnalla on the scale of 4 to 10.