CA1064813A - Gas-liquid exchange column - Google Patents
Gas-liquid exchange columnInfo
- Publication number
- CA1064813A CA1064813A CA246,594A CA246594A CA1064813A CA 1064813 A CA1064813 A CA 1064813A CA 246594 A CA246594 A CA 246594A CA 1064813 A CA1064813 A CA 1064813A
- Authority
- CA
- Canada
- Prior art keywords
- liquid
- column
- packing
- reaction chamber
- gas
- 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
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D59/00—Separation of different isotopes of the same chemical element
- B01D59/28—Separation by chemical exchange
- B01D59/32—Separation by chemical exchange by exchange between fluids
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
- B01D3/16—Fractionating columns in which vapour bubbles through liquid
- B01D3/18—Fractionating columns in which vapour bubbles through liquid with horizontal bubble plates
- B01D3/20—Bubble caps; Risers for vapour; Discharge pipes for liquid
-
- 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
- B01J19/32—Packing elements in the form of grids or built-up elements for forming a unit or module inside the apparatus for mass or heat transfer
-
- 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
- B01J2219/32—Details relating to packing elements in the form of grids or built-up elements for forming a unit of module inside the apparatus for mass or heat transfer
- B01J2219/322—Basic shape of the elements
- B01J2219/32203—Sheets
- B01J2219/32206—Flat sheets
-
- 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
- B01J2219/32—Details relating to packing elements in the form of grids or built-up elements for forming a unit of module inside the apparatus for mass or heat transfer
- B01J2219/322—Basic shape of the elements
- B01J2219/32203—Sheets
- B01J2219/32224—Sheets characterised by the orientation of the sheet
- B01J2219/32227—Vertical orientation
-
- 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
- B01J2219/32—Details relating to packing elements in the form of grids or built-up elements for forming a unit of module inside the apparatus for mass or heat transfer
- B01J2219/322—Basic shape of the elements
- B01J2219/32279—Tubes or cylinders
-
- 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
- B01J2219/32—Details relating to packing elements in the form of grids or built-up elements for forming a unit of module inside the apparatus for mass or heat transfer
- B01J2219/324—Composition or microstructure of the elements
- B01J2219/32408—Metal
Landscapes
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Organic Chemistry (AREA)
- Physical Or Chemical Processes And Apparatus (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
- Gas Separation By Absorption (AREA)
Abstract
ABSTRACT OF THE DISCLOSURE
The inside of a reaction chamber of a counter-flow gas-liquid exchange column is filled with a liquid and gas permeable packing made of solid material such as a wire mesh, and liquid is recirculated through this packing to increase the gas-liquid interfacial area and thus considerably increase . the exchange rate at a relatively low cost of the apparatus.
The inside of a reaction chamber of a counter-flow gas-liquid exchange column is filled with a liquid and gas permeable packing made of solid material such as a wire mesh, and liquid is recirculated through this packing to increase the gas-liquid interfacial area and thus considerably increase . the exchange rate at a relatively low cost of the apparatus.
Description
;48~3 The present invention relates to a gas liquid mass transfer column of -the type used in deuterium-hydrogen exchange or the like.
Columns of this type are used in distillation, extrac-tion, absorption and exchange processes and in par-ticular, in enriching of one phase with an isotope. In all such processes the phases which are to be mixed with each other must be brought into a thorough contact with each other i~ the process is to be rapid and satisfactory.
Columns are known in which the passage of the gaseous phase in the system is caused by temperature differential resulting in a pressure difference. Gravity is normally used for causing the flow of the liquid phase throughout the system.
In the columns of this type, the onl~ way of achieving a large throughput is to increase the cross section of the column. If, for instance, the rate of flow of the gaseous phase were increased in known systems, the separating effect of gravity would cease to be adequate to meet the requirements of appro-- priate separation of the two phases; in particular, when there is little difference between the specific weight of the liquid and the gaseous phase, the descending particles of liquid may become drawn along by the gas flow.
In exchange columns of the above type to which the invention relates, the volume ratio between the liquid and gas phases in the reaction chamber can be selected independent of the throughput ratio determined by the process, to meet the desired mass-transfer rate.
In such case forces which are a multiple of gravity have to be used to separate the phases, since the liquid is circulated several times through the reaction chamber of each exchange unit.
The amount of the substance transferred in the exchange 1t3~4~3 columns is increased by increasing the overall area of contact between the two phases.
It is known to provide sieve tray columns wherein a woven wire fabric is disposed in the bubble bed above the ;~
sieve tray, in order to reduce agglomeration of gas bubbles passing through the bed. ~owever, the liquid speed in such columns is limited as the amount of liquid per transfer stage is determined by the volume of liquid flowing through the column.
Consequently, it is impossible to achieve any considerable turbulence in the bubble bed so that the increase in the contact surface is not satisfactory. Moreover, the size of the gas bubbles produced is increased by increasing the volume of gas supplied to the bed; eventually the gas bubbles may become so large that the wixes of the bubblebreaking system fail to break the bubbles up.
It is an object of the invention to provide relativel~
inexpensive means whereby the area of contact between the phases is considerably increased.
According to the invention, a gas-liquid mass-transfex column is provided which comprises a plurality of vertically spaced exchange units for a counter-flow mass-transfer, wherein the passage of the liquid descending between adjacent units is boosted by a pump so that the pressure of the liquid in a lower unit is hi~her than the static pressure corresponding ~ ;
to the respective height of liquid colurnn between the adjacent units. Each of such exchange units has at least one reaction chamber surrounded by a level charnber for the liquid phase.
Means for circulating the liquid from said level chamber through the associated reaction chamber form a further part of the column. Each of the exchange units has a bottom plate with at least one nozzle for introducing the gas phase into ' ' ~648:1 3 the reaction chamber. The top of the reaction chamber commu-nicates with a separating chamber. A substantial portion of the inside of the reaction chamber comprises a gas and liquid permeable packing, the packing being made of solid material.
In one embodiment of the present invention the packing comprises at least one member made of a wire-like material of ~`
a generally uniform structure. The wire-like material is pre-ferably a woven or knitted wire structure. In an even more preferred embodiment, the packing includes at least one layer of fleece comprised of fiber-type wires. The packing is pre-ferably of the type of a coil or roll of the wire-fabric-like material, whose outside diameter generally corresponds to the inside diameter of the reaction chamber so that when the roll is placed inside the chamber, the wire-like material fills a substantial portion of the volume of the chamber.
The invention will now be described by way of preferred embodiments with reference to the accompanying schematic drawings.
In The Drawings:
Figure 1 is a schematic vertical section of a part of an exchange column including one embodiment of the present invention;
Figure 2 is a section similar to Figure 1 but showing another embodiment of the present invention;
Figure 3 is a perspective view of one embodiment of ~;
the packing; and `
Figure 4 is a detailed perspective view of an embodiment of wire fabric used introducing the packing of Figure 3.
Referring now to Figure 1, reference numeral 1 shows a column comprising a plurality of exchange units 2 which are disposed one above the other in a pressurized tube. The column of this kind is used in deuterium exchange between hydrogen and ~ 3 ~
., ., ~ . . . . . . .
~ .~
106413~3 methylamine.
The exchange units 2 are each of the type of a reac-tion chamber 3, equidistantly spaced across the column. Opera tively associated with each chamber 3 is a jet pump ~ compris-ing a nozzle 4a and a diffuser 4b. The nozzles 4a are disposed in bottom plates secured in a gas-tight fashion to the column 1. A gas and liquid pervious packing consisting of a plurality of coils as shown in Figure 3, is disposed in each of the chambers 3. The coils 5 are of the same diameter as the diameter of the respective chambers 3 and are stacked loosely on each other. As best seen from Figures 3 and 4, the coils 5 are each formed from a sheet 5a of woven fabric provided with obliquely oriented corrugations.
Each of the chambers 3 is open at the top to communi- -cate with an associated separation chamber 6 wherein the gas is separated from the liquid whereupon the gas is discharged upwards through a tube 7 and via nozzles 4a enters the next exchange unit located above.
Surrounding the reaction chambers is a liquid chamber 8 from which a pump 9 is arranged to convey liquid through a line 10 into the liquid chamber 8 of the exchange unit 2 located immediately below the former. The jet pump continuously circulates liquid from the level chamber 8 through the res-pective reaction chamber 3 wherein the liquid contacts the gas.
The gas bubbles strike the wires of the coils 5 at high speed with the resulting breaking of the bubbles into an increased number of same.
The embodiment of Figure 2 differs from that of Figure 1 by the used type of counter flow mixing. While the different exchange units 2 of Figure 1 have jet pumps which circulate through the respective reaction chambers 3 a volume of liquid in-dependent of the total liquid throughput of the column, the r ~
?~
; 1(~f~4813 embodiment shown in Figure 2 comprises an improvement wherein pumps 11 feed li~uid from the liquid chambers into the reaction chambers and the gas flows between consecutive exchange units through nozzles 12 into the reaction chambers. In Figure 2, the structural elements corresponding to those of Figure 1 are referred to with the same reference numerals, each having an apostrophe.
As mentioned above, Figures 1 and 2 show only portions of the entire respective columns. The column heads and bottoms are not shown as they are not essential for proper understanding of the principles of this invention. The gas entering the bottom of the column can be compressed e.g~ by means of a compressor (not shown) which can be placed inside the column and below the bottom plate thereof. The required total pressure drop across the column can be provided by a pressure vessel (not shown) which, in a particularly advantageous embodiment, is simul-taneously used for storage of the compressed phase in an overall system of which the gas-liquid exchange column is a part.
It will be appreciated that the invention is based ~;
on an inventive recognition of the fact that by combining the -;~
features of known bubble beds in the type of the column as described above, the exchange rate can be considerably improved.
This is due to the fact that by repeated circulation of the liquid through reaction chambers according to the present invention, relatively high turbulence can be produced in the reaction chambers resulting in considerable reduction of the ~
size of gas bubbles, in reduced agglomeration of gas bubbles, ~ i with the resulting possibility of considerable increase in mass-transfer rate.
Those skilled in the art will readily appreciate fur-ther embodiments of the present invention differing from the above preferred embodiments but still falling within the scope of the accompanying claims.
_ 5 _
Columns of this type are used in distillation, extrac-tion, absorption and exchange processes and in par-ticular, in enriching of one phase with an isotope. In all such processes the phases which are to be mixed with each other must be brought into a thorough contact with each other i~ the process is to be rapid and satisfactory.
Columns are known in which the passage of the gaseous phase in the system is caused by temperature differential resulting in a pressure difference. Gravity is normally used for causing the flow of the liquid phase throughout the system.
In the columns of this type, the onl~ way of achieving a large throughput is to increase the cross section of the column. If, for instance, the rate of flow of the gaseous phase were increased in known systems, the separating effect of gravity would cease to be adequate to meet the requirements of appro-- priate separation of the two phases; in particular, when there is little difference between the specific weight of the liquid and the gaseous phase, the descending particles of liquid may become drawn along by the gas flow.
In exchange columns of the above type to which the invention relates, the volume ratio between the liquid and gas phases in the reaction chamber can be selected independent of the throughput ratio determined by the process, to meet the desired mass-transfer rate.
In such case forces which are a multiple of gravity have to be used to separate the phases, since the liquid is circulated several times through the reaction chamber of each exchange unit.
The amount of the substance transferred in the exchange 1t3~4~3 columns is increased by increasing the overall area of contact between the two phases.
It is known to provide sieve tray columns wherein a woven wire fabric is disposed in the bubble bed above the ;~
sieve tray, in order to reduce agglomeration of gas bubbles passing through the bed. ~owever, the liquid speed in such columns is limited as the amount of liquid per transfer stage is determined by the volume of liquid flowing through the column.
Consequently, it is impossible to achieve any considerable turbulence in the bubble bed so that the increase in the contact surface is not satisfactory. Moreover, the size of the gas bubbles produced is increased by increasing the volume of gas supplied to the bed; eventually the gas bubbles may become so large that the wixes of the bubblebreaking system fail to break the bubbles up.
It is an object of the invention to provide relativel~
inexpensive means whereby the area of contact between the phases is considerably increased.
According to the invention, a gas-liquid mass-transfex column is provided which comprises a plurality of vertically spaced exchange units for a counter-flow mass-transfer, wherein the passage of the liquid descending between adjacent units is boosted by a pump so that the pressure of the liquid in a lower unit is hi~her than the static pressure corresponding ~ ;
to the respective height of liquid colurnn between the adjacent units. Each of such exchange units has at least one reaction chamber surrounded by a level charnber for the liquid phase.
Means for circulating the liquid from said level chamber through the associated reaction chamber form a further part of the column. Each of the exchange units has a bottom plate with at least one nozzle for introducing the gas phase into ' ' ~648:1 3 the reaction chamber. The top of the reaction chamber commu-nicates with a separating chamber. A substantial portion of the inside of the reaction chamber comprises a gas and liquid permeable packing, the packing being made of solid material.
In one embodiment of the present invention the packing comprises at least one member made of a wire-like material of ~`
a generally uniform structure. The wire-like material is pre-ferably a woven or knitted wire structure. In an even more preferred embodiment, the packing includes at least one layer of fleece comprised of fiber-type wires. The packing is pre-ferably of the type of a coil or roll of the wire-fabric-like material, whose outside diameter generally corresponds to the inside diameter of the reaction chamber so that when the roll is placed inside the chamber, the wire-like material fills a substantial portion of the volume of the chamber.
The invention will now be described by way of preferred embodiments with reference to the accompanying schematic drawings.
In The Drawings:
Figure 1 is a schematic vertical section of a part of an exchange column including one embodiment of the present invention;
Figure 2 is a section similar to Figure 1 but showing another embodiment of the present invention;
Figure 3 is a perspective view of one embodiment of ~;
the packing; and `
Figure 4 is a detailed perspective view of an embodiment of wire fabric used introducing the packing of Figure 3.
Referring now to Figure 1, reference numeral 1 shows a column comprising a plurality of exchange units 2 which are disposed one above the other in a pressurized tube. The column of this kind is used in deuterium exchange between hydrogen and ~ 3 ~
., ., ~ . . . . . . .
~ .~
106413~3 methylamine.
The exchange units 2 are each of the type of a reac-tion chamber 3, equidistantly spaced across the column. Opera tively associated with each chamber 3 is a jet pump ~ compris-ing a nozzle 4a and a diffuser 4b. The nozzles 4a are disposed in bottom plates secured in a gas-tight fashion to the column 1. A gas and liquid pervious packing consisting of a plurality of coils as shown in Figure 3, is disposed in each of the chambers 3. The coils 5 are of the same diameter as the diameter of the respective chambers 3 and are stacked loosely on each other. As best seen from Figures 3 and 4, the coils 5 are each formed from a sheet 5a of woven fabric provided with obliquely oriented corrugations.
Each of the chambers 3 is open at the top to communi- -cate with an associated separation chamber 6 wherein the gas is separated from the liquid whereupon the gas is discharged upwards through a tube 7 and via nozzles 4a enters the next exchange unit located above.
Surrounding the reaction chambers is a liquid chamber 8 from which a pump 9 is arranged to convey liquid through a line 10 into the liquid chamber 8 of the exchange unit 2 located immediately below the former. The jet pump continuously circulates liquid from the level chamber 8 through the res-pective reaction chamber 3 wherein the liquid contacts the gas.
The gas bubbles strike the wires of the coils 5 at high speed with the resulting breaking of the bubbles into an increased number of same.
The embodiment of Figure 2 differs from that of Figure 1 by the used type of counter flow mixing. While the different exchange units 2 of Figure 1 have jet pumps which circulate through the respective reaction chambers 3 a volume of liquid in-dependent of the total liquid throughput of the column, the r ~
?~
; 1(~f~4813 embodiment shown in Figure 2 comprises an improvement wherein pumps 11 feed li~uid from the liquid chambers into the reaction chambers and the gas flows between consecutive exchange units through nozzles 12 into the reaction chambers. In Figure 2, the structural elements corresponding to those of Figure 1 are referred to with the same reference numerals, each having an apostrophe.
As mentioned above, Figures 1 and 2 show only portions of the entire respective columns. The column heads and bottoms are not shown as they are not essential for proper understanding of the principles of this invention. The gas entering the bottom of the column can be compressed e.g~ by means of a compressor (not shown) which can be placed inside the column and below the bottom plate thereof. The required total pressure drop across the column can be provided by a pressure vessel (not shown) which, in a particularly advantageous embodiment, is simul-taneously used for storage of the compressed phase in an overall system of which the gas-liquid exchange column is a part.
It will be appreciated that the invention is based ~;
on an inventive recognition of the fact that by combining the -;~
features of known bubble beds in the type of the column as described above, the exchange rate can be considerably improved.
This is due to the fact that by repeated circulation of the liquid through reaction chambers according to the present invention, relatively high turbulence can be produced in the reaction chambers resulting in considerable reduction of the ~
size of gas bubbles, in reduced agglomeration of gas bubbles, ~ i with the resulting possibility of considerable increase in mass-transfer rate.
Those skilled in the art will readily appreciate fur-ther embodiments of the present invention differing from the above preferred embodiments but still falling within the scope of the accompanying claims.
_ 5 _
Claims (6)
1. A gas-liquid exchange column comprising a plurality of vertically spaced exchange units for a counter-flow mass-transfer of the type wherein the passage of the liquid descend-ing between adjacent units is boosted by a pump, whereby the pressure increase of the liquid in a lower unit is higher than a corresponding increase due to the static pressure correspond-ing to the height of liquid column between the adjacent units;
each of said exchange units having at least one reaction chamber surrounded by a liquid chamber for receiving the liquid phase; means for circulating the liquid from said liquid chamber through the associated reaction chamber; each of said units having a bottom plate with at least one nozzle for intro-ducing the gas phase into said reaction chamber; the top of said reaction chamber communicating with a separation chamber;
wherein substantial portion of said reaction chamber comprises a gas and liquid permeable packing, said packing being made of solid material.
each of said exchange units having at least one reaction chamber surrounded by a liquid chamber for receiving the liquid phase; means for circulating the liquid from said liquid chamber through the associated reaction chamber; each of said units having a bottom plate with at least one nozzle for intro-ducing the gas phase into said reaction chamber; the top of said reaction chamber communicating with a separation chamber;
wherein substantial portion of said reaction chamber comprises a gas and liquid permeable packing, said packing being made of solid material.
2. A column as claimed in claim 1 wherein said packing comprises at least one member made of a wire-like material and having a generally uniform structure.
3. A column as claimed in claim 2 wherein said packing is a woven wire structure.
4. A column as claimed in claim 2 wherein said packing is a knitted wire structure.
5. A column as claimed in claim 1 wherein the packing includes at least one layer of fleece comprising fiber-type wires.
6. A column as claimed in claims 3, 4 or 5, wherein said packing comprises at least one roll of wire-fabric-like material, the outside diameter of said roll being generally identical with the inside diameter of the reaction chamber, whereby said wire-like material fills a substantial portion of the inside space of the reaction chamber.
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CH13976A CH612591A5 (en) | 1976-01-08 | 1976-01-08 | Mass transfer column |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1064813A true CA1064813A (en) | 1979-10-23 |
Family
ID=4180129
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA246,594A Expired CA1064813A (en) | 1976-01-08 | 1976-02-26 | Gas-liquid exchange column |
Country Status (6)
| Country | Link |
|---|---|
| JP (1) | JPS5946652B2 (en) |
| CA (1) | CA1064813A (en) |
| CH (1) | CH612591A5 (en) |
| DE (1) | DE2649414C3 (en) |
| FR (1) | FR2337570A1 (en) |
| GB (1) | GB1531918A (en) |
Families Citing this family (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4322367A (en) * | 1979-11-26 | 1982-03-30 | Colgate-Palmolive Company | Deoiling of aqueous solutions of sodium lauryl sulfate |
| JPH01263287A (en) * | 1988-04-12 | 1989-10-19 | Purantetsukusu:Kk | Cleaning device |
| DE3814255A1 (en) * | 1988-04-27 | 1989-11-09 | Metallgesellschaft Ag | DEVICE FOR DESODORING ORGANIC LIQUIDS |
| FR2727692A1 (en) * | 1994-12-05 | 1996-06-07 | Europ Propulsion | GAS EXTRACTION DEVICE FOR A CHEMICAL STEAM INFILTRATION OVEN OR VAPOR DEPOSIT IN A PLANT FOR MANUFACTURING PARTS OF COMPOSITE MATERIAL |
| DE19549429A1 (en) * | 1995-10-27 | 1997-04-30 | Elwatec Elektrolyse Und Wasser | Apparatus for catalytic reduction of nitrate and nitrite in water |
| CN102089074A (en) * | 2008-07-11 | 2011-06-08 | 阿西德管道技术股份有限公司 | Packing element for heat and mass transfer towers |
Family Cites Families (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2047444A (en) * | 1935-01-14 | 1936-07-14 | Stedman Donald Frank | Packing for fractionating columns and the like |
| CH406143A (en) * | 1963-12-19 | 1966-01-31 | Sulzer Ag | Mass transfer column |
| DE1501731A1 (en) * | 1966-11-10 | 1969-12-04 | Linde Ag | Rectification column |
| DE1751501B2 (en) * | 1968-06-10 | 1972-06-15 | Linde Ag, 6200 Wiesbaden | FILLING MATERIAL FOR LOW TEMPERATURE REGENERATORS |
| GB1356651A (en) * | 1971-04-17 | 1974-06-12 | Knitmesh Ltd | Packing elements |
| DE2158171C3 (en) * | 1971-11-24 | 1981-02-19 | Julius Montz Gmbh, 4010 Hilden | Monofilament fabric for mass transfer columns and its use |
-
1976
- 1976-01-08 CH CH13976A patent/CH612591A5/en not_active IP Right Cessation
- 1976-02-26 CA CA246,594A patent/CA1064813A/en not_active Expired
- 1976-04-20 GB GB1599776A patent/GB1531918A/en not_active Expired
- 1976-10-29 DE DE19762649414 patent/DE2649414C3/en not_active Expired
- 1976-12-27 FR FR7639167A patent/FR2337570A1/en active Granted
-
1977
- 1977-01-07 JP JP52000703A patent/JPS5946652B2/en not_active Expired
Also Published As
| Publication number | Publication date |
|---|---|
| JPS5946652B2 (en) | 1984-11-14 |
| CH612591A5 (en) | 1979-08-15 |
| GB1531918A (en) | 1978-11-15 |
| DE2649414C3 (en) | 1979-01-18 |
| DE2649414A1 (en) | 1977-07-14 |
| JPS5285976A (en) | 1977-07-16 |
| FR2337570A1 (en) | 1977-08-05 |
| DE2649414B2 (en) | 1978-05-24 |
| FR2337570B1 (en) | 1983-01-21 |
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