CA1120395A - Process and apparatus for direct mass or heat exchange - Google Patents
Process and apparatus for direct mass or heat exchangeInfo
- Publication number
- CA1120395A CA1120395A CA000326703A CA326703A CA1120395A CA 1120395 A CA1120395 A CA 1120395A CA 000326703 A CA000326703 A CA 000326703A CA 326703 A CA326703 A CA 326703A CA 1120395 A CA1120395 A CA 1120395A
- Authority
- CA
- Canada
- Prior art keywords
- streams
- mixing chambers
- column
- hollow bodies
- liquid
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired
Links
- 238000000034 method Methods 0.000 title claims abstract description 11
- 239000000463 material Substances 0.000 claims abstract description 19
- 239000007788 liquid Substances 0.000 claims description 43
- 230000003197 catalytic effect Effects 0.000 claims description 4
- 230000002706 hydrostatic effect Effects 0.000 claims description 2
- 239000011248 coating agent Substances 0.000 claims 1
- 238000000576 coating method Methods 0.000 claims 1
- 239000007789 gas Substances 0.000 description 13
- 238000004519 manufacturing process Methods 0.000 description 5
- 238000012856 packing Methods 0.000 description 5
- 238000000926 separation method Methods 0.000 description 3
- 238000009826 distribution Methods 0.000 description 2
- 239000007921 spray Substances 0.000 description 2
- 238000009825 accumulation Methods 0.000 description 1
- 229910010293 ceramic material Inorganic materials 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000001788 irregular Effects 0.000 description 1
- 239000011344 liquid material Substances 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 229920003023 plastic Polymers 0.000 description 1
- 239000004033 plastic Substances 0.000 description 1
- 239000011343 solid material Substances 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/30—Loose or shaped packing elements, e.g. Raschig rings or Berl saddles, for pouring into the apparatus for mass or heat transfer
-
- B01J35/56—
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
- F28F25/00—Component parts of trickle coolers
- F28F25/02—Component parts of trickle coolers for distributing, circulating, and accumulating liquid
- F28F25/08—Splashing boards or grids, e.g. for converting liquid sprays into liquid films; Elements or beds for increasing the area of the contact surface
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/30—Details relating to random packing elements
- B01J2219/302—Basic shape of the elements
- B01J2219/30226—Cone or truncated cone
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/30—Details relating to random packing elements
- B01J2219/302—Basic shape of the elements
- B01J2219/3023—Triangle
Abstract
ABSTRACT OF THE DISCLOSURE
The invention provides a process for bringing two streams of material into contact for direct mass or heat exchange, wherein said streams are passed in counterflow through a column having mixing chambers defined by prismatic hollow bodies each having a central constriction, one of said streams entering and leaving said mixing chambers through inlets and outlets formed by said central constrictions, and the other of said streams entering and leaving said mixing chambers independently of said one stream through separate openings formed therein.
The invention provides a process for bringing two streams of material into contact for direct mass or heat exchange, wherein said streams are passed in counterflow through a column having mixing chambers defined by prismatic hollow bodies each having a central constriction, one of said streams entering and leaving said mixing chambers through inlets and outlets formed by said central constrictions, and the other of said streams entering and leaving said mixing chambers independently of said one stream through separate openings formed therein.
Description
1~2~3395 The present invention relates to a process for direct mass o~ heat exchange~ The present invention also relates to a device for use in the Process~
Various types of i-nternal column structures, that operate according to different principles or are constructed as a result of production considerations, are used for direct mass or heat exchange. For reasons of improved classification, these internal column structures are divided into groups. Thus, a distinction is made between the plate and packed columns as well as between spray and sprin~ler columns, and mechanically powered rotating and pulsing columns. Recently, column packings have grown more numerous. Unavoidably, all internal column structures have certain disadvantages in addition to their particular advantages so that their use is governed by the type of applica-tion. Thus, the objective must be to find a universally usable internal column structure that takes scientific knowledge of material, heat and pulse exchange into consideration, as well as the economic production of all the column sizes and materials re~uired by industry.
In order to be able to use this internal column structure for all column sizes, it must consist of individual elements of identical dimensions, that can be combined according to each parti-cular column diameter iand height. In addition, the design must be self-supporting to permit the use of the device with any desired material. Economical series production and storage will be ensured by the above-described design features. ~owever, the division of the total column volume must be such as to ensure that areas of equal size are formed, the configuration of which ensures the maximum mass, heat and ~ulse exchan~e, llZ~)395 In order to achieve a minimum specific column volume, B during ma~ r~ /or heat exchange the gases or vapours, or liquid or solid material particles must be passed through the column at different concentrations and/or temperatures as fast as possible, counter to the flow and be brought into contact with each other so that the maximum material, heat or pulse exchange results. In actual practice, in the case of most internal column structures the counterflow cannot be assured in the area of each individual column cross-section, and is disrupted to an ever-increasing degree as the column diameter increases. In addition,as the speeds of the material streams that are moving in counter-flow increase, remixing can easily occur throughout the whole height of the column, thereby reducing throughput capacity. In the case of plate columns, when the liquid is passed across the plates, only a cross flow is possible, so that plate divisions with additional drain-off possibilities are necessary in the event of large column diameters. Each size of column thus requires a different design. Not all materials are suitable for plate columns and so, for example, the most corrosion resistant and favourably priced ceramic materials and various plastics cannot be used for them.
~ lthough packed columns entail the advantages of econ-omical production and the possibility of using all materials, as well as the fact that columns of all diameters can be used, the liquid distribution within the column is disrupted so badly because of the random filling and the concomitant various spaces that remain that not only are the localized quantity ratios of the material streams different, but counterflow cannot be main-tained across the whole cross-section of the column (maldistri-bution). For this reason very large exchange columns cannot beoperated successfully with random-filling.
It is also understandable in sprinkler columns without llZ()395 internal structures tha~ restrict the maintenance of the counter-flow between the phases is impossible because of the remixing that cannot be avoided because of turbulence. Columns with dynamic internal structures are excluded from these considera-tions because of economic reasons.
Finally, only in spray towers (film towers) and with ordered packing is it possible to achieve a precise counterflow within the column by virtue of the regular division of the column areas. For these reasons this new type of internal column structure is being used more and more in high-performance columns, provided that excessive material or production costs do not prejudice the economics use of the internal column struc-tures. However, even with these regular internal column struc-tures a special problem is the even distribution of liquid in the relatively large number of vertical column spaces. The quantity ratios of the material streams in exchange is disrupted by a more or less unavoidable irregular supply of liquid to the individual spaces, and this results in a reduction of the selec-tive capacity of the overall column.
To a very great extent these difficulties and disad-vantages have been eliminated by the configuration of the column described in DT-PS No. 1,268,596, which has internal structures that are arranged regularly in layers, by the fact that pris-matic hollow bodies that are constricted at the middle and open in the direction of flow are arranged in relation to one another so that a number of individual streams through the hollow bGdies can mix with one another across the whole column cross-section in a common mantle space while forming two separate systems. In given separation operations the liquid quantity/column area can be increased by increasing the throughput capacity and thereby reducing the specific column area, whereby the liquid supply to the individual channels will be more even. In the sprinkler 112~)39~
columns and the column packings according to DT-PS No. 1,268,596 the throughput capacity is, however, limited by the fact that in each column cross-section the liquid must run off through the same openings through which the gases or vapours are moving counter to the flow. Therefore, at relatively high speeds a counterflow is no longer possible in the column since there are liquid buildups and liquid backflow in the column packing. In addition, the mixing of the individual streams in the mantle area of a column cross-section is more or less restricted to the gas or vapour streams, since the liquid films that are running off the vertical or inclined walls of the packing remain in the individual vertical channels and are not newly distributed. The necessary concentration equaliziation can thus take place only by a not completely attainable equal liquid supply only in the gas or vapour phase.
It has now been found however that the counterflow can also be maintained in a column at very high gas or vapour speeds for achieving a maximum material, heat and pulse exchange, and thereby in the individual vertical channels when liquid has accumulated if the gas or vapour, or liquid that is passed in counterflow flows not through the liquid layers that have accumu-lated at the constrictions of the vertical channels but through the side openings in the channel walls and into the adjacent mixing chambers. This leads to an alternating flow from the mixing chambers of one vertical channel to the mixing chambers that surround it to the sides, and vice versa, whereby an unavoid-ably repeated lateral mixing from mixing chamber to mixing chamber and, thereby, a concentration equalisation of all the vertical streams takes place across the whole column cross-section. This facilitates the redistribution of the unequal quantities of liquid that are supplied to the individual channels, in that the liquid film draining off the channel walls must drop from their ~2l)395 side openings, thereby getting into the gas or vapour, or liquid, streams that flow in alternating fashion from mixing chamber to mixing chamber, in which connection the walls of the mixing cham-bers serve as impact surfaces for the droplet separation and as material exchange surfaces.
According to the present invention there is provided a process for bringing two streams of material into contact for direct mass or heat exchange, wherein said streams are passed in counterflow through a column having mixing chambers defined by prismatic hollow bodies each having a central constriction, one of said streams entering and leaving said mixing chambers through inlets and outlets formed by said central constrictions, and the other of said streams entering and leaving said mixing chambers independently of said one stream through separate openings formed therein.
The present invention thus provides a device for effect-ing the aforesaid process according to the present invention in which every mixing chamber has additional openings both for the ingress and for the egress of the gases or vapours, or liquids, that are passed through the column, in addition to the liquid ingress and egress openings.
The present invention will be further illustrated by way of the accompanying drawings in which:
Figure l is a schematic representation of a device according to one embodiment of the present invention;
Figure 2 is a detail of the device of Figure l; and Figure 3 is a section taken along the line a-b in Figure l.
Referring to the accompanying drawings and particularly Figure l, the vertical stream channel ll is constricted above and below at the locations 12 and 13, so that the liquids flow-~ 5 -lilZ~)395 ing from top to bottom will accumulate at the locations 12 and 13 as the result of the pressure loss of the gas or liquid streams that are moving in counterflow. One embodiment of the configuration of the locations 12 and 13 can be seen in Figure
Various types of i-nternal column structures, that operate according to different principles or are constructed as a result of production considerations, are used for direct mass or heat exchange. For reasons of improved classification, these internal column structures are divided into groups. Thus, a distinction is made between the plate and packed columns as well as between spray and sprin~ler columns, and mechanically powered rotating and pulsing columns. Recently, column packings have grown more numerous. Unavoidably, all internal column structures have certain disadvantages in addition to their particular advantages so that their use is governed by the type of applica-tion. Thus, the objective must be to find a universally usable internal column structure that takes scientific knowledge of material, heat and pulse exchange into consideration, as well as the economic production of all the column sizes and materials re~uired by industry.
In order to be able to use this internal column structure for all column sizes, it must consist of individual elements of identical dimensions, that can be combined according to each parti-cular column diameter iand height. In addition, the design must be self-supporting to permit the use of the device with any desired material. Economical series production and storage will be ensured by the above-described design features. ~owever, the division of the total column volume must be such as to ensure that areas of equal size are formed, the configuration of which ensures the maximum mass, heat and ~ulse exchan~e, llZ~)395 In order to achieve a minimum specific column volume, B during ma~ r~ /or heat exchange the gases or vapours, or liquid or solid material particles must be passed through the column at different concentrations and/or temperatures as fast as possible, counter to the flow and be brought into contact with each other so that the maximum material, heat or pulse exchange results. In actual practice, in the case of most internal column structures the counterflow cannot be assured in the area of each individual column cross-section, and is disrupted to an ever-increasing degree as the column diameter increases. In addition,as the speeds of the material streams that are moving in counter-flow increase, remixing can easily occur throughout the whole height of the column, thereby reducing throughput capacity. In the case of plate columns, when the liquid is passed across the plates, only a cross flow is possible, so that plate divisions with additional drain-off possibilities are necessary in the event of large column diameters. Each size of column thus requires a different design. Not all materials are suitable for plate columns and so, for example, the most corrosion resistant and favourably priced ceramic materials and various plastics cannot be used for them.
~ lthough packed columns entail the advantages of econ-omical production and the possibility of using all materials, as well as the fact that columns of all diameters can be used, the liquid distribution within the column is disrupted so badly because of the random filling and the concomitant various spaces that remain that not only are the localized quantity ratios of the material streams different, but counterflow cannot be main-tained across the whole cross-section of the column (maldistri-bution). For this reason very large exchange columns cannot beoperated successfully with random-filling.
It is also understandable in sprinkler columns without llZ()395 internal structures tha~ restrict the maintenance of the counter-flow between the phases is impossible because of the remixing that cannot be avoided because of turbulence. Columns with dynamic internal structures are excluded from these considera-tions because of economic reasons.
Finally, only in spray towers (film towers) and with ordered packing is it possible to achieve a precise counterflow within the column by virtue of the regular division of the column areas. For these reasons this new type of internal column structure is being used more and more in high-performance columns, provided that excessive material or production costs do not prejudice the economics use of the internal column struc-tures. However, even with these regular internal column struc-tures a special problem is the even distribution of liquid in the relatively large number of vertical column spaces. The quantity ratios of the material streams in exchange is disrupted by a more or less unavoidable irregular supply of liquid to the individual spaces, and this results in a reduction of the selec-tive capacity of the overall column.
To a very great extent these difficulties and disad-vantages have been eliminated by the configuration of the column described in DT-PS No. 1,268,596, which has internal structures that are arranged regularly in layers, by the fact that pris-matic hollow bodies that are constricted at the middle and open in the direction of flow are arranged in relation to one another so that a number of individual streams through the hollow bGdies can mix with one another across the whole column cross-section in a common mantle space while forming two separate systems. In given separation operations the liquid quantity/column area can be increased by increasing the throughput capacity and thereby reducing the specific column area, whereby the liquid supply to the individual channels will be more even. In the sprinkler 112~)39~
columns and the column packings according to DT-PS No. 1,268,596 the throughput capacity is, however, limited by the fact that in each column cross-section the liquid must run off through the same openings through which the gases or vapours are moving counter to the flow. Therefore, at relatively high speeds a counterflow is no longer possible in the column since there are liquid buildups and liquid backflow in the column packing. In addition, the mixing of the individual streams in the mantle area of a column cross-section is more or less restricted to the gas or vapour streams, since the liquid films that are running off the vertical or inclined walls of the packing remain in the individual vertical channels and are not newly distributed. The necessary concentration equaliziation can thus take place only by a not completely attainable equal liquid supply only in the gas or vapour phase.
It has now been found however that the counterflow can also be maintained in a column at very high gas or vapour speeds for achieving a maximum material, heat and pulse exchange, and thereby in the individual vertical channels when liquid has accumulated if the gas or vapour, or liquid that is passed in counterflow flows not through the liquid layers that have accumu-lated at the constrictions of the vertical channels but through the side openings in the channel walls and into the adjacent mixing chambers. This leads to an alternating flow from the mixing chambers of one vertical channel to the mixing chambers that surround it to the sides, and vice versa, whereby an unavoid-ably repeated lateral mixing from mixing chamber to mixing chamber and, thereby, a concentration equalisation of all the vertical streams takes place across the whole column cross-section. This facilitates the redistribution of the unequal quantities of liquid that are supplied to the individual channels, in that the liquid film draining off the channel walls must drop from their ~2l)395 side openings, thereby getting into the gas or vapour, or liquid, streams that flow in alternating fashion from mixing chamber to mixing chamber, in which connection the walls of the mixing cham-bers serve as impact surfaces for the droplet separation and as material exchange surfaces.
According to the present invention there is provided a process for bringing two streams of material into contact for direct mass or heat exchange, wherein said streams are passed in counterflow through a column having mixing chambers defined by prismatic hollow bodies each having a central constriction, one of said streams entering and leaving said mixing chambers through inlets and outlets formed by said central constrictions, and the other of said streams entering and leaving said mixing chambers independently of said one stream through separate openings formed therein.
The present invention thus provides a device for effect-ing the aforesaid process according to the present invention in which every mixing chamber has additional openings both for the ingress and for the egress of the gases or vapours, or liquids, that are passed through the column, in addition to the liquid ingress and egress openings.
The present invention will be further illustrated by way of the accompanying drawings in which:
Figure l is a schematic representation of a device according to one embodiment of the present invention;
Figure 2 is a detail of the device of Figure l; and Figure 3 is a section taken along the line a-b in Figure l.
Referring to the accompanying drawings and particularly Figure l, the vertical stream channel ll is constricted above and below at the locations 12 and 13, so that the liquids flow-~ 5 -lilZ~)395 ing from top to bottom will accumulate at the locations 12 and 13 as the result of the pressure loss of the gas or liquid streams that are moving in counterflow. One embodiment of the configuration of the locations 12 and 13 can be seen in Figure
2.
The gas or vapour, or liquid stream entering the verti-cal flow channel 11 through the openings 14 that are arranged so as to be separate from the liquid ingress and egress points 12 and 13 can leave the vertical flow channel 11 once again through the openings 15 after it has been mixed with the liquid and once again separated from it. The separation of the liquid and the vapour is made possible by the impact effect on the walls of the mixing chamber. This also makes it possible to avoid the fact that the gas or vapour, or liquid, stream has to flow through the liquid that has accumulated at the run-off points 12 and 13, and there~y undergo a corresponding pressure loss. The openings 14 of a ~ertical flow channel 11, like the openings lS
of the same flow channel 11, are larger than the liquid run-off openings 12 or 13. The pressure loss of the gas or vapour, or liqu..d, flowing from top to bottom is thereby smaller than the liquid head at the ingress and egress points 12 and 13 of the liquid that is flowing through the column. By virtue of this concept of the invention, of the vapour separated from the liquid feed in the mixing chamber 11, the throughput capacity of the column is not limited by the accumulation of liquid that has flowed through, as is the case, for example, with column fillings or duel-flow systems.
Referring to Figure 2 and Figure 3, a liquid supply that is separate from the vapour is ensured by a liquid run-off pipe 16 with a liquid closure 17. In addition, the quantity of liquid that has built up as a result of the pressure loss of the counterflow runs off through the side openings 19 onto the llZU395 outer surfaces 20 of the triangular hollow body 18. Especially in the case of high throughput capacities, this leads to repeated redistribution of the liquid that runs off and is sprayed through the counterflow in the flow channels 11 that are arranged in parallel, whereupon the quantities of liquid that are supplied unequally to the vertical channels 11 are equalized over the column cross-section.
The hydrostatic liquid lock can also be achieved by a suitable configuration of the run-off points 12, 13 in that the free cross-section 12, 13 is smaller than the side vapour open-ings 14, 15.
B As can be seen from Fig. 3, the openings~ and corres-pondingly the openings 14 of Figure 1 of the channel 11 that are below are formed by triangular hollow bodies 18 that are placed one on top of the other, in such a manner that the faces of the triangular hollow bodies 18 are concave or convex. When the tri-angular hollow bodies are placed one on top of the other, this forms the openings 14, 15 for the vertical gas or vapour, or liquid, streams that are directed from bottom to top. Several vertical channels 11 are formed next to each other, and connected to each other through the openings 14 and 15 of the concave or convex curved triangle sides, by the familiar triangular arrange-ment of the triangular hollow bodies 18 that are curved either con-cavely or convexly and arranged in layers next to each other and stood Gn gaps over each other. For the sake of completeness it is mentioned that in special cases the hollow bodies 18 may be made of catalytic material or coated with catalytic material.
The gas or vapour, or liquid stream entering the verti-cal flow channel 11 through the openings 14 that are arranged so as to be separate from the liquid ingress and egress points 12 and 13 can leave the vertical flow channel 11 once again through the openings 15 after it has been mixed with the liquid and once again separated from it. The separation of the liquid and the vapour is made possible by the impact effect on the walls of the mixing chamber. This also makes it possible to avoid the fact that the gas or vapour, or liquid, stream has to flow through the liquid that has accumulated at the run-off points 12 and 13, and there~y undergo a corresponding pressure loss. The openings 14 of a ~ertical flow channel 11, like the openings lS
of the same flow channel 11, are larger than the liquid run-off openings 12 or 13. The pressure loss of the gas or vapour, or liqu..d, flowing from top to bottom is thereby smaller than the liquid head at the ingress and egress points 12 and 13 of the liquid that is flowing through the column. By virtue of this concept of the invention, of the vapour separated from the liquid feed in the mixing chamber 11, the throughput capacity of the column is not limited by the accumulation of liquid that has flowed through, as is the case, for example, with column fillings or duel-flow systems.
Referring to Figure 2 and Figure 3, a liquid supply that is separate from the vapour is ensured by a liquid run-off pipe 16 with a liquid closure 17. In addition, the quantity of liquid that has built up as a result of the pressure loss of the counterflow runs off through the side openings 19 onto the llZU395 outer surfaces 20 of the triangular hollow body 18. Especially in the case of high throughput capacities, this leads to repeated redistribution of the liquid that runs off and is sprayed through the counterflow in the flow channels 11 that are arranged in parallel, whereupon the quantities of liquid that are supplied unequally to the vertical channels 11 are equalized over the column cross-section.
The hydrostatic liquid lock can also be achieved by a suitable configuration of the run-off points 12, 13 in that the free cross-section 12, 13 is smaller than the side vapour open-ings 14, 15.
B As can be seen from Fig. 3, the openings~ and corres-pondingly the openings 14 of Figure 1 of the channel 11 that are below are formed by triangular hollow bodies 18 that are placed one on top of the other, in such a manner that the faces of the triangular hollow bodies 18 are concave or convex. When the tri-angular hollow bodies are placed one on top of the other, this forms the openings 14, 15 for the vertical gas or vapour, or liquid, streams that are directed from bottom to top. Several vertical channels 11 are formed next to each other, and connected to each other through the openings 14 and 15 of the concave or convex curved triangle sides, by the familiar triangular arrange-ment of the triangular hollow bodies 18 that are curved either con-cavely or convexly and arranged in layers next to each other and stood Gn gaps over each other. For the sake of completeness it is mentioned that in special cases the hollow bodies 18 may be made of catalytic material or coated with catalytic material.
Claims (12)
PROPERTY OR PRIVILEGE IS CLAIMED ARE DEFINED AS FOLLOWS:
1. A process for bringing two streams of material into contact for direct mass or heat exchange, wherein said streams are passed in counterflow through a column having mixing chambers defined by prismatic hollow bodies each having a central constriction, one of said streams entering and leaving said mixing chambers through inlets and outlets formed by said central con-strictions, and the other of said streams entering and leaving said mixing chambers independently of said one stream through separate openings formed therein.
2. A process according to claim 1, wherein said one stream is a liquid.
3. A process according to claim 1, wherein said one stream is a gas.
4. A process according to claim 2 or 3, wherein said other stream is a liquid.
5. A process according to claim 2 or 3, wherein said other stream is a gas.
6. An apparatus for effecting direct mass or heat ex-change between two streams of material by bringing them into con-tact, comprising a column having mixing chambers defined by prismatic hollow bodies having central constrictions, said hollow bodies being arranged such that said constrictions provide res-pective inlets and outlets for one of said streams, and separate openings in said mixing chambers providing inlets and outlets for the other of said streams whereby said two streams enter and leave said mixing chambers independently of each other.
7. An apparatus according to claim 6, in which the inlets and outlets formed by the constrictions have a hydrostatic liquid lock.
8. An apparatus according to claim 7, in which said openings have a larger cross-sectional area than said inlets and outlets formed by said constrictions.
9. An apparatus according to claim 6, 7 or 8, in which each mixing chamber has a plurality of openings defining the inlet and a plurality of apertures defining the outlet for said other stream.
10. An apparatus according to claim 6, 7 or 8, in which the prismatic hollow bodies are formed by concavely or convexly bulged triangular hollow bodies located one on top of the other and said openings are defined between adjacent said hollow bodies.
11. An apparatus according to claim 6, 7 or 8, in which the mixing chambers are formed by the hollow bodies which are arranged both on top of each other and next to each other.
12. An apparatus according to claim 6, 7 or 8 in which the walls of the mixing chambers are either of catalytic material or have a catalytic coating.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| BE867.241 | 1978-05-19 | ||
| BE867241 | 1978-05-19 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1120395A true CA1120395A (en) | 1982-03-23 |
Family
ID=3861671
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA000326703A Expired CA1120395A (en) | 1978-05-19 | 1979-05-01 | Process and apparatus for direct mass or heat exchange |
Country Status (5)
| Country | Link |
|---|---|
| EP (1) | EP0005535B1 (en) |
| AT (1) | ATE114T1 (en) |
| BR (1) | BR7902694A (en) |
| CA (1) | CA1120395A (en) |
| DE (1) | DE2919463C2 (en) |
Families Citing this family (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| PL129859B1 (en) * | 1981-07-29 | 1984-06-30 | Inst Chemii Przemyslowej | Method of contacting gaseous and liquid media and packing therefor |
| DE3515300A1 (en) * | 1985-04-27 | 1986-10-30 | Gerd Dr Wilhelm | PYRAMID PACK FOR PROCESS ENGINEERING |
| AT383888B (en) * | 1985-05-02 | 1987-09-10 | Waagner Biro Ag | VIBRATION APPARATUS, ESPECIALLY VIBRATION COOLER |
| GB8528031D0 (en) * | 1985-11-13 | 1985-12-18 | Ici Plc | Ceramic structures |
| CA2124609A1 (en) * | 1993-06-23 | 1994-12-24 | Peter Barry Bosman | Packing elements, a pack, a method of constructing a pack, and a method for installing a packing in an evaporative cooler |
| US5460755A (en) * | 1993-06-23 | 1995-10-24 | T. C. Watermeyer Group, Inc. | Packing elements, a pack, a method of constructing a pack, and a method for installing a packing in an evaporative cooler |
Family Cites Families (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2960322A (en) * | 1957-04-03 | 1960-11-15 | Gulf Oil Corp | Apparatus for countercurrent contacting of liquid and vapor streams |
| DE1059888B (en) * | 1957-11-30 | 1959-06-25 | Degussa | Method and device for carrying out an exchange of substance and / or heat between gaseous and / or liquid media |
| DE1268596B (en) * | 1965-10-06 | 1968-05-22 | Rolf Manteufel | Device for mass and / or heat exchange and for mixing gaseous and / or liquid media or solid material particles |
| DE1542055A1 (en) * | 1966-01-25 | 1970-03-12 | Chevron Res | Facility for contact procedures involving dissimilar phases |
| US3804389A (en) * | 1969-06-17 | 1974-04-16 | Baltimore Aircoil Co Inc | Wet deck fill section |
| GB1294926A (en) * | 1970-01-27 | 1972-11-01 |
-
1979
- 1979-05-01 CA CA000326703A patent/CA1120395A/en not_active Expired
- 1979-05-03 BR BR7902694A patent/BR7902694A/en unknown
- 1979-05-15 EP EP79101484A patent/EP0005535B1/en not_active Expired
- 1979-05-15 AT AT79101484T patent/ATE114T1/en not_active IP Right Cessation
- 1979-05-15 DE DE2919463A patent/DE2919463C2/en not_active Expired
Also Published As
| Publication number | Publication date |
|---|---|
| EP0005535B1 (en) | 1981-07-15 |
| DE2919463C2 (en) | 1984-12-06 |
| DE2919463A1 (en) | 1979-11-29 |
| EP0005535A3 (en) | 1979-12-12 |
| EP0005535A2 (en) | 1979-11-28 |
| ATE114T1 (en) | 1981-07-15 |
| BR7902694A (en) | 1979-11-27 |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| MKEX | Expiry |