CN1220179A - Vapour-liquid parallel flow jet contact non-backmixing double-layer tower tray device - Google Patents
Vapour-liquid parallel flow jet contact non-backmixing double-layer tower tray device Download PDFInfo
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- CN1220179A CN1220179A CN 98124512 CN98124512A CN1220179A CN 1220179 A CN1220179 A CN 1220179A CN 98124512 CN98124512 CN 98124512 CN 98124512 A CN98124512 A CN 98124512A CN 1220179 A CN1220179 A CN 1220179A
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Abstract
The present invention discloses a vapor-liquid parallel-flow jet contact non-backmixing double-layer tower plate equipment. It is mainly characterized by that said plate body consists of two layers of upper layer plate and lower layer plate, in which the lower plate is equipped with through hole, and the upper plate is equipped with lift pipe which is passed through the upper plate and fixed, and there is a gap between the lower end of the lift pipe and lower plate surface, and the upper end of said lift pipe is higher than the upper plate surface, and is equipped with cap cover or stuffing plate liquid-stopping unit body, and the same-side segmental zone of the upper and lower plates is closed by down-flow apron. Said invention implements the vapor-liquid parallel-flow jet contact in lift pipe, not only can prevent the backmixing of liquid, but also raise the plate efficiency and tower efficiency, and possesses large operation elasticity.
Description
The present invention relates to a kind of vapour-liquid and stream and spray the no back-mixing two-layer equation tower tray device of contact.It belongs to the innovation of destilling tower tower tray device.
Plate column is widely used in the separation process in the fields such as chemical industry.Its weak point mainly shows as follows: one, on the column plate vapour-liquid two-phase with bubbling form (as common sieve tray, valve plate, calotte column plate etc.) or with after liquid droplets form (as jet tray, the vertical sieve tray etc.) contact mass transfer, vapour phase enters the last layer column plate at once, and the liquid phase at diverse location place can not be left at once and enters down one deck column plate on the column plate, but flow with the distribution in liquid phase flow field on the column plate, and constantly mix with its liquid on every side, so-called back-mixing promptly takes place, and has reduced the mass transfer force between the vapour-liquid two-phase; Two, ubiquity the liquid flow non-uniform phenomenon on the large-scale column plate, and as channel, short circuit, backflow etc., channel and short circuit will reduce the chance of liquid and vapour phase generation mass transfer and reduce plate effect and tower effect; Backflow mostly occurs in arch area, it can cause liquid in the recirculating zone very fast with pass this regional vapour phase near equilibrium state, cause and pass this regional vapour phase concentration and change hardly and just leave column plate, plate is imitated reduces; Three, on large-scale column plate because flow path is long, and liquid layer thickness is inhomogeneous, easily causing on the plate mass transfer force and vapour phase to pass speed has than big-difference, so also can cause plate to imitate and the reduction of tower effect.
In order to overcome the particularly above-mentioned weak point of large-scale plate column of existing plate column, the object of the present invention is to provide a kind of vapour-liquid and stream to spray the no back-mixing two-layer equation tower tray device of contact.With this plate tower or absorption tower of installing formation, there is not air-teturning mixed phenomenon in liquid during operation, and plate is imitated and imitated high with tower.
For achieving the above object, the present invention is realized by following proposal.By plate body, downspout, riser, block vapour-liquid and the stream that the liquid cell cube constituted and spray the no back-mixing two-layer equation tower tray device of contact, it is characterized in that plate body is made of two-layer up and down, wherein lower floor's plate body edge is most of is connected with the tower wall, leave the arch area opening, offer through hole on the plate; The last layer plate body is about one to offer the plate of arch area, the arch area size is identical with the lower plate arch area, other edges of plate also are connected with the tower wall, and to the downward-sloping placement of downspout direction level, this plate wear diameter greater than lower plate through-hole diameter, radical equate with lower plate through hole number, the riser of center line and lower plate through hole central lines, riser lower port and lower face have spacing, and upper port is higher than top plate plate face, and the upper orifice of each riser is provided with and blocks the liquid cell cube; Top plate and lower plywood homonymy arch area are shut by the baffle plate of downspout; For giving full play to excellent properties of the present invention, its feature also is, the through hole that lower plywood is offered can be circular hole or for elliptical aperture or for square hole or be oblong aperture; The downward inclination alpha of top plate level=0～15 °; The riser that is located on the plate body of upper strata can be pipe or for elliptical tube or for square tube or for the rectangle pipe, can offer slot on the upper and lower port wall of pipe, and aperture can be offered in the top of tube wall the first half; Blocking the liquid cell cube can be calotte or is the ripple packing dish of silk screen or plate system. can offer aperture on the calotte, the calotte external profile diameter is more than or equal to the riser caliber, and leave the slit with the pipe upper end, the packing box diameter is fixed on the riser upper end more than or equal to riser caliber and contact.
The destilling tower joint schematic diagram of Fig. 1 for constituting by the present invention.Fig. 2 is an A-A schematic diagram among Fig. 1.Wherein 1 is the tower wall, and 2 are following (end) laminate body, and 3 is the upper strata plate body, and 4 is riser, and 5 are calotte (blocking the liquid cell cube), and 6 is the baffle plate of downspout.
Below in conjunction with accompanying drawing the present invention is described in detail.Lower floor of the present invention plate body (2) is similar with existing sieve tray, and it is except the liquid mouth falls in arch area, and other outer rims of plate are connected with tower wall or tower circle by welding or screw, and the size of the through hole of offering on it and layout need design to be determined.Upper strata plate body (3) is shaped on the plate of arch area about being, it also is to be connected with tower wall or tower circle by welding or screw, and two-ply homonymy arch area opening is shut by the baffle plate (6) of downspout up and down.The main employing of riser on the top plate (4) is welded to connect, the size of riser diameter, the lower port height apart from the distance of lower plywood, upper port apart from top plate plate face etc. all is the key factor of decision vapour-liquid contact condition quality, and these all need accurate Calculation to determine.Calotte (5) has the interception liquid effects for blocking the liquid cell cube, can offer aperture on it, and the diameter of calotte outer rim reaches and the structural parameters such as distance of the mouth of pipe are the key factors of decision plate pressure drop and entrainment; Adopt packing box to replace calotte if block the liquid cell cube, the height of packing box so, the model of filler then is an important parameter.
The process that realizes vapour-liquid mass is: liquid is by the dirty interlayer that enters this layer column plate of the downspout of last layer doubling plate, enter riser by the slit between riser bottom and the lower plywood, because the vapour phase that rises has enough vapour speed, liquid that can not is dirty by through hole, but under the effect of high velocity air, move upward with membranaceous and drop form, in this process, realized the mass transfer between the vapour-liquid two-phase, after liquid-vapor mixture flows out riser by calotte or packing box, liquid drops on the plate body of upper strata, and by flowing under this layer downspout on the double-deck column plate of next layer, gas then rises and enters the double-deck column plate of last layer.Take a broad view of said process, the mass transfer of vapour-liquid two-phase mainly carries out in riser He in the calotte with the liquid droplets form, if blocking the liquid cell cube is packing box, then the mass transfer of vapour-liquid two-phase is the liquid droplets form in riser, is the liquid film form in packing box.On same block of column plate, the mass transfer of vapour-liquid two-phase is disposable to liquid, therefore can stop the back-mixing of liquid.
Owing to stopped the back-mixing of liquid, make that the vapour-liquid two-phase is remaining a higher mass transfer force on the monoblock column plate; Owing to the liquid lifting capacity of calotte on the diverse location on the column plate is basic identical, so can not exist because the plate efficiency decline problem that factors such as channel, short circuit, backflow cause; Because design feature of the present invention, so do not have diverse location place on the column plate that causes because of liquid flow, the uneven distribution of each concentration of component of liquid phase and because the liquid layer thickness difference causes vapour phase to pass the uneven distribution of speed.Therefore, adopt the present invention can improve plate efficiency and column efficiency greatly.Adopting double-deck another one advantage is to improve the operating flexibility of tower.
The general plate column structure of the present invention is complicated a little, but its manufacturing still easily, is easy to grasp.
Claims (5)
1. vapour-liquid and stream spray the no back-mixing two-layer equation tower tray device of contact, mainly by plate body, downspout, riser, block the liquid cell cube and constituted, it is characterized in that, plate body is made of two-layer up and down, wherein big of lower plywood edge is connected with the tower wall, leaves the arch area opening, offers through hole on the plate face; The last layer plate is a plate of offering arch area about one, the arch area size is identical with the lower plate arch area, other edge of plate also is connected with the tower wall, and to the downward-sloping placement of downspout direction level, this plate be equipped with diameter greater than lower plate through-hole diameter, radical equate with lower plate through hole number, the riser of center line and through hole central lines, riser lower port and lower face have spacing, and upper port is higher than top plate plate face, and each riser upper orifice is provided with and blocks the liquid cell cube; Top plate and lower plywood homonymy arch area are shut by the liquid barrier of downspout.
2. spray the no back-mixing two-layer equation tower tray device of contact by said vapour-liquid of claim 1 and stream, it is characterized in that the through hole that lower plywood is offered can be circular hole, or be elliptical aperture, or be square hole, or be oblong aperture.
3. spray the no back-mixing two-layer equation tower tray device of contact by said vapour-liquid of claim 1 and stream, it is characterized in that, dip down oblique angle α=1～15 ° of top plate level.
4. spray the no back-mixing two-layer equation tower tray device of contact by said vapour-liquid of claim 1 and stream, it is characterized in that, be located in the riser on the top plate, can be pipe, or be elliptical tube, or be square tube, or be the rectangle pipe, offer slot on the wall of two-port up and down of pipe, aperture can be offered in the top of tube wall the first half.
5. spray the no back-mixing two-layer equation tower tray device of contact by said vapour-liquid of claim 1 and stream, it is characterized in that, block the liquid cell cube and can be calotte, or be the ripple packing dish of silk screen or plate, offer aperture on the calotte, edge diameter is equal to or greater than the lifting caliber, and leaves the slit with the pipe upper end, and the packing box diameter is fixed on the riser upper end more than or equal to riser caliber and contact.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN98124512A CN1061897C (en) | 1998-11-10 | 1998-11-10 | Vapour-liquid parallel flow jet contact non-backmixing double-layer tower tray device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN98124512A CN1061897C (en) | 1998-11-10 | 1998-11-10 | Vapour-liquid parallel flow jet contact non-backmixing double-layer tower tray device |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1220179A true CN1220179A (en) | 1999-06-23 |
| CN1061897C CN1061897C (en) | 2001-02-14 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN98124512A Expired - Fee Related CN1061897C (en) | 1998-11-10 | 1998-11-10 | Vapour-liquid parallel flow jet contact non-backmixing double-layer tower tray device |
Country Status (1)
| Country | Link |
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| CN (1) | CN1061897C (en) |
Cited By (16)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100428976C (en) * | 2005-12-06 | 2008-10-29 | 中国石油天然气集团公司 | Vapour-liquid mass transfering method without amplifying effect |
| CN100428975C (en) * | 2005-12-05 | 2008-10-29 | 中国石油天然气集团公司 | Efficient high-speed vapour-liquid mass transfer structure form |
| CN101507883B (en) * | 2009-02-23 | 2010-12-29 | 天津市创举科技有限公司 | Film spray no-back mixing column plate |
| CN103252205A (en) * | 2013-05-14 | 2013-08-21 | 河北工业大学 | Full-countercurrent mass transfer unit and tower plate with unit |
| CN103463828A (en) * | 2013-09-05 | 2013-12-25 | 中国海洋石油总公司 | Vertical film blowing tower plate |
| CN103949079A (en) * | 2014-04-08 | 2014-07-30 | 天津大学 | Catalytic distillation column tray |
| CN104888486A (en) * | 2014-03-06 | 2015-09-09 | 朱莫惠 | Rectification tower and rectification method |
| CN105413222A (en) * | 2015-12-29 | 2016-03-23 | 天津市创举科技有限公司 | Dual layer equal effect tower plate |
| CN108404440A (en) * | 2018-03-25 | 2018-08-17 | 杭州众盛新科技有限公司 | Ellipse head sieve pore cap plate destilling tower |
| CN108452641A (en) * | 2018-03-29 | 2018-08-28 | 杭州众盛新科技有限公司 | Ellipse head sieve pore cap plate tower |
| CN108525471A (en) * | 2018-03-29 | 2018-09-14 | 杭州众盛新科技有限公司 | The tower made of oval ripple sieve tray |
| CN108619863A (en) * | 2018-03-29 | 2018-10-09 | 杭州众盛新科技有限公司 | The tower made of ellipse head sieve pore cap plate |
| CN108745268A (en) * | 2018-02-06 | 2018-11-06 | 杭州众盛新科技有限公司 | A kind of ellipse head sieve pore cap plate tower tray having liquid-bearing pan |
| CN110871021A (en) * | 2018-08-30 | 2020-03-10 | 中国石油化工股份有限公司 | Gas-liquid mass transfer device |
| CN112770823A (en) * | 2018-09-28 | 2021-05-07 | 卡萨乐有限公司 | Perforated plate tower and modification method thereof |
| CN115999316A (en) * | 2021-10-21 | 2023-04-25 | 中国石油化工股份有限公司 | Absorption stabilization process and absorption desorption coupling tower thereof |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1065446C (en) * | 1996-07-09 | 2001-05-09 | 兰仁水 | Parallel jet compounding tower |
-
1998
- 1998-11-10 CN CN98124512A patent/CN1061897C/en not_active Expired - Fee Related
Cited By (19)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100428975C (en) * | 2005-12-05 | 2008-10-29 | 中国石油天然气集团公司 | Efficient high-speed vapour-liquid mass transfer structure form |
| CN100428976C (en) * | 2005-12-06 | 2008-10-29 | 中国石油天然气集团公司 | Vapour-liquid mass transfering method without amplifying effect |
| CN101507883B (en) * | 2009-02-23 | 2010-12-29 | 天津市创举科技有限公司 | Film spray no-back mixing column plate |
| CN103252205A (en) * | 2013-05-14 | 2013-08-21 | 河北工业大学 | Full-countercurrent mass transfer unit and tower plate with unit |
| CN103463828A (en) * | 2013-09-05 | 2013-12-25 | 中国海洋石油总公司 | Vertical film blowing tower plate |
| CN103463828B (en) * | 2013-09-05 | 2015-09-02 | 中国海洋石油总公司 | Vertical blown film column plate |
| CN104888486A (en) * | 2014-03-06 | 2015-09-09 | 朱莫惠 | Rectification tower and rectification method |
| CN103949079B (en) * | 2014-04-08 | 2016-02-10 | 天津大学 | A kind of catalytic distillation tower tray |
| CN103949079A (en) * | 2014-04-08 | 2014-07-30 | 天津大学 | Catalytic distillation column tray |
| CN105413222A (en) * | 2015-12-29 | 2016-03-23 | 天津市创举科技有限公司 | Dual layer equal effect tower plate |
| CN108745268A (en) * | 2018-02-06 | 2018-11-06 | 杭州众盛新科技有限公司 | A kind of ellipse head sieve pore cap plate tower tray having liquid-bearing pan |
| CN108404440A (en) * | 2018-03-25 | 2018-08-17 | 杭州众盛新科技有限公司 | Ellipse head sieve pore cap plate destilling tower |
| CN108452641A (en) * | 2018-03-29 | 2018-08-28 | 杭州众盛新科技有限公司 | Ellipse head sieve pore cap plate tower |
| CN108525471A (en) * | 2018-03-29 | 2018-09-14 | 杭州众盛新科技有限公司 | The tower made of oval ripple sieve tray |
| CN108619863A (en) * | 2018-03-29 | 2018-10-09 | 杭州众盛新科技有限公司 | The tower made of ellipse head sieve pore cap plate |
| CN110871021A (en) * | 2018-08-30 | 2020-03-10 | 中国石油化工股份有限公司 | Gas-liquid mass transfer device |
| CN110871021B (en) * | 2018-08-30 | 2022-03-08 | 中国石油化工股份有限公司 | Gas-liquid mass transfer device |
| CN112770823A (en) * | 2018-09-28 | 2021-05-07 | 卡萨乐有限公司 | Perforated plate tower and modification method thereof |
| CN115999316A (en) * | 2021-10-21 | 2023-04-25 | 中国石油化工股份有限公司 | Absorption stabilization process and absorption desorption coupling tower thereof |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1061897C (en) | 2001-02-14 |
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