Conveyors: fluid current – Processes
Reexamination Certificate
2001-08-07
2003-08-26
Dillon, Joseph A. (Department: 3651)
Conveyors: fluid current
Processes
C406S198000, C406S092000, C406S093000, C406S191000
Reexamination Certificate
active
06609857
ABSTRACT:
FIELD OF THE INVENTION
The present invention relates to a method for mixing a pulverulent material in a main gas flow with a view to achieving uniform distribution of the pulverulent material.
The present invention also relates to a device for carrying out the method, comprising a gas duct for the main gas flow with vortex-generating means and an introducing means for introducing pulverulent material in dispersed state with a carrier gas flow.
The invention is especially intended for use in gas cleaning with a view to separating gaseous pollutants. The pulverulent material is selected so that it can absorb or adsorb undesirable gas components.
BACKGROUND ART
In gas cleaning, there are frequently two completely different tasks. On the one hand, particles are to be removed from a gas flow and, on the other hand, certain gas components are to be removed. Relatively simple techniques of separating particles are well established since the beginning of the century, but separating gas components is a considerably more complicated operation.
In situations where the gas flow is small and not heavily polluted, for instance fractionated condensation or a membrane technique can be used, but in technical contexts, it is often necessary to choose a roundabout method so as to bind any existing gaseous pollutants to particles, powder or droplets, and then separate the particles.
When introducing absorbing or adsorbing particles, the accessible surface thereof and the mixing in the gas flow are of great importance. It is thus a matter of introducing as finely divided particles as possible and distributing these as uniformly as possible. Moreover, a high relative speed between particles and gas is desirable. The turbulence, in a wide sense, should thus be high. By turbulence is here and below meant every motion in the gas that deviates from the average motion of the flow, thus also macroscopic vortices etc.
To achieve this mixing effect, particles are frequently introduced at a velocity which significantly deviates from the velocity of the gas. In a scrubber, fine droplets are injected at high velocity in a slowly flowing gas. In a venturi, gas flows at high velocity through curtains of liquid or a mist of liquid. This utilisation of differences in velocity is not possible to the same extent when a dry sorbent is introduced. In such situations, the homogenous distribution in the gas will be particularly important.
An example of such a technique is disclosed in EP-200 695, where moistened gas is conducted upwards through a vortex-generating device past an introducing means through which a pulverulent absorbent is introduced into the flowing gas in a direction of motion essentially opposite to the main flow direction of the gas. However, the publication does not provide any information about a suitable design of the introducing means.
OBJECT OF THE INVENTION
An object of the invention is provide a method and a device for good contact between a pulverulent material and a flowing gas by effecting a distribution, which is as uniform as possible, of the powder in the gas flow and at the same time achieving a high relative motion between particles and gas.
SUMMARY OF THE INVENTION
The present invention relates to a method for mixing a pulverulent material in a main gas flow with a view to achieving uniform distribution of the pulverulent material. The turbulence in the main gas flow is increased in a vortex-generating zone. The pulverulent material is introduced into the main gas flow, in a mixing zone, with a carrier gas flow whose net motion during introduction is essentially opposite to the main gas flow. The mixing zone is positioned downstream of the vortex-generating zone and in the vicinity thereof. The zones can be slightly overlapping.
In the method according to the invention, the carrier gas flow with the pulverulent material is given, in a rotational zone, a helical motion, whose symmetry axis is essentially parallel with the direction of flow of the main gas flow. The carrier gas flow with the pulverulent material is introduced into the mixing zone in the form of a divergent hollow cone.
The present invention also relates to a device for carrying out the method, comprising a gas duct for the main gas flow with vortex-generating means and an introducing means for introducing pulverulent material in dispersed state with a carrier gas flow.
The introducing means comprises a cylindrical pipe with an open end and a closed end, a tangential inlet in the vicinity of the closed end of the cylindrical pipe, a divergent axial outlet at the open end of the cylindrical pipe and an insert adjacent to the axial outlet. The divergent axial outlet, comprises a truncated conical jacket, and a centred insert adjacent to the axial outlet is so adapted that an annular opening forms between the truncated conical jacket and the insert.
GENERAL DESCRIPTION OF THE INVENTION
With a view to establishing a good contact between a pulverulent material and a gas when introducing the pulverulent material into a gas flow, a uniform distribution of the pulverulent material in the gas flow is most essential. Therefore, it is suggested according to the present invention that the pulverulent material be dispersed in a carrier gas, the flow of which is essentially smaller than the main flow, for instance 1-10%, preferably 1-5%, of the gas to be cleaned. The carrier gas flow with dispersed pulverulent material, below referred to as carrier gas flow only, is passed at a velocity of 10-25 m/s through an inlet, comprising a slot-shaped opening, tangentially, into a rotational zone consisting of a cylindrical pipe. The carrier gas flow is given a helical motion in the rotational zone, preferably with a constant diameter, in a first part of the rotational zone, and with an increasing diameter, in a second part of the rotational zone.
The slot is positioned at one end of the cylindrical pipe and is oriented in such a manner that its longest extent is parallel with the axis of symmetry of the cylindrical pipe. The extent, in the radial direction, of the projection of the inlet is significantly smaller. The area of the slot is 0.1-0.4 times the cross-sectional area of the cylindrical pipe, preferably 0.2-0.3 times the cross-sectional area of the cylindrical pipe. The ratio of the length of the slot to the length of the cylindrical pipe should be 0.1-0.6, preferably 0.3-0.5.
The shape of the slot is of decisive importance to the invention owing to the fact that a considerably more uniform distribution, seen as a function of an angular coordinate round the outlet, of the pulverulent material is achieved. Prior-art devices have a marked asymmetry round the outlet of the introducing device.
The carrier gas flow is passed to the inlet through a duct which gradually passes from a circular or square cross-section to said slot shape. The velocity of the carrier gas is then kept constant or is slightly increased.
The carrier gas flow is adjusted to the need for pulverulent material that exists so that a diluted transport can be carried out with up to 2 kg of powder, preferably 0.1-1.5 kg of powder, per cubic meter of carrier gas.
The length of the cylindrical pipe is 1 to 5 times, preferably 2 to 5 times, its diameter. The cylindrical pipe is closed at one end, adjacent to the slot-shaped opening, preferably with a bottom comprising a conical part or the like, the top being directed inwards. At the other end, the pipe changes to the form of a truncated cone jacket diverging away from the pipe.
The conical part should have a height which is 0.2-0.6 times the diameter of the cylindrical pipe and a diameter which is 0.6-1.0 times the diameter of the cylindrical pipe. The shape of this bottom part can be slightly modified without significantly impairing the function, but should have a central elevation, such as a tip.
The truncated conical jacket should have a length which is 0.5-3.0 times the diameter of the cylindrical pipe and a maximum diameter which is 1.4-4.0 times the diameter of the cylindrical pipe.
To obtain a carrier gas flow in the fo
Hjortstam Magnus
Johansson Lars-Erik
ABB Fläkt Aktiebolag
Burns Doane Swecker & Mathis L.L.P.
Dillon Joseph A.
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