CA1199262A - Apparatus for exchanging material between a gas and a liquid - Google Patents
Apparatus for exchanging material between a gas and a liquidInfo
- Publication number
- CA1199262A CA1199262A CA000406335A CA406335A CA1199262A CA 1199262 A CA1199262 A CA 1199262A CA 000406335 A CA000406335 A CA 000406335A CA 406335 A CA406335 A CA 406335A CA 1199262 A CA1199262 A CA 1199262A
- Authority
- CA
- Canada
- Prior art keywords
- liquid
- tray
- pressure vessel
- gas
- connecting ducts
- 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
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- Physical Or Chemical Processes And Apparatus (AREA)
Abstract
ABSTRACT OF THE DISCLOSURE
The present invention relates to a static contact appara-tus which makes it possible to reduce the otherwise required large dimensions of the material exchange columns at a low solu-bility of the gas in the liquid and at slow kinetics of the reac-tions in the liquid phase. According to the present invention this is attained by means of a suitable guidance of the liquid stream and by means of a thus attainable extension of the resi-dence time of the liquid. According to the invention the appara-tus comprises a plurality of perforated trays superposed in a pressure vessel comprising connecting ducts for passing the liquid to a next lower tray, the path of the liquid at the end of said connecting ducts being arranged to be directed upwardly to prevent an undesired inflow of gas at said end of the connecting ducts, said connecting ducts being disposed in the region of the axis of said pressure vessel.
The present invention relates to a static contact appara-tus which makes it possible to reduce the otherwise required large dimensions of the material exchange columns at a low solu-bility of the gas in the liquid and at slow kinetics of the reac-tions in the liquid phase. According to the present invention this is attained by means of a suitable guidance of the liquid stream and by means of a thus attainable extension of the resi-dence time of the liquid. According to the invention the appara-tus comprises a plurality of perforated trays superposed in a pressure vessel comprising connecting ducts for passing the liquid to a next lower tray, the path of the liquid at the end of said connecting ducts being arranged to be directed upwardly to prevent an undesired inflow of gas at said end of the connecting ducts, said connecting ducts being disposed in the region of the axis of said pressure vessel.
Description
26~ .
The present invention relates ~o an apparatus for ex-changing material between a downwarclly flowlng liquid and an up-wardly flowing gas counterflow to the liquid. The conditions of the exchange of material for which the apparatus according to the present inven~ion is par~icularly suitable will be described hereinafter.
When the solubility of a gas, participating in the ex-change of material, is low in a liquid also participating in the exchange of material and ~urther when the exchange of material depends on a chemical reaction or on an isotope reaction in the liquid phase and the kinetics of this reaction are slow as compar-ed with the kinetics of the exchange of material of a dissolved ~as with the gas phase, then a lony residence time of the liquid in contact with the gas is required. This can be attained at a favourable cost when as large a proportion as possible of the column volume is used for the liquid. Furthermore when process conditions require the use of several trays, then they should be disposed in as small a number of pressure vessels as possible - while counterflow must be maintained and remixing flows must be avoided.
Material-exchange columns whose trays ~re superposed in a pressure vessel are known. In such a case the liquid ~lows from one tray via an overflow to the next lower tray. The over-~low is disposed in the gas cha,mber and is filled with liquid merely in the lowest region of the seal. Because of the hydro-dynamic conditions only approximately one quarter of the distance betwee~ the trays, ill which the liquid i5 in contact with the gas bubbles, can be used in these columns as the contact space.
Columns in wh:ich the liquid flows downwardly,primarily on the surface of packings, agalnst the gas ~low through the in-terstices of these packings are also known~ The proportion of volume filled with liquid in the columns is even substantially ~ 1 ~
6~
"~ smaller than that in the Eirst case. Columns which are filled almost completely with liquid and in which the gas to be contacted wit.h this li.quid flows upwardly in -the form of bubbles are also known.
The liquid is mixed in many dirèc-tions so that this kind of column can at best satisfy only the function of a single theoretical. tray.
Finally columns are known in which machines having a mechanical, electric or an intensified hydraulic drive for inten-sifying the exchange of material are known. In the last mentionedcase this occurs when the pressure drop on the gas side exceeds the available hydros-ta-tic pressure of the liquid and pumps must be used between -the trays in order -to convey the liquid. How-ever, these types of columns are -too costly to acquire and main-tain. Furthermore, in oprera-tion they can cause long interrup-tions due to their susceptibi.lity to trouble.
Accordi.ng to the presen-t invention there is provided an apparatus for exchanging material between a downwardly flowing liquid and an upwarding flowiny gas counterflow to said liquid, comprising a plurali-ty of perfora-ted trays superposed in a pres-sure vessel, comprising connecting ducts for passing the liquid to a next. lower -tray, the path of the li~uid at the end of said connecting ducts being arranged to be directed upwardly to prevent an undesired inflow of gas at said .end of the connec-ting ducts, said connecting ducts being disposed in the region of the axis o~ said pressure vessel. Suitably said connecting ducts comprise a pair of semicircular surfaces extending around the axis of said pressure vessel, said semicircular surfaces alternately connec-ting two adjacent trays. Desirably the liquid pa-th from an ou-tlet from said connec-ti.ng duct, which passes the liquid on from a next iligher tray, to the inl.et in said connecting duct, whi.ch removes the liquid to a next lowe~ tray, extends via concentrically dis-posect and ~,e.ries-connected semi-cylindrical chambers and sai~
]:iquid path e~tends first from the region of said axis of -the pressure vessel in the direction of the walls oE sa:id pressure vessel and then in -the opposite direc-tion. Preferably the space in which the liquid is in contact with -the gas bubbles is filled with fine-mesh gauze wire.
The present invention also provides a tray for use in such apparatus which comprises a perforated base; an inner con-centric part acting as a connecting duc-t, with a connectiny inlet tube for leading the liquid from an upstream tray to said -tray, concentrically disposed and series-connec-ted semi-cylindrical chambers formed by metal walls, an opening in said tray which is the outle-t fox a connecting inle-t tube -to a downstream tray, the metal wall, on the side of said opening, being lower than on the side of the connecting inlet tube from the upstream tray, so tha-t the liquid on said tray res-ts on a part of the perfora-ted base of said tray before ~alling into said opening.
Thus, according to the present invention in an appara-tus for exchanging material between a downwardly flowing liquid and an upwardly flowing gas couhterflow to said liquid, the liquid forms a hydrostatically continuous column extending from the top level to the lowes-t tapping point whereby the ratio of -the resi-dence time of the liquid to the volume content of the column is as large as possible. This column is merely loosened up by ~as bubbles in the regions of contact wi-th gas but it is not interrup-ted anywhere. ~ bubble cap is formed below each of said trays and within sai~ bubb]e cap ~he level of the liquid is displaced downwardly by the gas whereby, as compared wi-th the level of the liquid above the tray, a higher gas pressure is produced below the tray, the difference o:E said pressures being used to overcome -the pressure loss because of the gas flowing through the holes of t.he tray and simu:ltalleously to preven-t the flow o.~ liquid ~ ~B ~
26~
througll these holes. The connectin~ ducts for passin~ the ].iquid to the 3~
-- 2b next lower tray are disposed outside said bubblP caps or they cross said bubble caps. At the end of said connecting ducts the path of the liquid is directed upwards, thus preventing an un-desired entrance of gas at said end of the connecting ducts.
It is not sufficient to assure a long average residence time of the liquid on each tray~ but in order to attain a good tray fficiency, it is important that the divergence of this re-sidence time remains small when considering increasingly smaller portions of the -total liquid flow~ This condition cannot be sat-isfied without a forced guidance of the liquid via sufficientlynarrow ducts distributed over the entire tray~ According to the present invention this is achieved when said GOnneCting ducts are disposed in the region of the axis of the aforesaid pressure ve~-sel~ said connecting ducts consist of two semicircular surfaces encompassing the axis of said pressure vessel, said semicircular surfaces being alternately used for connecting two adjacent trays, and the path of the liquid from the outlet from said connecting ductl which supp1ies the liquid from the next higher tray, to the inlet into said connecting duct, which supplies the liquid to the next lower tray, extends via concentrically arranged and series-connected semicylindrical chambers, said liquid path ex-tending firstt from the region of said axis of the pressure vessel in the direction of the walls of said pressure vessel and then in the opposite direction.
The gas bubbles rising upwardly through the liquid should be as small as possible and should preferably be divided repeated-ly while rising. According to the present invention this is achieved when the volumel in which the liquid is in contact with the gas bu~bles~ is filled with fine-meshed gauze wire.
The present invention will be further described by way of the accompanying drawings, in which:-Fi~ure 1 is a vertical section along the lines A, B, C, D in Figure ~;
Figure 2 is a horizontal section along the line EF in Fiyure l;
Figure 3 is a horizontal section along the line GH in Figuxe l; and Figure 4 is a horizontal section along the line J~ in Figure 1.
Referring to Figure 1 three trays 1, 2 and 3 are shown in the vertical section ABCD. The tray 2 is described hereafter.
The other trays, whose number is optional, are identical directly or in mirror image.
From the gas chambers 4 below the tray 2 the gas passes via the opening 5 to the liquid chamber 6, through which it flows in the for~ of bubbles 7 on its way to the nex-t gas chamber 8 be-low the tray 3.
The liquid from the tray 3 flows via the connecting duct 9 to the tray 2. Said duct can ~e seen in Figure 1 as well as in Figures 2 and 3~ In the lower portion 10 of the connecting duct g, which can also be seen in Figure 4, the direction of the liquid path is reversed. The liquid flows to the liquid chamber 6 vertically upwards through the last portion 11 of the connecting duct 9. The further horizontal path of the liquid is evident from the arrows shown in Figure 2. This path ends in the space 12, which extends as far as the connecting duct 13 to the next lower tray 1.
Amon~ the partially cylindrical walls 14, 15, 16 and 17 disposed in the liquid chamber and shown in Figures 2, 3 and 4, only the two walls mentioned first can be seen in Figure 1 because of the manner in which the sections are represented. Walls pos-3Q sibly visi~le behind the sectional areas are not shown in thedrawing to avoid a complicated representation~
The celltl-al flat partition 18 ~ivides the annuli into chambers through which the liquid f:lows towards the outside and to the inside. The pressure housing 19 forms the external en-closure.
The num~er of concentric annuli formed by the partially cylindrical walls is optional, depending on the dimensions of the column and on the ~hroughput of liquid. The liquid chamber 6 is filled with gauze wire ~not shown in Figure 1).
The level 20 of the liquid in the liquid chamber adjusts itself as a function of the gas throughput with the exception of the uppermost tray, where this level must be adjusted either by means of the flow of liquid to the column or by means of the flow of liquid from the column.
The present invention relates ~o an apparatus for ex-changing material between a downwarclly flowlng liquid and an up-wardly flowing gas counterflow to the liquid. The conditions of the exchange of material for which the apparatus according to the present inven~ion is par~icularly suitable will be described hereinafter.
When the solubility of a gas, participating in the ex-change of material, is low in a liquid also participating in the exchange of material and ~urther when the exchange of material depends on a chemical reaction or on an isotope reaction in the liquid phase and the kinetics of this reaction are slow as compar-ed with the kinetics of the exchange of material of a dissolved ~as with the gas phase, then a lony residence time of the liquid in contact with the gas is required. This can be attained at a favourable cost when as large a proportion as possible of the column volume is used for the liquid. Furthermore when process conditions require the use of several trays, then they should be disposed in as small a number of pressure vessels as possible - while counterflow must be maintained and remixing flows must be avoided.
Material-exchange columns whose trays ~re superposed in a pressure vessel are known. In such a case the liquid ~lows from one tray via an overflow to the next lower tray. The over-~low is disposed in the gas cha,mber and is filled with liquid merely in the lowest region of the seal. Because of the hydro-dynamic conditions only approximately one quarter of the distance betwee~ the trays, ill which the liquid i5 in contact with the gas bubbles, can be used in these columns as the contact space.
Columns in wh:ich the liquid flows downwardly,primarily on the surface of packings, agalnst the gas ~low through the in-terstices of these packings are also known~ The proportion of volume filled with liquid in the columns is even substantially ~ 1 ~
6~
"~ smaller than that in the Eirst case. Columns which are filled almost completely with liquid and in which the gas to be contacted wit.h this li.quid flows upwardly in -the form of bubbles are also known.
The liquid is mixed in many dirèc-tions so that this kind of column can at best satisfy only the function of a single theoretical. tray.
Finally columns are known in which machines having a mechanical, electric or an intensified hydraulic drive for inten-sifying the exchange of material are known. In the last mentionedcase this occurs when the pressure drop on the gas side exceeds the available hydros-ta-tic pressure of the liquid and pumps must be used between -the trays in order -to convey the liquid. How-ever, these types of columns are -too costly to acquire and main-tain. Furthermore, in oprera-tion they can cause long interrup-tions due to their susceptibi.lity to trouble.
Accordi.ng to the presen-t invention there is provided an apparatus for exchanging material between a downwardly flowing liquid and an upwarding flowiny gas counterflow to said liquid, comprising a plurali-ty of perfora-ted trays superposed in a pres-sure vessel, comprising connecting ducts for passing the liquid to a next. lower -tray, the path of the li~uid at the end of said connecting ducts being arranged to be directed upwardly to prevent an undesired inflow of gas at said .end of the connec-ting ducts, said connecting ducts being disposed in the region of the axis o~ said pressure vessel. Suitably said connecting ducts comprise a pair of semicircular surfaces extending around the axis of said pressure vessel, said semicircular surfaces alternately connec-ting two adjacent trays. Desirably the liquid pa-th from an ou-tlet from said connec-ti.ng duct, which passes the liquid on from a next iligher tray, to the inl.et in said connecting duct, whi.ch removes the liquid to a next lowe~ tray, extends via concentrically dis-posect and ~,e.ries-connected semi-cylindrical chambers and sai~
]:iquid path e~tends first from the region of said axis of -the pressure vessel in the direction of the walls oE sa:id pressure vessel and then in -the opposite direc-tion. Preferably the space in which the liquid is in contact with -the gas bubbles is filled with fine-mesh gauze wire.
The present invention also provides a tray for use in such apparatus which comprises a perforated base; an inner con-centric part acting as a connecting duc-t, with a connectiny inlet tube for leading the liquid from an upstream tray to said -tray, concentrically disposed and series-connec-ted semi-cylindrical chambers formed by metal walls, an opening in said tray which is the outle-t fox a connecting inle-t tube -to a downstream tray, the metal wall, on the side of said opening, being lower than on the side of the connecting inlet tube from the upstream tray, so tha-t the liquid on said tray res-ts on a part of the perfora-ted base of said tray before ~alling into said opening.
Thus, according to the present invention in an appara-tus for exchanging material between a downwardly flowing liquid and an upwardly flowing gas couhterflow to said liquid, the liquid forms a hydrostatically continuous column extending from the top level to the lowes-t tapping point whereby the ratio of -the resi-dence time of the liquid to the volume content of the column is as large as possible. This column is merely loosened up by ~as bubbles in the regions of contact wi-th gas but it is not interrup-ted anywhere. ~ bubble cap is formed below each of said trays and within sai~ bubb]e cap ~he level of the liquid is displaced downwardly by the gas whereby, as compared wi-th the level of the liquid above the tray, a higher gas pressure is produced below the tray, the difference o:E said pressures being used to overcome -the pressure loss because of the gas flowing through the holes of t.he tray and simu:ltalleously to preven-t the flow o.~ liquid ~ ~B ~
26~
througll these holes. The connectin~ ducts for passin~ the ].iquid to the 3~
-- 2b next lower tray are disposed outside said bubblP caps or they cross said bubble caps. At the end of said connecting ducts the path of the liquid is directed upwards, thus preventing an un-desired entrance of gas at said end of the connecting ducts.
It is not sufficient to assure a long average residence time of the liquid on each tray~ but in order to attain a good tray fficiency, it is important that the divergence of this re-sidence time remains small when considering increasingly smaller portions of the -total liquid flow~ This condition cannot be sat-isfied without a forced guidance of the liquid via sufficientlynarrow ducts distributed over the entire tray~ According to the present invention this is achieved when said GOnneCting ducts are disposed in the region of the axis of the aforesaid pressure ve~-sel~ said connecting ducts consist of two semicircular surfaces encompassing the axis of said pressure vessel, said semicircular surfaces being alternately used for connecting two adjacent trays, and the path of the liquid from the outlet from said connecting ductl which supp1ies the liquid from the next higher tray, to the inlet into said connecting duct, which supplies the liquid to the next lower tray, extends via concentrically arranged and series-connected semicylindrical chambers, said liquid path ex-tending firstt from the region of said axis of the pressure vessel in the direction of the walls of said pressure vessel and then in the opposite direction.
The gas bubbles rising upwardly through the liquid should be as small as possible and should preferably be divided repeated-ly while rising. According to the present invention this is achieved when the volumel in which the liquid is in contact with the gas bu~bles~ is filled with fine-meshed gauze wire.
The present invention will be further described by way of the accompanying drawings, in which:-Fi~ure 1 is a vertical section along the lines A, B, C, D in Figure ~;
Figure 2 is a horizontal section along the line EF in Fiyure l;
Figure 3 is a horizontal section along the line GH in Figuxe l; and Figure 4 is a horizontal section along the line J~ in Figure 1.
Referring to Figure 1 three trays 1, 2 and 3 are shown in the vertical section ABCD. The tray 2 is described hereafter.
The other trays, whose number is optional, are identical directly or in mirror image.
From the gas chambers 4 below the tray 2 the gas passes via the opening 5 to the liquid chamber 6, through which it flows in the for~ of bubbles 7 on its way to the nex-t gas chamber 8 be-low the tray 3.
The liquid from the tray 3 flows via the connecting duct 9 to the tray 2. Said duct can ~e seen in Figure 1 as well as in Figures 2 and 3~ In the lower portion 10 of the connecting duct g, which can also be seen in Figure 4, the direction of the liquid path is reversed. The liquid flows to the liquid chamber 6 vertically upwards through the last portion 11 of the connecting duct 9. The further horizontal path of the liquid is evident from the arrows shown in Figure 2. This path ends in the space 12, which extends as far as the connecting duct 13 to the next lower tray 1.
Amon~ the partially cylindrical walls 14, 15, 16 and 17 disposed in the liquid chamber and shown in Figures 2, 3 and 4, only the two walls mentioned first can be seen in Figure 1 because of the manner in which the sections are represented. Walls pos-3Q sibly visi~le behind the sectional areas are not shown in thedrawing to avoid a complicated representation~
The celltl-al flat partition 18 ~ivides the annuli into chambers through which the liquid f:lows towards the outside and to the inside. The pressure housing 19 forms the external en-closure.
The num~er of concentric annuli formed by the partially cylindrical walls is optional, depending on the dimensions of the column and on the ~hroughput of liquid. The liquid chamber 6 is filled with gauze wire ~not shown in Figure 1).
The level 20 of the liquid in the liquid chamber adjusts itself as a function of the gas throughput with the exception of the uppermost tray, where this level must be adjusted either by means of the flow of liquid to the column or by means of the flow of liquid from the column.
Claims (5)
PROPERTY OR PRIVILEGE IS CLAIMED ARE DEFINED AS FOLLOWS:
1. An apparatus for exchanging material between a downwardly flowing liquid and an upwarding flowing gas counterflow to said liquid, comprising a plurality of perforated trays super-posed in a pressure vessel, comprising connecting ducts for pass-ing the liquid to a next lower tray, the path of the liquid at the end of said connecting ducts being arranged to be directed upwardly to prevent an undesired inflow of gas at said end of the connecting ducts, said connecting ducts being disposed in the region of the axis of said pressure vessel.
2. An apparatus according to claim 1, in which said connecting ducts comprise a pair of semicircular surfaces extend-ing around the axis of said pressure vessel, said semicircular surfaces alternately connecting two adjacent trays.
3. An apparatus according to claim 1, in which the liquid path from an outlet from said connecting ducts, which passes the liquid on from a next higher tray, to the inlet in said connecting duct, which removes the liquid to a next lower tray, extends via concentrically disposed and series-connected semi-cylindrical chambers and said liquid path extends first from the region of said axis of the pressure vessel in the direction of the walls of said pressure vessel and then in the opposite direction.
4. An apparatus according to claim 3, in which the space in which the liquid is in contact with the gas bubbles is filled with fine mesh gauze wire.
5. A tray for use in the apparatus according to claim 1, having a perforated base; an inner concentric part acting as a connecting duct, with a connecting inlet tube for leading the liquid from an upstream tray to concentrically disposed and series connected semi-cylindrical chamber formed by metal walls, an opening in said tray which is the outlet for a connecting inlet tube to a downstream tray, the metal wall, on the side of said opening, being lower than on the side of the connecting inlet tube from the upstream tray, so that the liquid on said tray rests on a part of the perforated base of said tray before falling into said opening.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CA000406335A CA1199262A (en) | 1982-06-30 | 1982-06-30 | Apparatus for exchanging material between a gas and a liquid |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CA000406335A CA1199262A (en) | 1982-06-30 | 1982-06-30 | Apparatus for exchanging material between a gas and a liquid |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1199262A true CA1199262A (en) | 1986-01-14 |
Family
ID=4123127
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA000406335A Expired CA1199262A (en) | 1982-06-30 | 1982-06-30 | Apparatus for exchanging material between a gas and a liquid |
Country Status (1)
| Country | Link |
|---|---|
| CA (1) | CA1199262A (en) |
-
1982
- 1982-06-30 CA CA000406335A patent/CA1199262A/en not_active Expired
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| MKEX | Expiry |