CN104815531B - 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
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- CN104815531B CN104815531B CN201510247883.0A CN201510247883A CN104815531B CN 104815531 B CN104815531 B CN 104815531B CN 201510247883 A CN201510247883 A CN 201510247883A CN 104815531 B CN104815531 B CN 104815531B
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- 239000007788 liquid Substances 0.000 title claims abstract description 89
- 238000000034 method Methods 0.000 title claims abstract description 32
- 239000007791 liquid phase Substances 0.000 claims abstract description 87
- 239000012071 phase Substances 0.000 claims abstract description 30
- 230000000630 rising effect Effects 0.000 claims abstract description 5
- 239000000463 material Substances 0.000 claims abstract description 3
- 241000736911 Turritella communis Species 0.000 claims description 24
- 238000002955 isolation Methods 0.000 claims description 2
- 238000001727 in vivo Methods 0.000 claims 1
- 238000000926 separation method Methods 0.000 abstract description 4
- 238000004945 emulsification Methods 0.000 description 5
- 239000012530 fluid Substances 0.000 description 3
- 230000000712 assembly Effects 0.000 description 2
- 238000000429 assembly Methods 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- 230000008676 import Effects 0.000 description 2
- 239000011344 liquid material Substances 0.000 description 2
- 230000002411 adverse Effects 0.000 description 1
- 238000010008 shearing Methods 0.000 description 1
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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 the gas-liquid mass transfer separation method of petrochemical industry and mass transfer apparatus, especially relate to a kind of biliquid
Alternately flow pattern mass transfer method and its applicable plate column.
Background technology
Using column plate as the basic building block of gas-liquid contact, the sieve aperture that gas phase is passed through on column plate enters last layer to general plate column
Tower tray, liquid phase passes across tower tray and enters next layer of tower tray by downspout in the form of overflow, on column plate gas-liquid two-phase with
Cross-current flow contacts, and the gas-liquid two-phase of whole tower is in step by step countercurrently.Cross-flow configuration is the main flow of plate column, has mass-transfer efficiency height,
Disposal ability is big, the advantages of stable operation.But in the case of big liquid measure, low gas phase load, due to there is larger hydraulics
The gradient, on tower tray, liquid level difference is excessive, easily causes bias current；Under big liquid-gas ratio, the liquor stream of high intensity is to the shearing force of gaseous fluid relatively
Greatly, air-flow is cut into countless tiny bubbles, forms a kind of gas-liquid state of emulsification, causes the separative efficiency of column plate significantly to drop
Low or even rush tower accident.
For big liquid measure, low gas phase load system, mainly take multi-overflow tower tray or multiple downcomer tray, Qian Zheyou at present
The double overflow that commonly uses at present, four overflow tower trays.The latter's such as China Patent Publication No.: cn103432764a, publication date 2013
In the patent document on December 11, disclosed a kind of multiple downcomer tray and there is its plate column, tower tray includes: disk body；
At least one anti-jump plate, at least one anti-jump plate described is located on described disk body so that described disk body is divided at least two regions；
At least two descending liquid assemblies, described at least two descending liquid assemblies correspond respectively to described at least two regions settings, described in each
Descending liquid assembly all includes at least one column plate, at least one downspout and at least one seal pot being set parallel to each other, wherein
Described downspout and described seal pot are respectively positioned at the both lateral sides of described column plate.
Although these patterns preferably overcome the problem of plate column bias current, also therefore reduce fluid course length,
Sacrifice certain plate efficiency；Most importantly do not solve the problems, such as the emulsification state that the liquid-gas ratio on concrete column plate leads to greatly, because
In this practical operation, liquid phase load does not increase, even much lower than design load.In addition tray structure also becomes extremely complex.
Content of the invention
The present invention is to solve the problems, such as the bias current, emulsification state that existing plate column exists under big liquid-gas ratio, there is provided one
Plant improved biliquid and replace flow pattern mass transfer method.Invention also provides being suitable for the plate column of this mass transfer method.
To achieve these goals, the present invention employs the following technical solutions:
A kind of biliquid replaces flow pattern mass transfer method, and the gas phase of material and liquid phase counter current contacting in plate column are realized mass transfer and divided
From gas phase successively passes through tower tray and liquid layer thereon until tower top goes out tower from bottom of towe；Liquid phase is divided into two strands, respectively from tower top first
Toward dirty, two bursts of liquid phases are alternately contacted with the gas phase rising on tower tray for layer tower tray and second layer tower tray, between two bursts of liquid phases
In plate column mass transport process, cocurrent does not contact.
Preferably, two strands of liquid and gas replace contacting, every alternating floor tower tray alternately once, liquid on m layer tower tray
The downspout mutually passing through in plate column passes through next layer of tower tray, reaches the seal pot of m+2 layer tower tray.
Preferably, two strands of liquid and gas replace contacting, every two-layer tower tray alternately once, n-th (n is odd number) layer tower
The downspout that liquid phase on disk is passed through in plate column passes through two-layer tower tray, reaches the seal pot of the n-th+3 layers tower tray；(n+1)th layer of tower
Liquid phase on disk passes through the downspout in plate column, reaches 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 do not reducing total tower
In the case of liquid-gas ratio, reduce the liquid-gas ratio on each layer of tower tray.In the case of big liquid measure, the mass transfer of low gas phase load, phase
Ratio, in the mass transfer method of multi-overflow or multiple-downcomer, had both overcome the bias current problem causing because of big liquid-gas ratio, in turn ensure that liquor stream
Passage length, also solves simultaneously or greatly alleviates the gas-liquid state of tower internal emulsification, therefore, it is possible to the separation of tower is significantly increased
Efficiency.Simultaneously biliquid replace flow pattern plate column structure also fairly simple.
Preferably, the flow ratio of first burst of liquid phase and second burst of liquid phase is 0.2 ~ 5.
Preferably, the flow ratio of first burst of liquid phase and second burst of liquid phase is 1.
Be applied to biliquid replace flow pattern mass transfer method plate column have following two.
The structure of the first plate column is as follows:
A kind of be applied to biliquid replace flow pattern mass transfer method plate column, including tower shell, in tower casing body, be provided with some towers
Disk, tower tray is provided with downflow weir, seal pot, is provided with downspout between upper and lower tower tray, and tower tray is divided into by liquid phase flow direction
Liquid receiving area, exchange area, descending liquid area, are provided with the first inlet positioned at the tower shell of tower tray ground floor, positioned at the tower tray second layer
Tower shell is provided with the second inlet, and the tower shell of tower tray last layer is provided with gas phase air inlet, and the downspout on m layer tower tray is even
The seal pot of logical m+2 layer tower tray, the dividing plate of two bursts of liquid phases of setting isolation between adjacent tower tray.
Preferably, at least four layers of described tower tray, every four layers of the tower tray in tower casing body is a unit group, a unit
Ground floor tower tray in group and third layer tower tray constitute the first switch room exchanging for first strand of liquid and gas mass transfer, and second
Layer tower tray and the 4th layer of tower tray constitute the second switch room exchanging for second strand of liquid and gas mass transfer, the first switch room and the
Described dividing plate is set between two switch rooms.
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 strands of liquid and gas replace contact, and every alternating floor tower tray is alternately once.Liquid phase enters from tower top
Two strands are split into, two bursts of liquid phases are not in contact with each other, alternately the gentle mass transfer that contacts, then two bursts of liquid phases are collaborated at tower reactor before tower.
In order to realize the every alternating floor tower tray of two bursts of liquid phases alternately once, the flow trace cross of two bursts of liquid phases staggers, i.e. first burst of liquid phase
In 9 o ' clock orientation to 3 o ' clock orientation Radial Flow of tower tray, 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
Outside disk, other tower trays are equipped with dividing plate in the descending liquid area of last layer tower tray, prevent last layer liquid phase from flowing into this layer of tower tray, cause two
Stock liquid phase mixing.
Above-mentioned dividing plate can be separately configured or downspout tube wall one dual-purpose.
The structure of second plate column is as follows:
A kind of be applied to biliquid replace flow pattern mass transfer method plate column, including tower shell, in tower casing body, be provided with some towers
Disk, tower tray is provided with downflow weir, seal pot, is provided with downspout between upper and lower tower tray, and tower tray is divided into by liquid phase flow direction
Liquid receiving area, exchange area, descending liquid area, are provided with the first inlet positioned at the tower shell of tower tray ground floor, positioned at the tower tray second layer
Tower shell is provided with the second inlet, and the tower shell of tower tray last layer is provided with gas phase air inlet, and the n-th n is on odd-level tower tray
Downspout connects the seal pot of the n-th+3 layers tower tray, and the downspout on (n+1)th layer of tower tray connects the seal pot of the n-th+2 layers tower tray.
Preferably, at least four layers of described tower tray, every four layers of the tower tray in tower casing body is a unit group, a unit
Ground floor tower tray in group and the 4th layer of tower tray constitute the first switch room exchanging for first strand of liquid and gas mass transfer, and second
Layer tower tray and third layer tower tray constitute the second switch room exchanging for second strand of liquid and gas mass transfer.
Second plate column, two strands of liquid and gas replace contact, every two-layer tower tray alternately once.Liquid phase enters from tower top
Two strands are split into, two bursts of liquid phases are not in contact with each other, alternately the gentle mass transfer that contacts, then two bursts of liquid phases are collaborated at tower reactor before tower.
Every two-layer tower tray alternately once, its flow trace is abreast to flow parallel to two bursts of liquid phases, two strands of liquid phase flow traces without
Cross staggers.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 invention has the benefit that biliquid had replaced flow pattern plate column and both having overcome and had asked because of the bias current that big liquid-gas ratio causes
Topic, in turn ensure that fluid course length, also solves simultaneously or greatly alleviate the gas-liquid state of tower internal emulsification, therefore, it is possible to significantly
Ground improves the separative efficiency of tower.
Brief description
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 of the embodiment of the present invention 1 plate column with reference to figure.
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 of the embodiment of the present invention 2 plate column with reference to figure.
In figure: tower shell 1, tower tray 2, downflow weir 3, seal pot 4, downspout 5, the first inlet 61, the second inlet 62；
First gang of liquid phase descending liquid area l1-1, first gang of liquid phase liquid receiving area l1-2, first gang of liquid material exchange area l1-3, second strand
Liquid phase descending liquid area l2-1, second gang of liquid phase liquid receiving area l2-2, second gang of liquid material exchange area l3-3.
Specific embodiment
The present invention will be further described with reference to the accompanying drawings and detailed description.
Embodiment 1
A kind of be applied to the plate column that biliquid replaces flow pattern mass transfer method, the top section structure of plate column as shown in figure 1,
Including tower shell 1, in tower casing body, it is provided with multilayer tower tray 2, tower tray 2 is provided with downflow weir 3, seal pot 4.It is provided with fall up and down between tower tray
Liquid pipe 5, tower tray is divided into liquid receiving area, exchange area, descending liquid area by liquid phase flow direction.Tower shell positioned at tower tray ground floor
It is provided with the first inlet 61, the first inlet 61 is directed at the seal pot 4 on ground floor tower tray.Tower casing positioned at the tower tray second layer
Body is provided with the second inlet 62, and the second inlet 62 is directed at the seal pot 4 on second layer tower tray.First inlet and second enters
Liquid opening's edge plate column periphery is separated by 90 degree and is 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 casing body is a unit group.Ground floor in one unit group
Tower tray and third layer tower tray constitute the first switch room exchanging for first strand of liquid and gas mass transfer, second layer tower tray and the 4th
Layer tower tray constitutes the second switch room exchanging for second strand of liquid and gas mass transfer, sets between the first switch room and the second switch room
Put dividing plate.In addition to ground floor tower tray, other tower trays are equipped with dividing plate in the descending liquid area of last layer tower tray, prevent last layer liquid phase stream
Enter this layer of tower tray, cause two bursts of liquid phase mixing.Dividing plate herein is that the descending liquid tube wall of last layer serves as dividing plate.
Gas phase successively passes through tower tray and liquid layer thereon until tower top goes out tower from bottom of towe；Liquid phase is divided into two strands, respectively from tower
Toward dirty, two bursts of liquid phases are alternately contacted with the gas phase rising on tower tray, two bursts of liquid phases for top ground floor tower tray and second layer tower tray
Between in plate column mass transport process cocurrent do not contact.Two strands of liquid and gas replace and contact, every alternating floor tower tray alternately once,
The downspout that liquid phase on m layer tower tray is passed through in plate column passes through next layer of tower tray, reaches the seal pot of m+2 layer tower tray.
The flow ratio of first burst of liquid phase and second burst of liquid phase is 1:1.
In order to realize the every alternating floor tower tray of two bursts of liquid phases alternately once, the flow trace cross of two bursts of liquid phases staggers.First
Stock liquid phase flows to 3 o ' clock orientation in 9 o ' clock orientation of ground floor tower tray, and second burst of liquid phase is in 6 o ' clock orientation of second layer tower tray
Flow to 12 o ' clock orientation.React in the structure of tower tray, tray structure such as Fig. 2 of the first six layer of plate column, Fig. 3, Fig. 4, Fig. 5, figure
6th, shown in Fig. 7.
On plate column, as shown in figure 8, l represents liquid phase, g represents gas phase to gas-liquid mass transfer.On tower tray press liquid phase flow direction according to
Secondary be divided into liquid receiving area, exchange area, descending liquid area, represented with l j-k, j represents that liquid phase is classified, first burst of liquid phase is 1, second burst of liquid phase
For 2；K represents region, and wherein descending liquid area 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, flows through the
After the exchange area l1-3 contact mass transfer of one layer of tower tray, cross the downspout that downflow weir enters ground floor tower tray, reach third layer tower
The liquid receiving area l1-2 of disk；After then passing through the exchange area l1-3 contact mass transfer of third layer tower tray, cross downflow weir and enter third layer
The downspout of tower tray, the liquid receiving area l1-2 ... of arrival layer 5 tower tray so sequentially passes through each odd-level tower tray and finally flows into tower
Kettle.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
Downflow weir enters the downspout of second layer tower tray, reaches the liquid receiving area l2-2 of the 4th layer of tower tray；Then pass through the 4th layer of tower tray
After the l2-3 contact mass transfer of exchange area, cross the downspout that downflow weir enters the 4th layer of tower tray, reach the liquid receiving area of layer 6 tower tray
L2-2 ... so sequentially passes through each even level tower tray and finally imports tower reactor, goes out tower with l1 after mixing.
Embodiment 2
A kind of be applied to the plate column that biliquid replaces flow pattern mass transfer method, the top section structure of plate column as shown in figure 9,
Including tower shell 1, in tower casing body, it is provided with multilayer tower tray 2, tower tray 2 is provided with downflow weir 3, seal pot 4.It is provided with fall up and down between tower tray
Liquid pipe 5, tower tray is divided into liquid receiving area, exchange area, descending liquid area by liquid phase flow direction.Tower shell positioned at tower tray ground floor
It is provided with the first inlet 61, the first inlet 61 is directed at the seal pot 4 on ground floor tower tray.Tower casing positioned at the tower tray second layer
Body is provided with the second inlet 62, and the second inlet 62 is directed at the seal pot 4 on second layer tower tray.On the tower shell of tower tray last layer
It is provided with gas phase air inlet.
Tower tray has three Floor 12s, and every four layers of the tower tray in tower casing body is a unit group.Ground floor in one unit group
Tower tray and the 4th layer of tower tray constitute the first switch room exchanging for first strand of liquid and gas mass transfer, second layer tower tray and the 3rd
Layer tower tray constitutes the second switch room exchanging for second strand of liquid and gas mass transfer.
Gas phase successively passes through tower tray and liquid layer thereon until tower top goes out tower from bottom of towe；Liquid phase is divided into two strands, respectively from tower
Toward dirty, two bursts of liquid phases are alternately contacted with the gas phase rising on tower tray, two bursts of liquid phases for top ground floor tower tray and second layer tower tray
Between in plate column mass transport process cocurrent do not contact.Two strands of liquid and gas replace contact, every two-layer tower tray alternately once.
The downspout that liquid phase on n-th (n is odd number) layer tower tray is passed through in plate column passes through two-layer tower tray, reaches the n-th+3 layers tower tray
Seal pot；Liquid phase on (n+1)th layer of tower tray passes through the downspout in plate column, reaches the seal pot of the n-th+2 layers tower tray.First strand
The flow ratio of liquid phase and second burst of liquid phase is 0.2.
The tray structure sectional view of Figure 10, Figure 11, Figure 12, Figure 13, Figure 14, Figure 15 the first six layer of plate column.On plate column, gas
As shown in figure 16, l represents liquid phase to liquid mass transfer, and g represents gas phase.It is divided into liquid receiving area, exchange by liquid phase flow direction on tower tray
Area, descending liquid area, are represented with l j-k, and j represents that liquid phase is classified, and first burst of liquid phase is 1, and second burst of liquid phase is 2；K represents region, its
Middle descending liquid area is 1, and liquid receiving area is 2, and exchange area is 3.
Liquid phase is divided into two gangs of l1, l2 by flow ratio for 1:5.Wherein l1 enters the liquid receiving area of tower top ground floor tower tray
L1-2, 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
Reach the liquid receiving area l1-2 of the 4th layer of tower tray；After then passing through the exchange area l1-3 contact mass transfer of the 4th layer of tower tray, cross downflow weir
Enter the downspout of the 4th layer of tower tray, the liquid receiving area l1-2 ... reaching layer 5 tower tray finally flows into tower reactor by that analogy.l2
Enter 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, cross overflow
Weir enters the downspout of second layer tower tray, reaches the liquid receiving area l2-2 of third layer tower tray；Then pass through the exchange of third layer tower tray
After area's l2-3 contact mass transfer, cross the downspout that downflow weir enters third layer tower tray, reach the liquid receiving area l2- of layer 6 tower tray
2 ... finally import tower reactor by that analogy, go out tower with l1 after mixing.
Embodiment 3
It is 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. a kind of biliquid replaces flow pattern mass transfer method, and the gas phase of material and liquid phase counter current contacting in plate column are realized mass transfer and divided
From it is characterised in that gas phase successively passes through tower tray and liquid layer thereon until tower top goes out tower from bottom of towe；Liquid phase is divided into two strands, point
Not from tower top ground floor tower tray and second layer tower tray toward dirty, two bursts of liquid phases are alternately contacted with the gas phase rising on tower tray, and two
Between stock liquid phase, in plate column mass transport process, cocurrent does not contact.
2. a kind of biliquid according to claim 1 replaces flow pattern mass transfer method it is characterised in that two strands of liquid and gas are handed over
For contact, alternately once, the downspout that the liquid phase on m layer tower tray is passed through in plate column passes through next layer of tower to every alternating floor tower tray
Disk, reaches the seal pot of m+2 layer tower tray.
3. a kind of biliquid according to claim 1 replaces flow pattern mass transfer method it is characterised in that two strands of liquid and gas are handed over
For contact, every two-layer tower tray alternately once, the downspout that the liquid phase on n-th layer tower tray is passed through in plate column passes through two-layer tower
Disk, reaches the seal pot of the n-th+3 layers tower tray；Liquid phase on (n+1)th layer of tower tray passes through the downspout in plate column, reaches n-th+2
The seal pot of layer tower tray；Wherein, n is odd number.
4. a kind of biliquid according to Claims 2 or 3 replace flow pattern mass transfer method it is characterised in that first burst of liquid phase and
The flow ratio of 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 characterised in that first burst of liquid phase and second
The flow ratio of stock liquid phase is 1.
6. a kind of be applied to biliquid as claimed in claim 2 replace flow pattern mass transfer method plate column, including tower shell (1),
It is provided with some tower trays (2), tower tray (2) is provided with downflow weir (3), seal pot (4), is provided with downspout between upper and lower tower tray in tower casing body
(5), tower tray is divided into liquid receiving area, exchange area, descending liquid area it is characterised in that being located at tower tray first by liquid phase flow direction
The tower shell of layer is provided with the first inlet (61), is provided with the second inlet (62), tower positioned at the tower shell of the tower tray second layer
The tower shell of disk last layer is provided with gas phase air inlet, and the downspout on m layer tower tray connects the seal pot of m+2 layer tower tray, phase
The dividing plate of two bursts of liquid phases of setting isolation between adjacent tower tray.
7. a kind of biliquid that is applied to according to claim 6 replaces the plate column of flow pattern mass transfer method it is characterised in that institute
State at least four layers of tower tray, the tower tray in tower casing body every four layers be a unit group, the ground floor tower tray in a unit group and
Third layer tower tray constitutes the first switch room, second layer tower tray and the 4th layer of tower tray exchanging for first strand of liquid and gas mass transfer
Constitute the second switch room exchanging for second strand of liquid and gas mass transfer, arrange described between the first switch room and the second switch room
Dividing plate.
8. a kind of biliquid that is applied to according to claim 6 replaces the plate column of flow pattern mass transfer method it is characterised in that the
One inlet (61) and the second inlet (62) are separated by 90 degree along plate column periphery and are staggeredly arranged.
9. a kind of be applied to biliquid as claimed in claim 3 replace flow pattern mass transfer method plate column, including tower shell, tower casing
It is provided with some tower trays in vivo, tower tray is provided with downflow weir, seal pot, is provided with downspout between upper and lower tower tray, tower tray is pressed liquid phase stream
Dynamic direction is divided into liquid receiving area, exchange area, descending liquid area it is characterised in that the tower shell being located at tower tray ground floor is provided with the
One inlet, is provided with the second inlet positioned at the tower shell of the tower tray second layer, and the tower shell of tower tray last layer is provided with gas phase and enters
Gas port, downspout on n-th layer tower tray connects the seal pot of the n-th+3 layers tower tray, downspout connection on (n+1)th layer of tower tray n-th+
The seal pot of 2 layers of tower tray；Wherein, n is odd number.
10. according to claim 9 a kind of be applied to biliquid replace flow pattern mass transfer method plate column it is characterised in that
At least four layers of described tower tray, every four layers of the tower tray in tower casing body is a unit group, the ground floor tower tray in a unit group
Constitute the first switch room, second layer tower tray and the third layer tower exchanging for first strand of liquid and gas mass transfer with the 4th layer of tower tray
Disk constitutes the second switch room exchanging for second strand of liquid and gas mass transfer.
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 |
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| Publication Number | Publication Date |
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| CN104815531A CN104815531A (en) | 2015-08-05 |
| CN104815531B true CN104815531B (en) | 2017-01-18 |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| 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 |
Family Cites Families (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB1432944A (en) * | 1972-05-09 | 1976-04-22 | Hydronyl Ltd | Distillation or absorption columns |
| DE3268060D1 (en) * | 1981-01-22 | 1986-02-06 | Distillation Technology Limite | Mass transfer apparatus |
| JPS5995903A (en) * | 1982-11-24 | 1984-06-02 | Nippon Kayaku Co Ltd | Baffle tray column |
| US5213719A (en) * | 1992-09-28 | 1993-05-25 | Chuang Karl T | Gas-liquid contacting 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 |
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