CA2009183A1 - Method and a device for treating or mixing components in gas or liquid streams - Google Patents
Method and a device for treating or mixing components in gas or liquid streamsInfo
- Publication number
- CA2009183A1 CA2009183A1 CA 2009183 CA2009183A CA2009183A1 CA 2009183 A1 CA2009183 A1 CA 2009183A1 CA 2009183 CA2009183 CA 2009183 CA 2009183 A CA2009183 A CA 2009183A CA 2009183 A1 CA2009183 A1 CA 2009183A1
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- fluid
- mixture
- insert
- reaction products
- substances
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Abstract
Title:
A method and a device for treating or mixing components in gas or liquid streams.
ABSTRACT
A method of, and apparatus for, cleaning contaminated gas or liquid streams by intensive mixing of the contaminants with neutralizing and/or absorbing agents, using repeated compression and expansion whirls (a,b,c) produced by conical constructions inside a cylindrical housing (2).
A method and a device for treating or mixing components in gas or liquid streams.
ABSTRACT
A method of, and apparatus for, cleaning contaminated gas or liquid streams by intensive mixing of the contaminants with neutralizing and/or absorbing agents, using repeated compression and expansion whirls (a,b,c) produced by conical constructions inside a cylindrical housing (2).
Description
2 2C9~9~ ~33 This invention relates to a method of removing, possibly by chemical binding, contaminants in a fluid, such as a gas or liquid stream, in which the fluid is contacted with neutralizing and/or absorbing su-bstances and the resulting mixing or reaction products are separated.
One example of an appliance wherein this method is performed is the cyclone-shaped reaction chamber(s) wherein absorption/neutralizing substances are contacted with contaminated flue gases of refuse incinerators.
In these, the cyclones' first function is the capture of sparks entrained from the incinerators in those cases wherein cloth filters are used to remove fly ash and reaction products from the 1ue gases, before said flue gases are discharged into the atmosphere through a chimney stack. The contact between the flue gases and the absorption/neutralizing su~stances added thereto in the cyclones is such that a part of the acid components from the flue gases are bonded and neutralized. Tests have shown that the neutralizing effect inside the cyclones is higher than that of the neutralizing layer formed on the downstream filter cloths. Yet there is evidence that, in the case of heavy loads with acid components as regularly occurring in practice in flue gases, the total efficiency of upstream cyclones and downstream cloth filters, is insufficient to meet the emission standards recently laid down in national and international regulations.
One example of an appliance wherein this method is performed is the cyclone-shaped reaction chamber(s) wherein absorption/neutralizing substances are contacted with contaminated flue gases of refuse incinerators.
In these, the cyclones' first function is the capture of sparks entrained from the incinerators in those cases wherein cloth filters are used to remove fly ash and reaction products from the 1ue gases, before said flue gases are discharged into the atmosphere through a chimney stack. The contact between the flue gases and the absorption/neutralizing su~stances added thereto in the cyclones is such that a part of the acid components from the flue gases are bonded and neutralized. Tests have shown that the neutralizing effect inside the cyclones is higher than that of the neutralizing layer formed on the downstream filter cloths. Yet there is evidence that, in the case of heavy loads with acid components as regularly occurring in practice in flue gases, the total efficiency of upstream cyclones and downstream cloth filters, is insufficient to meet the emission standards recently laid down in national and international regulations.
3 ~9~33 The alternative option would be for wet flue gas cleaning, with which these standards can be met.
The consequence of that, however, is that it will increase investments by a factor of 2 or 3 as a result of the elaborate processing involved in this methocl, on top of which, in most cases, additional waste water purification is required.
It is an object of the present invention to improve the dry flue gas purification with cyclones in such a manner that emission standards are met and expected by even lower valuas will result, thus achieving a particular improvement in the solution of environmental problems in respect of, for example, refuse incinerators.
This can be realized at quite acceptable prices at that.
To that effect, according to the present invention, by application of the features reclted in the characterizing clause of claim 1, the components entering the cyclone are not only centrifugad but the light fractions in the flue gases, including the major part of the gaseous acid components, are prevented from diffusing directly through the flue gas stream to the cyclone exit, so that the contact with the neutralizing heavier components is too short.
According to the present invention, the light fractions in the flue gases, together with the heavier fractions are jointly centrifuged after entering the cyclones, while in contrast to the situation in the 4 2~ 33 present design within cyclones, increasingly intensive contact is enforced by increased concentration and at the same time strongly increased velocity by means of an inverted cone provided preferably in the centre of the cyclone. This forces the light (i.e. the acid) com-ponents in the flue gases to react with the neutralizing substances immediately, intensively and for a prolonged period of time.
By repeating the inverted cone construction, as indicated above, at a lower level, there is obtained a reversal of the flue gas motion, whereby the descending high-velocity whirl is converted into a rising initially expanding whirl of relatively low velocity. According as the whirl thereafter at higher level again approaches the centre of the cyclone, the acceleration and the concentration are considerably increased. The heavier fractions in the strongly accelerated rising whirl are again mixed intensively with the light fractions (including those to be neutralized) in the gas stream. Repetition of the above inverted cone constructions in the interior of the cyclone will increase the effect of mixing and neutralizing acid components in the flue gases. Moreover, the effect of mixing and chemical reaction can be increased per "floor" by rendering the distance between the internal cones adjustable. In this manner, substantially higher vortex speeds (and hence higher mixing efficiency) can be achieved than provided initially (i.e. upon entry 2Q~9~83 into the cyclone). The variation of the distance between the internal cones can be controlled by coupling the adjustment to e.g. the measured acidity of the flue gases prior to their discharge to the chimney stack.
The last fixed cone can be extended to a cylindrical bin where the vortex can be reduced to such a low velocity - by properly dimensioning the cylinder - that solid components (fly ash, chemical reaction products and possible excess of neutralizing substances) are separated.
The purified gas stream is removed through a central exhaust within the lowest cylinder. Naturally, exhaust from the installation need not necessarily take place in the above manner. It is also possible for instance to select tangential exhaust from the circumference~
Another possibility could be: exhaust from the top of the device in the case where one "floor" would be sufficient to attain the required efficiency. IE an enlargement of the lowest cone is selected, as mentioned abo~e, there is automatically produced a collectin~ bin which can selectively perform a number of useful functions:
a) temporary storage of separated and/or reacted products prior to discharge into a container;
b) return of the separated products to the inlet of the cyclone or one of the floors, to thereby allow any neutralizing material not yet entirely reacted to participated again in the process.
6 Z~)9~L133 Some embodiments of apparatus according to the present invention will now be described, by way of example, with reference to the accompanying drawings, in which:
Fig. 1 diagrammatically shows the ope~ation of a conventional cyclone;
Fig. lA is a cross-sectional view according to the arrow A in Fig. l;
Fig. 2 shows in top plan view the operation of a cyclone according to the present invention;
Fig. 3 is a diagrammatic cross-sectional view of the cyclone shown in Fig. 2;
Fig. 4 is a view similar to E'ig. 3 but showing the top of the cyclone illustrated in Fig. 3 and its operation in more detail;
Fig. 5 is a view similar to Fig. 4, but in a further stage of the fluid motion;
Fig. 6 is a similar view showing fluid motion subsequent to the situation shown in Fig. 5; and Fig. 7 shows the completion of the process by collecting reaction products.
Fig. 1 is a cross-sectional view of a conventional cyclone construction, showing the centrifugal separation of heavier fly ash, neutralizing substances and reaction products via the descending vortex (a) and the rapid diffusion of the light (e.g. acid) components (b), including light solid components of the flue gases, which are 7 Z~ 83 subsequently discharged to filters upstream of the chimney stack. The flue gases mixed with absorbing and/or neutralizing substances are introduced tangentially through 1 into the cylindrical portion 2 where they are contacted with each other. The heavier components, such as fly ash and a part of the reaction material, descend via vortex (a) into the discharge or collecting hopper 8. The lighter fractions, such as acid gases, light fly ash particles and residual reaction material, are separated from vortex (a) directly at the open bottom of exhaust pipe 11 and disappear through vortex (b) in fractions of seconds through pipe 11. The reaction time available for neutralizing undes:irable components is therefore very short. In those cases where the percentage of undesirable chPmical components in the gas stream is high, the added neutralizing and/or absorption agent will react insufficiently. Thus the composition of the flue gases discharged via 11 will fail to meet the recently raised emission standards.
A substantial excess of neutralizing agent has proved unable to solve the problem and moreover creates two additional problems:
- the extra cost connected with the discharge of substantial amounts of residues to dumping sites which - can accept these materials only at increase rates.
8 2Q~ 8~
The residues, in fact, require additional provisions at the dumping sites to control the water economy and quality.
It is an object of the present invention to avoid these drawbacks and to positively improve the result in a manner as shown in principle in Figs. 2-7.
As shown in Figs. 2 and 3, flue gases are introduced tangentially through 1 into the cylinder 2 - the cyclone -possibly with added neutralizing substances. The additions of these and/or other substances, naturally, can also take place after the entry, e.g. through the apex of cone 4 or the base of cone 5.
Undesirable components, together with the heavier components (fly ash and neutralizing substances) are centrifuged in cylinder ~, while in contrast to the situation described for the cyclones of the prior art, increasingl~ intensive contact is promoted by increased concentration and at the same time strongly increase velocity of vortex (a) by means of an inverted cone 4 provided (preferably) in the centre of the cyclone.
As appears from the detail shown in Fig. 4, the centrality suspended inverted cone 4 products intially the accelerated descending vortex (a) shown in Fig. 3.
This vortex is deflected 180 from its original direction by the bottom of cone 5 and has as the only way out the cylindrical cross-section II, being substantially larger than cross-section I, in other words, besides 2C~9~ 33 a reversal through an angle of 180, a sudden expansion takes place. This is highly favourable to additional vortex effects/ resulting in additional mixing and enchanced chemical reactions. The cyclonic gas motion cannot become suddenly rectilinear, for a new vortex (b) is formed, as model tests have shown, ~hich ascends according to the dotted lines shown in the drawings between the two cones at in'creasingly higher vertical and tangential speed = mixing speed = chemical reaction speed. The absorption/neutralizing agent is enforced to react for the second time.
Fig. 5 shows the same cyclone detail as Fig. ~
with a representation o the gas motions which are deve~
loping in a stage further than that shown in Fig. 4.
From cross-section III, a substantially 180 reversal of gas motions takes place again. It should be noted that a 180 reversal, as used herein, should be construed to mean the eventual effect in a vertical sense. The actual gas motion remains tangential, resulting a vortex ascending or descending, as a whirl, perpendicularly.
In cross-section III, such a 180 reversal takes place again. Vortex (c) is formed, resulting-in very high speeds, in other'words, a very high mixing effect and very high chemical reaction speeds. The absorption/neutralizing agent is enforced to react for the third time, now in the second "floor".
Fig. 6 shows the possible sequel to the situation shown in Figr 5. By repeating this construction over Z~ 83 various "floors", the reaction eEficiency can, in fact, be increased to an unlimited extent.
- Fig. 7 shows one of the possibilities to complete the reaction process, using the same principle according to the present invention, with the capture of reaction products. When the wall of cone 7 is extended, the speed of vortex (d) can be reduced by dimensioning of diameters so that the solid components: fly ash, chemical reaction products and any excess of neutralizing substances are deposited within cylinder 8. The vortex (d) will automatic:ally produce vortex (e), which now ascends according to the dotted lines and the~eafter discharges through the central exhaust the now strongly chemically purified gases through 11 .
The increase in efficiency of the deposition of solids results in a lower load of the filters, which reduces the cost of energy and maintenance. The increase in efficiency of the chemical reactions means a saving in chemicals and residual materials, hence lower exploitation cost which, by means of the method and device according to the present invention, can even be lower than those of known installations.
It will be clear that where reference is made to flue gases and acid components, the principle of the present invention also applies to other fluids, e.g. industrail exhaust gases or liquids and basic components in which case naturally other absorption/neutralizing agents can play a role. Where the term "absorption"
is used in the specification, the term "adsorption"
or a similar term may be used instead.
The consequence of that, however, is that it will increase investments by a factor of 2 or 3 as a result of the elaborate processing involved in this methocl, on top of which, in most cases, additional waste water purification is required.
It is an object of the present invention to improve the dry flue gas purification with cyclones in such a manner that emission standards are met and expected by even lower valuas will result, thus achieving a particular improvement in the solution of environmental problems in respect of, for example, refuse incinerators.
This can be realized at quite acceptable prices at that.
To that effect, according to the present invention, by application of the features reclted in the characterizing clause of claim 1, the components entering the cyclone are not only centrifugad but the light fractions in the flue gases, including the major part of the gaseous acid components, are prevented from diffusing directly through the flue gas stream to the cyclone exit, so that the contact with the neutralizing heavier components is too short.
According to the present invention, the light fractions in the flue gases, together with the heavier fractions are jointly centrifuged after entering the cyclones, while in contrast to the situation in the 4 2~ 33 present design within cyclones, increasingly intensive contact is enforced by increased concentration and at the same time strongly increased velocity by means of an inverted cone provided preferably in the centre of the cyclone. This forces the light (i.e. the acid) com-ponents in the flue gases to react with the neutralizing substances immediately, intensively and for a prolonged period of time.
By repeating the inverted cone construction, as indicated above, at a lower level, there is obtained a reversal of the flue gas motion, whereby the descending high-velocity whirl is converted into a rising initially expanding whirl of relatively low velocity. According as the whirl thereafter at higher level again approaches the centre of the cyclone, the acceleration and the concentration are considerably increased. The heavier fractions in the strongly accelerated rising whirl are again mixed intensively with the light fractions (including those to be neutralized) in the gas stream. Repetition of the above inverted cone constructions in the interior of the cyclone will increase the effect of mixing and neutralizing acid components in the flue gases. Moreover, the effect of mixing and chemical reaction can be increased per "floor" by rendering the distance between the internal cones adjustable. In this manner, substantially higher vortex speeds (and hence higher mixing efficiency) can be achieved than provided initially (i.e. upon entry 2Q~9~83 into the cyclone). The variation of the distance between the internal cones can be controlled by coupling the adjustment to e.g. the measured acidity of the flue gases prior to their discharge to the chimney stack.
The last fixed cone can be extended to a cylindrical bin where the vortex can be reduced to such a low velocity - by properly dimensioning the cylinder - that solid components (fly ash, chemical reaction products and possible excess of neutralizing substances) are separated.
The purified gas stream is removed through a central exhaust within the lowest cylinder. Naturally, exhaust from the installation need not necessarily take place in the above manner. It is also possible for instance to select tangential exhaust from the circumference~
Another possibility could be: exhaust from the top of the device in the case where one "floor" would be sufficient to attain the required efficiency. IE an enlargement of the lowest cone is selected, as mentioned abo~e, there is automatically produced a collectin~ bin which can selectively perform a number of useful functions:
a) temporary storage of separated and/or reacted products prior to discharge into a container;
b) return of the separated products to the inlet of the cyclone or one of the floors, to thereby allow any neutralizing material not yet entirely reacted to participated again in the process.
6 Z~)9~L133 Some embodiments of apparatus according to the present invention will now be described, by way of example, with reference to the accompanying drawings, in which:
Fig. 1 diagrammatically shows the ope~ation of a conventional cyclone;
Fig. lA is a cross-sectional view according to the arrow A in Fig. l;
Fig. 2 shows in top plan view the operation of a cyclone according to the present invention;
Fig. 3 is a diagrammatic cross-sectional view of the cyclone shown in Fig. 2;
Fig. 4 is a view similar to E'ig. 3 but showing the top of the cyclone illustrated in Fig. 3 and its operation in more detail;
Fig. 5 is a view similar to Fig. 4, but in a further stage of the fluid motion;
Fig. 6 is a similar view showing fluid motion subsequent to the situation shown in Fig. 5; and Fig. 7 shows the completion of the process by collecting reaction products.
Fig. 1 is a cross-sectional view of a conventional cyclone construction, showing the centrifugal separation of heavier fly ash, neutralizing substances and reaction products via the descending vortex (a) and the rapid diffusion of the light (e.g. acid) components (b), including light solid components of the flue gases, which are 7 Z~ 83 subsequently discharged to filters upstream of the chimney stack. The flue gases mixed with absorbing and/or neutralizing substances are introduced tangentially through 1 into the cylindrical portion 2 where they are contacted with each other. The heavier components, such as fly ash and a part of the reaction material, descend via vortex (a) into the discharge or collecting hopper 8. The lighter fractions, such as acid gases, light fly ash particles and residual reaction material, are separated from vortex (a) directly at the open bottom of exhaust pipe 11 and disappear through vortex (b) in fractions of seconds through pipe 11. The reaction time available for neutralizing undes:irable components is therefore very short. In those cases where the percentage of undesirable chPmical components in the gas stream is high, the added neutralizing and/or absorption agent will react insufficiently. Thus the composition of the flue gases discharged via 11 will fail to meet the recently raised emission standards.
A substantial excess of neutralizing agent has proved unable to solve the problem and moreover creates two additional problems:
- the extra cost connected with the discharge of substantial amounts of residues to dumping sites which - can accept these materials only at increase rates.
8 2Q~ 8~
The residues, in fact, require additional provisions at the dumping sites to control the water economy and quality.
It is an object of the present invention to avoid these drawbacks and to positively improve the result in a manner as shown in principle in Figs. 2-7.
As shown in Figs. 2 and 3, flue gases are introduced tangentially through 1 into the cylinder 2 - the cyclone -possibly with added neutralizing substances. The additions of these and/or other substances, naturally, can also take place after the entry, e.g. through the apex of cone 4 or the base of cone 5.
Undesirable components, together with the heavier components (fly ash and neutralizing substances) are centrifuged in cylinder ~, while in contrast to the situation described for the cyclones of the prior art, increasingl~ intensive contact is promoted by increased concentration and at the same time strongly increase velocity of vortex (a) by means of an inverted cone 4 provided (preferably) in the centre of the cyclone.
As appears from the detail shown in Fig. 4, the centrality suspended inverted cone 4 products intially the accelerated descending vortex (a) shown in Fig. 3.
This vortex is deflected 180 from its original direction by the bottom of cone 5 and has as the only way out the cylindrical cross-section II, being substantially larger than cross-section I, in other words, besides 2C~9~ 33 a reversal through an angle of 180, a sudden expansion takes place. This is highly favourable to additional vortex effects/ resulting in additional mixing and enchanced chemical reactions. The cyclonic gas motion cannot become suddenly rectilinear, for a new vortex (b) is formed, as model tests have shown, ~hich ascends according to the dotted lines shown in the drawings between the two cones at in'creasingly higher vertical and tangential speed = mixing speed = chemical reaction speed. The absorption/neutralizing agent is enforced to react for the second time.
Fig. 5 shows the same cyclone detail as Fig. ~
with a representation o the gas motions which are deve~
loping in a stage further than that shown in Fig. 4.
From cross-section III, a substantially 180 reversal of gas motions takes place again. It should be noted that a 180 reversal, as used herein, should be construed to mean the eventual effect in a vertical sense. The actual gas motion remains tangential, resulting a vortex ascending or descending, as a whirl, perpendicularly.
In cross-section III, such a 180 reversal takes place again. Vortex (c) is formed, resulting-in very high speeds, in other'words, a very high mixing effect and very high chemical reaction speeds. The absorption/neutralizing agent is enforced to react for the third time, now in the second "floor".
Fig. 6 shows the possible sequel to the situation shown in Figr 5. By repeating this construction over Z~ 83 various "floors", the reaction eEficiency can, in fact, be increased to an unlimited extent.
- Fig. 7 shows one of the possibilities to complete the reaction process, using the same principle according to the present invention, with the capture of reaction products. When the wall of cone 7 is extended, the speed of vortex (d) can be reduced by dimensioning of diameters so that the solid components: fly ash, chemical reaction products and any excess of neutralizing substances are deposited within cylinder 8. The vortex (d) will automatic:ally produce vortex (e), which now ascends according to the dotted lines and the~eafter discharges through the central exhaust the now strongly chemically purified gases through 11 .
The increase in efficiency of the deposition of solids results in a lower load of the filters, which reduces the cost of energy and maintenance. The increase in efficiency of the chemical reactions means a saving in chemicals and residual materials, hence lower exploitation cost which, by means of the method and device according to the present invention, can even be lower than those of known installations.
It will be clear that where reference is made to flue gases and acid components, the principle of the present invention also applies to other fluids, e.g. industrail exhaust gases or liquids and basic components in which case naturally other absorption/neutralizing agents can play a role. Where the term "absorption"
is used in the specification, the term "adsorption"
or a similar term may be used instead.
Claims (10)
1. A method of chemical binding and/or absorbing contaminants in a fluid, said fluid selected from the group consisting of contaminated gas and liquid streams, comprising:
a) contacting said contaminated fluid by mixing said fluid with neutralizing and/or absorbing substances; said contacting step causing the formation of reaction products comprising said contaminants and said substances;
b) increasing said contacting step by giving said mixture a whirling motion, and said whirling motion is accelerated with simultaneous compression of said mixture; and c) discharging said reaction products and the possible excess of neutralizing and/or absorbing subtances to an outlet, and/or discharging part of said reaction products and excess of added substances to a position upstream of the outlet for renewed use.
a) contacting said contaminated fluid by mixing said fluid with neutralizing and/or absorbing substances; said contacting step causing the formation of reaction products comprising said contaminants and said substances;
b) increasing said contacting step by giving said mixture a whirling motion, and said whirling motion is accelerated with simultaneous compression of said mixture; and c) discharging said reaction products and the possible excess of neutralizing and/or absorbing subtances to an outlet, and/or discharging part of said reaction products and excess of added substances to a position upstream of the outlet for renewed use.
2. A method according to claim 1, wherein said mixture is subjected to at least one continued contacting step.
3. A method according to claim 2, wherein in said continued contacting step said accelerated and compressed whirling mixture is forced to expand; is subsequently accelerated with simultaneous compression again; and is then decelerated in such a way that solids and/or reaction products are deposited from said whirling mixture.
4. An apparatus for chemical binding by contacting contaminated fluid with neutralizing and/or absorbing substances and for removing the reaction products from said fluid, said fluid selected from the group consisting of contaminate. gas and liquid streams, comprising:
a cylindrical chamber (2), said chamber having at its closed top a tangential inlet;
an assembly located in said chamber providing means for giving a whirling motion to the mixture of said fluid and said substances, comprising:
a first hollow conical insert (4) closed at its narrow top relatively to said cylindrical chamber (2), and having its wide lower edge at a short interspace (I) from the cylindrical wall of said chamber (2);
a second frusto-conical insert (5) having an open top and at its wide lower end is circumferentially and sealingly connected to the opposed side wall of said cylindrical chamber (2) by means to form a floor in said chamber;
said second frusto-conical insert (5) being located under-neath said first conical insert (4) at an adjustable distance wherein the open narrow top of said second insert (5) being at a level relative to the wider lower edge of said first insert (4) such that a fluid vortex descending over said wider lower edge of said first insert (4), is forced into a narrowing upward path under the said first insert (4) so as to further accelerate the entire mixture before entering the open top of the second insert (5); and means for delivering the entire fluid mixture to separating means.
a cylindrical chamber (2), said chamber having at its closed top a tangential inlet;
an assembly located in said chamber providing means for giving a whirling motion to the mixture of said fluid and said substances, comprising:
a first hollow conical insert (4) closed at its narrow top relatively to said cylindrical chamber (2), and having its wide lower edge at a short interspace (I) from the cylindrical wall of said chamber (2);
a second frusto-conical insert (5) having an open top and at its wide lower end is circumferentially and sealingly connected to the opposed side wall of said cylindrical chamber (2) by means to form a floor in said chamber;
said second frusto-conical insert (5) being located under-neath said first conical insert (4) at an adjustable distance wherein the open narrow top of said second insert (5) being at a level relative to the wider lower edge of said first insert (4) such that a fluid vortex descending over said wider lower edge of said first insert (4), is forced into a narrowing upward path under the said first insert (4) so as to further accelerate the entire mixture before entering the open top of the second insert (5); and means for delivering the entire fluid mixture to separating means.
5. An apparatus according to claim 4, wherein the top end of said first conical insert (4) or of said second conical insert (5) is connected to a central outlet (11) (Fig. 3).
6. An apparatus according to claim 4, wherein underneath said assembly of said first conical insert (4) and said second conical insert (5) there is provided at least one further similar assembly of said first and said second conical inserts in said chamber (2).
7. An apparatus according to claim 6, wherein said assembly is located at a variable distance underneath said floor.
8. An apparatus according to claim 6, wherein the floor of said assembly connects to a subjacent collecting space (8) of larger diameter than said cylindrical chamber (2), said diameter being of such a dimension to cause, through deceleration of the whirling mixture, the depositing of reaction products and any excess neutralizing and/or absorbing substances in said collecting space (8); said collecting space functioning as a storage space and having an exhaust mean (11) extending centrally downwards through said space.
9. An apparatus according to claim 5, wherein the mixture of said fluid and said substances or the reaction products are discharged to a container, to a recirculation pipe and/or to a downstream filtering device.
10. The invention or inventions substantially as described herein with reference to any of the preceding claims.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CA 2009183 CA2009183A1 (en) | 1990-02-02 | 1990-02-02 | Method and a device for treating or mixing components in gas or liquid streams |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CA 2009183 CA2009183A1 (en) | 1990-02-02 | 1990-02-02 | Method and a device for treating or mixing components in gas or liquid streams |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA2009183A1 true CA2009183A1 (en) | 1991-08-02 |
Family
ID=4144189
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA 2009183 Abandoned CA2009183A1 (en) | 1990-02-02 | 1990-02-02 | Method and a device for treating or mixing components in gas or liquid streams |
Country Status (1)
| Country | Link |
|---|---|
| CA (1) | CA2009183A1 (en) |
-
1990
- 1990-02-02 CA CA 2009183 patent/CA2009183A1/en not_active Abandoned
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