CN104815531A - Double-liquid alternative flow type mass transfer method and plate towers suitable for same - Google Patents
Double-liquid alternative flow type mass transfer method and plate towers suitable for same Download PDFInfo
- Publication number
- CN104815531A CN104815531A CN201510247883.0A CN201510247883A CN104815531A CN 104815531 A CN104815531 A CN 104815531A CN 201510247883 A CN201510247883 A CN 201510247883A CN 104815531 A CN104815531 A CN 104815531A
- Authority
- CN
- China
- Prior art keywords
- tower tray
- tower
- liquid
- layer
- mass transfer
- 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.)
- Granted
Links
- 239000007788 liquid Substances 0.000 title claims abstract description 85
- 238000000034 method Methods 0.000 title claims abstract description 32
- 239000007791 liquid phase Substances 0.000 claims abstract description 88
- 239000012071 phase Substances 0.000 claims abstract description 28
- 239000000463 material Substances 0.000 claims abstract description 3
- 241000736911 Turritella communis Species 0.000 claims description 38
- 238000002955 isolation Methods 0.000 claims description 2
- 238000000926 separation method Methods 0.000 abstract description 3
- 230000000630 rising effect Effects 0.000 abstract 1
- 238000004945 emulsification Methods 0.000 description 5
- 239000012530 fluid Substances 0.000 description 4
- 230000002411 adverse Effects 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 230000008676 import Effects 0.000 description 2
- 239000011344 liquid material Substances 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000010008 shearing Methods 0.000 description 1
Landscapes
- Physical Or Chemical Processes And Apparatus (AREA)
Abstract
The invention discloses a double-liquid alternative flow type mass transfer method. A gas phase and a liquid phase of materials are in countercurrent contact with each other in plate towers, so that mass transfer separation is realized; the gas phase penetrates through tower trays and a liquid layer above the tower trays layer by layer from the bottoms of the towers to the tops of the towers and then is discharged outside the towers; the liquid phase is divided into two streams; the two streams of liquid phases respectively flow downwards from the first layers of tower trays and the second layers of tower trays on the tops of the towers and are alternately contacted with the rising gas phase on the tower trays; the two streams of liquid phases flow in parallel and are not contacted with each other in the mass transfer process of the plate towers. The invention also discloses the two plate towers suitable for the double-liquid alternative flow type. After the mass transfer method and the plate towers suitable for the method are used, the problem caused by high liquid-gas ratio can be solved, the length of a liquid flow channel is guaranteed, and the emulsified gas-liquid state in the towers can be solved or greatly relieved; therefore, the separation efficiency of the towers can be greatly improved.
Description
Technical field
The present invention relates to gas-liquid mass transfer separation method and the mass transfer apparatus of petrochemical industry, especially relate to a kind of biliquid and replace flow pattern mass transfer method and applicable plate column thereof.
Background technology
General plate column is using column plate as the basic building block of gas-liquid contact, gas phase enters last layer tower tray by the sieve aperture on column plate, liquid phase passes across tower tray and enters lower one deck tower tray with the form of overflow by downspout, on column plate, gas-liquid two-phase contacts with cross-current flow, and the gas-liquid two-phase of whole tower is in adverse current step by step.Cross-flow configuration is the main flow of plate column, has mass-transfer efficiency high, and disposal ability is large, the advantages such as stable operation.But when large liquid measure, low gas phase load, owing to there is the larger hydraulics gradient, on tower tray, liquid level difference is excessive, easily causes bias current; Under large liquid-gas ratio, the liquid stream of high strength is comparatively large to the shearing force of gaseous fluid, and air-flow is cut into countless tiny bubble, forms a kind of gas-liquid state of emulsification, causes the separative efficiency of column plate significantly to reduce and even rushes tower accident.
For large liquid measure, low gas phase load system, mainly take multi-overflow tower tray or multiple downcomer tray at present, the former has the double overflow, the four overflow tower trays that generally use at present.The latter is as China Patent Publication No.: CN103432764A, in the patent document in publication date on December 11st, 2013, and disclosed a kind of multiple downcomer tray and there is its plate column, tower tray comprises: disk body; At least one anti-plate that jumps, at least one anti-plate that jumps described is located on described disk body so that described disk body is divided at least two regions; At least two are fallen liquid assembly, described at least two fall liquid assembly correspond respectively to described at least two regions arrange, fall liquid assembly described in each and include at least one column plate, at least one downspout and at least one seal pot that are set parallel to each other, wherein said downspout and described seal pot lay respectively at the both lateral sides of described column plate.
Although these patterns overcome the problem of plate column bias current preferably, also because this reducing fluid course length, sacrifice certain plate efficiency; Most importantly do not solve the emulsification state problem that the liquid-gas ratio on concrete column plate causes greatly, therefore in practical operation, liquid phase load does not increase, even far below design load.In addition tray structure also becomes very complicated.
Summary of the invention
The present invention is that the biliquid providing a kind of improvement replaces flow pattern mass transfer method in order to solve bias current that existing plate column exists under large liquid-gas ratio, emulsification state problem.Invention also provides the plate column being suitable for this mass transfer method.
To achieve these goals, the present invention is by the following technical solutions:
A kind of biliquid replaces flow pattern mass transfer method, and the gas phase of material realizes mass transfer with liquid phase counter current contacting in plate column and is separated, gas phase successively pass at the bottom of tower tower tray and liquid layer until tower top goes out tower; Liquid phase is divided into two strands, respectively from tower top ground floor tower tray and second layer tower tray toward dirty, two bursts of liquid phases alternately contacts with the gas phase risen on tower tray, also flow and do not contact between two bursts of liquid phases in plate column mass transport process.
As preferably, two bursts of liquid and gas alternately contacts, alternately once, the liquid phase on m layer tower tray through lower one deck tower tray, arrives the seal pot of m+2 layer tower tray by the downspout in plate column to every alternating floor tower tray.
As preferably, two bursts of liquid and gas alternately contacts, every two-layer tower tray alternately once, the liquid phase on n-th (n is odd number) layer tower tray through two-layer tower tray, arrives the seal pot of the n-th+3 layers tower tray by the downspout in plate column; Liquid phase on (n+1)th layer of tower tray, by the downspout in plate column, arrives the seal pot of the n-th+2 layers tower tray.
In the present invention, liquid phase is divided into two strands, replaces and gas phase adverse current contact mass transfer after shunting, so when not reducing total tower liquid-gas ratio, reducing the liquid-gas ratio on every one deck tower tray.In the mass transfer situation of large liquid measure, low gas phase load, compared to the mass transfer method of multi-overflow or multiple-downcomer, both the bias current problem because large liquid-gas ratio causes had been overcome, in turn ensure that fluid course length, also solve simultaneously or greatly alleviate the gas-liquid state of tower internal emulsification, therefore, it is possible to improve the separative efficiency of tower significantly.The structure of biliquid alternating current plate-type tower is also fairly simple simultaneously.
As preferably, the flow ratio of first burst of liquid phase and second burst of liquid phase is 0.2 ~ 5.
As preferably, the flow ratio of first burst of liquid phase and second burst of liquid phase is 1.
Be applicable to the plate column that biliquid replaces flow pattern mass transfer method and have following two kinds.
The structure of the first plate column is as follows:
A kind ofly be applicable to the plate column that biliquid replaces flow pattern mass transfer method, comprise tower shell, some tower trays are provided with in tower shell, tower tray is provided with downflow weir, seal pot, downspout is provided with between upper and lower tower tray, tower tray is divided into liquid receiving area successively by liquid phase flow direction, exchange area, liquid zone falls, the tower shell being positioned at tower tray ground floor is provided with the first inlet, the tower shell being positioned at the tower tray second layer is provided with the second inlet, the tower shell of tower tray last layer is provided with gas phase air inlet, downspout on m layer tower tray is communicated with the seal pot of m+2 layer tower tray, the dividing plate of isolation two bursts of liquid phases is set between adjacent tower tray.
As preferably, described tower tray has four layers at least, every four layers of tower tray in tower shell is a unit group, ground floor tower tray in a unit group and third layer tower tray are configured for the first switch room that first strand of liquid and gas mass transfer exchanges, second layer tower tray and the 4th layer of tower tray are configured for the second switch room that second strand of liquid and gas mass transfer exchanges, and arrange described dividing plate between the first switch room and the second switch room.
As preferably, the first inlet and the second inlet are separated by 90 degree along plate column periphery and are staggeredly arranged.
The first plate column, two bursts of liquid and gas alternately contacts, every alternating floor tower tray alternately once.Liquid phase splits into two strands before tower top enters tower, and two bursts of liquid phases are not in contact with each other, alternately the gentle mass transfer that contacts, and then two bursts of liquid phases are collaborated at tower reactor place.In order to realize two strands of every alternating floor tower trays of liquid phase alternately once, the flow trace cross of two bursts of liquid phases staggers, namely first burst of liquid phase tower tray 9 o'clock orientation to 3 o'clock orientation Radial Flow, second burst of liquid phase tower tray 6 o'clock orientation to 12 o'clock orientation Radial Flow.So the first inlet and the second inlet are separated by 90 degree along plate column periphery and are staggeredly arranged.Except ground floor tower tray, other tower trays are equipped with dividing plate in the liquid zone that falls of last layer tower tray, prevent last layer liquid phase from flowing into this layer of tower tray, cause two bursts of liquid phase mixing.
Above-mentioned dividing plate can be independent configuration, also can be that the tube wall one of downspout is dual-purpose.
The structure of the second plate column is as follows:
A kind ofly be applicable to the plate column that biliquid replaces flow pattern mass transfer method, comprise tower shell, some tower trays are provided with in tower shell, tower tray is provided with downflow weir, seal pot, downspout is provided with between upper and lower tower tray, tower tray is divided into liquid receiving area successively by liquid phase flow direction, exchange area, liquid zone falls, the tower shell being positioned at tower tray ground floor is provided with the first inlet, the tower shell being positioned at the tower tray second layer is provided with the second inlet, the tower shell of tower tray last layer is provided with gas phase air inlet, n-th n is the seal pot of downspout connection the n-th+3 layers tower tray on odd-level tower tray, downspout on (n+1)th layer of tower tray is communicated with the seal pot of the n-th+2 layers tower tray.
As preferably, described tower tray has four layers at least, every four layers of tower tray in tower shell is a unit group, ground floor tower tray in a unit group and the 4th layer of tower tray are configured for the first switch room that first strand of liquid and gas mass transfer exchanges, and second layer tower tray and third layer tower tray are configured for the second switch room that second strand of liquid and gas mass transfer exchanges.
The second plate column, two bursts of liquid and gas alternately contacts, every two-layer tower tray alternately once.Liquid phase splits into two strands before tower top enters tower, and two bursts of liquid phases are not in contact with each other, alternately the gentle mass transfer that contacts, and then two bursts of liquid phases are collaborated at tower reactor place.Every two-layer tower tray alternately once, its flow trace is parallel flowing abreast to two bursts of liquid phases, and two strands of liquid phase flow traces stagger without cross.Its downspout also divides and is listed in tower shell both sides, and the downspout of Liang Ge switch room is arranged side by side.
The beneficial effect that the present invention has: biliquid alternating current plate-type tower had both overcome the bias current problem because large liquid-gas ratio causes, in turn ensure that fluid course length, also solve simultaneously or greatly alleviate the gas-liquid state of tower internal emulsification, therefore, it is possible to improve the separative efficiency of tower significantly.
Accompanying drawing explanation
Fig. 1 is the structural representation of the embodiment of the present invention 1 plate column.
Fig. 2 is the A-A sectional view of Fig. 1.
Fig. 3 is the B-B sectional view of Fig. 1.
Fig. 4 is the C-C sectional view of Fig. 1.
Fig. 5 is the D-D sectional view of Fig. 1.
Fig. 6 is the E-E sectional view of Fig. 1.
Fig. 7 is the F-F sectional view of Fig. 1.
Fig. 8 is the flow process reference diagram of the embodiment of the present invention 1 plate column.
Fig. 9 is the structural representation of the embodiment of the present invention 2 plate column.
Figure 10 is the U-U sectional view of Fig. 9.
Figure 11 is the V-V sectional view of Fig. 9.
Figure 12 is the W-W sectional view of Fig. 9.
Figure 13 is the X-X sectional view of Fig. 9.
Figure 14 is the Y-Y sectional view of Fig. 9.
Figure 15 is the Z-Z sectional view of Fig. 9.
Figure 16 is the flow process reference diagram of the embodiment of the present invention 2 plate column.
In figure: tower shell 1, tower tray 2, downflow weir 3, seal pot 4, downspout 5, first inlet 61, second inlet 62;
Liquid zone L1-1 falls in first burst of liquid phase, first gang of liquid phase liquid receiving area L1-2, first gang of liquid material exchange district L1-3, and liquid zone L2-1 falls in second burst of liquid phase, second gang of liquid phase liquid receiving area L2-2, second gang of liquid material exchange district L3-3.
Detailed description of the invention
Below in conjunction with the drawings and specific embodiments, the present invention will be further described.
Embodiment 1
Be applicable to the plate column that biliquid replaces flow pattern mass transfer method, the top section structure of plate column as shown in Figure 1, comprises tower shell 1, is provided with multilayer tower tray 2 in tower shell, and tower tray 2 is provided with downflow weir 3, seal pot 4.Be provided with downspout 5 between upper and lower tower tray, tower tray is divided into liquid receiving area, exchange area successively by liquid phase flow direction, falls liquid zone.The tower shell being positioned at tower tray ground floor is provided with the first inlet 61, first inlet 61 and aims at seal pot 4 on ground floor tower tray.The tower shell being positioned at the tower tray second layer is provided with the second inlet 62, second inlet 62 and aims at seal pot 4 on second layer tower tray.First inlet and the second inlet are separated by 90 degree along plate column periphery and are staggeredly arranged.The tower shell of tower tray last layer is provided with gas phase air inlet.
Tower tray has three Floor 12s, and every four layers of the tower tray in tower shell is a unit group.Ground floor tower tray in a unit group and third layer tower tray are configured for the first switch room that first strand of liquid and gas mass transfer exchanges, second layer tower tray and the 4th layer of tower tray are configured for the second switch room that second strand of liquid and gas mass transfer exchanges, and arrange dividing plate between the first switch room and the second switch room.Except ground floor tower tray, other tower trays are equipped with dividing plate in the liquid zone that falls of last layer tower tray, prevent last layer liquid phase from flowing into this layer of tower tray, cause two bursts of liquid phase mixing.Dividing plate is herein that the downspout tube wall of last layer serves as dividing plate.
Gas phase at the bottom of tower successively through tower tray and liquid layer until tower top goes out tower; Liquid phase is divided into two strands, respectively from tower top ground floor tower tray and second layer tower tray toward dirty, two bursts of liquid phases alternately contacts with the gas phase risen on tower tray, also flow and do not contact between two bursts of liquid phases in plate column mass transport process.Two bursts of liquid and gas alternately contacts, alternately once, the liquid phase on m layer tower tray through lower one deck tower tray, arrives the seal pot of m+2 layer tower tray by the downspout in plate column to every alternating floor tower tray.The flow ratio of first burst of liquid phase and second burst of liquid phase is 1:1.
In order to realize two strands of every alternating floor tower trays of liquid phase alternately once, the flow trace cross of two bursts of liquid phases staggers.First burst of liquid phase flows to 3 o'clock orientation in the 9 o'clock orientation of ground floor tower tray, and second burst of liquid phase flows to 12 o'clock orientation in the 6 o'clock orientation of second layer tower tray.Reaction is in the structure of tower tray, and the tray structure of the first six layer of plate column is as shown in Fig. 2, Fig. 3, Fig. 4, Fig. 5, Fig. 6, Fig. 7.
On plate column, as shown in Figure 8, L represents liquid phase to gas-liquid mass transfer, and G represents gas phase.Tower tray is divided into liquid receiving area, exchange area successively by liquid phase flow direction, falls liquid zone, represents with L j-k, j represents that liquid phase is classified, and first burst of liquid phase is 1, second burst of liquid phase is 2; K represents region, and wherein falling liquid zone is 1, and liquid receiving area is 2, and exchange area is 3.
Liquid phase L is divided into two gangs of L1, L2 in equal size.Wherein L1 enters the liquid receiving area L1-2 of tower top ground floor tower tray, after flowing through the exchange area L1-3 contact mass transfer of ground floor tower tray, crosses the downspout that downflow weir enters ground floor tower tray, arrives the liquid receiving area L1-2 of third layer tower tray; Then after flowing through the exchange area L1-3 contact mass transfer of third layer tower tray, cross the downspout that downflow weir enters third layer tower tray, arrive the liquid receiving area L1-2 of layer 5 tower tray ... so finally flow into tower reactor through each odd-level tower tray successively.L2 enters the liquid receiving area L2-2 of tower top second layer tower tray, after flowing through the exchange area L2-3 contact mass transfer of second layer tower tray, crosses the downspout that downflow weir enters second layer tower tray, arrives the liquid receiving area L2-2 of the 4th layer of tower tray; Then after flowing through the exchange area L2-3 contact mass transfer of the 4th layer of tower tray, cross the downspout that downflow weir enters the 4th layer of tower tray, arrive the liquid receiving area L2-2 of layer 6 tower tray ... so finally import tower reactor through each even level tower tray successively, after mixing with L1, go out tower.
Embodiment 2
Be applicable to the plate column that biliquid replaces flow pattern mass transfer method, the top section structure of plate column as shown in Figure 9, comprises tower shell 1, is provided with multilayer tower tray 2 in tower shell, and tower tray 2 is provided with downflow weir 3, seal pot 4.Be provided with downspout 5 between upper and lower tower tray, tower tray is divided into liquid receiving area, exchange area successively by liquid phase flow direction, falls liquid zone.The tower shell being positioned at tower tray ground floor is provided with the first inlet 61, first inlet 61 and aims at seal pot 4 on ground floor tower tray.The tower shell being positioned at the tower tray second layer is provided with the second inlet 62, second inlet 62 and aims at seal pot 4 on second layer tower tray.The tower shell of tower tray last layer is provided with gas phase air inlet.
Tower tray has three Floor 12s, and every four layers of the tower tray in tower shell is a unit group.Ground floor tower tray in a unit group and the 4th layer of tower tray are configured for the first switch room that first strand of liquid and gas mass transfer exchanges, and second layer tower tray and third layer tower tray are configured for the second switch room that second strand of liquid and gas mass transfer exchanges.
Gas phase at the bottom of tower successively through tower tray and liquid layer until tower top goes out tower; Liquid phase is divided into two strands, respectively from tower top ground floor tower tray and second layer tower tray toward dirty, two bursts of liquid phases alternately contacts with the gas phase risen on tower tray, also flow and do not contact between two bursts of liquid phases in plate column mass transport process.Two bursts of liquid and gas alternately contacts, every two-layer tower tray alternately once.Liquid phase on n-th (n is odd number) layer tower tray through two-layer tower tray, arrives the seal pot of the n-th+3 layers tower tray by the downspout in plate column; Liquid phase on (n+1)th layer of tower tray, by the downspout in plate column, arrives the seal pot of the n-th+2 layers tower tray.The flow ratio of first burst of liquid phase and second burst of liquid phase is 0.2.
The tray structure sectional view of the first six layer of Figure 10, Figure 11, Figure 12, Figure 13, Figure 14, Figure 15 plate column.On plate column, as shown in figure 16, L represents liquid phase to gas-liquid mass transfer, and G represents gas phase.Tower tray is divided into liquid receiving area, exchange area successively by liquid phase flow direction, falls liquid zone, represents with L j-k, j represents that liquid phase is classified, and first burst of liquid phase is 1, second burst of liquid phase is 2; K represents region, and wherein falling liquid zone is 1, and liquid receiving area is 2, and exchange area is 3.
Liquid phase is that 1:5 is divided into two gangs of L1, L2 by flow ratio.Wherein L1 enters the liquid receiving area L1-2 of tower top ground floor tower tray, after flowing through the exchange area L1-3 contact mass transfer of ground floor tower tray, crosses the downspout that downflow weir enters ground floor tower tray, arrives the liquid receiving area L1-2 of the 4th layer of tower tray; Then after flowing through the exchange area L1-3 contact mass transfer of the 4th layer of tower tray, cross the downspout that downflow weir enters the 4th layer of tower tray, arrive the liquid receiving area L1-2 of layer 5 tower tray ... finally flow into tower reactor by that analogy.L2 enters the liquid receiving area L2-2 of tower top second layer tower tray, after flowing through the exchange area L2-3 contact mass transfer of second layer tower tray, crosses the downspout that downflow weir enters second layer tower tray, arrives the liquid receiving area L2-2 of third layer tower tray; Then after flowing through the exchange area L2-3 contact mass transfer of third layer tower tray, cross the downspout that downflow weir enters third layer tower tray, arrive the liquid receiving area L2-2 of layer 6 tower tray ... finally import tower reactor by that analogy, after mixing with L1, go out tower.
Embodiment 3
Be with the difference of embodiment 1, the flow ratio of first burst of liquid phase and second burst of liquid phase is 5:1.
Claims (10)
1. biliquid replaces a flow pattern mass transfer method, and the gas phase of material realizes mass transfer with liquid phase counter current contacting in plate column and is separated, and it is characterized in that, gas phase at the bottom of tower successively through tower tray and liquid layer until tower top goes out tower; Liquid phase is divided into two strands, respectively from tower top ground floor tower tray and second layer tower tray toward dirty, two bursts of liquid phases alternately contacts with the gas phase risen on tower tray, also flow and do not contact between two bursts of liquid phases in plate column mass transport process.
2. a kind of biliquid according to claim 1 replaces flow pattern mass transfer method, it is characterized in that, two bursts of liquid and gas alternately contacts, every alternating floor tower tray alternately once, liquid phase on m layer tower tray through lower one deck tower tray, arrives the seal pot of m+2 layer tower tray by the downspout in plate column.
3. a kind of biliquid according to claim 1 replaces flow pattern mass transfer method, it is characterized in that, two bursts of liquid and gas alternately contacts, every two-layer tower tray alternately once, liquid phase on n-th (n is odd number) layer tower tray through two-layer tower tray, arrives the seal pot of the n-th+3 layers tower tray by the downspout in plate column; Liquid phase on (n+1)th layer of tower tray, by the downspout in plate column, arrives the seal pot of the n-th+2 layers tower tray.
4. a kind of biliquid according to Claims 2 or 3 replaces flow pattern mass transfer method, it is characterized in that, the flow ratio of first burst of liquid phase and second burst of liquid phase is 0.2 ~ 5.
5. a kind of biliquid according to claim 4 replaces flow pattern mass transfer method, it is characterized in that, the flow ratio of first burst of liquid phase and second burst of liquid phase is 1.
6. one kind is applicable to the plate column that biliquid as claimed in claim 2 replaces flow pattern mass transfer method, comprise tower shell (1), some tower trays (2) are provided with in tower shell, tower tray (2) is provided with downflow weir (3), seal pot (4), downspout (5) is provided with between upper and lower tower tray, tower tray is divided into liquid receiving area successively by liquid phase flow direction, exchange area, liquid zone falls, it is characterized in that, the tower shell being positioned at tower tray ground floor is provided with the first inlet (61), the tower shell being positioned at the tower tray second layer is provided with the second inlet (62), the tower shell of tower tray last layer is provided with gas phase air inlet, downspout on m layer tower tray is communicated with the seal pot of m+2 layer tower tray, the dividing plate of isolation two bursts of liquid phases is set between adjacent tower tray.
7. be according to claim 6ly a kind ofly applicable to the plate column that biliquid replaces flow pattern mass transfer method, it is characterized in that, described tower tray has four layers at least, every four layers of tower tray in tower shell is a unit group, ground floor tower tray in a unit group and third layer tower tray are configured for the first switch room that first strand of liquid and gas mass transfer exchanges, second layer tower tray and the 4th layer of tower tray are configured for the second switch room that second strand of liquid and gas mass transfer exchanges, and arrange described dividing plate between the first switch room and the second switch room.
8. be according to claim 6ly a kind ofly applicable to the plate column that biliquid replaces flow pattern mass transfer method, it is characterized in that, the first inlet (61) and the second inlet (62) are separated by 90 degree along plate column periphery and are staggeredly arranged.
9. one kind is applicable to the plate column that biliquid as claimed in claim 3 replaces flow pattern mass transfer method, comprise tower shell, some tower trays are provided with in tower shell, tower tray is provided with downflow weir, seal pot, downspout is provided with between upper and lower tower tray, tower tray is divided into liquid receiving area successively by liquid phase flow direction, exchange area, liquid zone falls, it is characterized in that, the tower shell being positioned at tower tray ground floor is provided with the first inlet, the tower shell being positioned at the tower tray second layer is provided with the second inlet, the tower shell of tower tray last layer is provided with gas phase air inlet, downspout on n-th (n is odd number) layer tower tray is communicated with the seal pot of the n-th+3 layers tower tray, downspout on (n+1)th layer of tower tray is communicated with the seal pot of the n-th+2 layers tower tray.
10. be according to claim 9ly a kind ofly applicable to the plate column that biliquid replaces flow pattern mass transfer method, it is characterized in that, described tower tray has four layers at least, every four layers of tower tray in tower shell is a unit group, ground floor tower tray in a unit group and the 4th layer of tower tray are configured for the first switch room that first strand of liquid and gas mass transfer exchanges, and second layer tower tray and third layer tower tray are configured for the second switch room that second strand of liquid and gas mass transfer exchanges.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510247883.0A CN104815531B (en) | 2015-05-15 | 2015-05-15 | Double-liquid alternative flow type mass transfer method and plate towers suitable for same |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510247883.0A CN104815531B (en) | 2015-05-15 | 2015-05-15 | Double-liquid alternative flow type mass transfer method and plate towers suitable for same |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN104815531A true CN104815531A (en) | 2015-08-05 |
| CN104815531B CN104815531B (en) | 2017-01-18 |
Family
ID=53726155
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201510247883.0A Expired - Fee Related CN104815531B (en) | 2015-05-15 | 2015-05-15 | Double-liquid alternative flow type mass transfer method and plate towers suitable for same |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN104815531B (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109663561A (en) * | 2018-12-21 | 2019-04-23 | 北京泽华化学工程有限公司 | For the Vierendeel girder and tower inner assembly in tower |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS4954272A (en) * | 1972-05-09 | 1974-05-27 | ||
| GB2130499A (en) * | 1982-11-24 | 1984-06-06 | Nippon Kayaku Kk | Baffle tray tower |
| US4496430A (en) * | 1981-01-22 | 1985-01-29 | Distillation Technology Limited | Mass transfer apparatus |
| CN1088844A (en) * | 1992-09-28 | 1994-07-06 | 戈里特斯奇公司 | Gas-liquid contact device |
| US6645350B1 (en) * | 2001-06-15 | 2003-11-11 | Uop Llc | Dividing wall column fractionation tray |
| CN201049217Y (en) * | 2007-04-05 | 2008-04-23 | 南京化工职业技术学院 | Board type tower |
| CN104492349A (en) * | 2014-11-20 | 2015-04-08 | 常州市安佳涂装设备有限公司 | Improved plate-type tower |
-
2015
- 2015-05-15 CN CN201510247883.0A patent/CN104815531B/en not_active Expired - Fee Related
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS4954272A (en) * | 1972-05-09 | 1974-05-27 | ||
| US4496430A (en) * | 1981-01-22 | 1985-01-29 | Distillation Technology Limited | Mass transfer apparatus |
| GB2130499A (en) * | 1982-11-24 | 1984-06-06 | Nippon Kayaku Kk | Baffle tray tower |
| CN1088844A (en) * | 1992-09-28 | 1994-07-06 | 戈里特斯奇公司 | Gas-liquid contact device |
| US6645350B1 (en) * | 2001-06-15 | 2003-11-11 | Uop Llc | Dividing wall column fractionation tray |
| CN201049217Y (en) * | 2007-04-05 | 2008-04-23 | 南京化工职业技术学院 | Board type tower |
| CN104492349A (en) * | 2014-11-20 | 2015-04-08 | 常州市安佳涂装设备有限公司 | Improved plate-type tower |
Non-Patent Citations (1)
| Title |
|---|
| 计建炳: "板式塔的进展", 《化工时刊》 * |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109663561A (en) * | 2018-12-21 | 2019-04-23 | 北京泽华化学工程有限公司 | For the Vierendeel girder and tower inner assembly in tower |
| CN109663561B (en) * | 2018-12-21 | 2020-12-22 | 北京泽华化学工程有限公司 | Frame beam used in tower and assembly in tower |
Also Published As
| Publication number | Publication date |
|---|---|
| CN104815531B (en) | 2017-01-18 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US10458703B2 (en) | Method for liquid-vapor contacting in a mass transfer column using multiple pass, parallel flow downcomer trays | |
| CN102961888B (en) | Flow-separation back-mixing-free spraying tower disc | |
| AU737526B2 (en) | Co-current contacting separation tray design and methods for using same | |
| AU718717B2 (en) | Co-current contacting separation tray design and methods for using same | |
| KR101879899B1 (en) | Use of downcomer beam to support adjacent cross flow trays within a mass transfer column and process involving same | |
| US7052000B2 (en) | Liquid distributor and method for operating the same | |
| CN101927097A (en) | By in having the tower of one or more continuous partition walls, distilling the method for separating one or more incoming mixtures | |
| US20140318945A1 (en) | Distillation station | |
| CN104815531A (en) | Double-liquid alternative flow type mass transfer method and plate towers suitable for same | |
| EP1372806A1 (en) | Gas-liquid separator | |
| US2804292A (en) | Gas-liquid contact apparatus | |
| CN112774237B (en) | Heat integration shell-and-tube type next door tower system | |
| US20220370973A1 (en) | Grid-like fractal distributor or collector element | |
| CN204745712U (en) | Biliquid is flow pattern plate tower in turn | |
| KR20200133791A (en) | Vapor-liquid contact apparatus and method with offset contact modules | |
| CN201791392U (en) | Stereoscopic mass transfer liquid identical-direction flow tower | |
| TWI701074B (en) | Vapor-liquid contacting apparatus and process with cross contacting | |
| WO2001060481A2 (en) | Column for counter-currently contacting gas and liquid | |
| CN103301645B (en) | A kind of High-flux plate-type tower | |
| CN205549653U (en) | Divide wall rectifying column column plate and have branch wall rectifying column of this column plate | |
| CN203281316U (en) | Complete countercurrent mass transfer unit and tower with same | |
| CN104784968B (en) | A kind of method of continuous phase cocurrent extraction tower and extraction | |
| CN100546688C (en) | The vapour-liquid separating phase transformation is imitated column plate and platelet entirely apart from rectifying column | |
| CN201551865U (en) | Rectifying tower | |
| CN103252205B (en) | Full-countercurrent mass transfer unit and tower plate with unit |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| EXSB | Decision made by sipo to initiate substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20170118 |