CN101036840A - Full effective tray with separating phase transformation and small plate distance rectifying tower - Google Patents
Full effective tray with separating phase transformation and small plate distance rectifying tower Download PDFInfo
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- CN101036840A CN101036840A CN 200610067755 CN200610067755A CN101036840A CN 101036840 A CN101036840 A CN 101036840A CN 200610067755 CN200610067755 CN 200610067755 CN 200610067755 A CN200610067755 A CN 200610067755A CN 101036840 A CN101036840 A CN 101036840A
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Abstract
An equilibrium segregation distillation full-effective plate and a small-plate-distance rectification tower is a innovation for tower, especially plate, which is aimed to solve the problems of low plate efficiency, a large number of plates, long space distance, etc. The invention employs liquid-state polycomponent balancing separation manner that the gas phase is condensed and the liquid phase is distilled simultaneously in indirect heat transfer process, instead of the prior mass transfer manner that gas-liquid equilibrium will not be achieved in process of direct contact of gas and liquid. The rectification process of the full-tower is analogous to that of a multiple effect evaporator, wherein heat exchange is carried out between condensation and evaporation. The invention has the advantages of high plate efficiency, a few number of plates, short plate distance, and low tower height.
Description
Affiliated technical field
The invention relates to the innovation of plate column, especially tower plate structure in the vapour-liquid mass equipment of Chemical Manufacture.
Background technology
Rectifying column is to carry out the most frequently used equipment that fluid multi-component separates in the various Chemical Manufacture flow processs, rectifying column is divided into plate column and packed tower, plate column uses more, the core component of plate column is a column plate, the column plate that various ways such as bubble-cap, float valve, sieve plate are arranged, existing column plate contacts closely by making the vapour-liquid two-phase, and vapour phase is partly vaporized by partial liquefaction while liquid phase in the contact, reaches the purpose of mass transfer.Can not reach like this mass transfer balance, plate efficiency always less than 1 (king's arrow, the chemical industry dictionary, Chemical Industry Press, 200 year August the 4th edition, p897).
The structure of existing column plate, vapour phase is passed plate hole and is passed liquid phase again, and this just brings a series of unfavorable phenomenons such as " liquid floodings " that is full of liquid-vapor mixture between liquid foam entrainment in plate hole leakage, the vapour phase even plate, bigger distance between plates must be arranged for this reason.
Summary of the invention
The objective of the invention is, problem such as plate efficiency low, distance between plates big many for the plate number that solves rectifying column as mentioned above.
The total design of the present invention is: abandon present vapour-liquid two-phase in direct contact vapour phase by partial liquefaction simultaneously liquid phase by the mass transfer mode of partial liquefaction, adopt vapour-liquid two isolated, do not contact mutually, in indirect heat transfer vapour phase be balanced fractional condensation simultaneously liquid phase be balanced the mode of distillation.
Left figure is t-X, t-Y figure in the accompanying drawing 1, (t temperature, X liquid phase are formed, Y vapour phase form), can represent the principles such as concrete heat exchange, phase transformation, motion mode of vapour, liquid phase in conjunction with right figure.Vapour phase V below the n+1 piece plate
(n+1)With the liquid phase L above the n+1 piece plate
(n+1), mutually reverse flow and conduct heat by n+1 piece plate.Vapour phase V
(n+1)Flow in (right figure) from right to left, temperature is reduced to d point (left figure), liquid phase L from initial c point
(n+1)Flow from left to right, temperature rises to a point from initial e point.
By conducting heat V
(n+1), L
(n+1)Respectively by fractional condensation and distillation.Vapour phase V
(n+1)(c point) obtains condensate liquid Lv through fractional condensation (dotted line)
(n+1)(a point) and steam Vv
(n+1)(d point), liquid phase L
(n+1)(e point) obtains raffinate L through distillation (solid line)
L (n+1)(a point) and steam V
L (n+1)(d point).Steam Vv
(n+1)With V
L (n+1)Merge and rise under the n piece plate, as V
(n)By fractional condensation; Lv
(n+1)With L
L (n+1)Merging compiles, and flow to downwards on the n+2 piece plate, as the liquid phase L on the n+2 piece plate
(n+2)(a point).
L
(n+2)On n+2 piece plate, be heated distillation again, obtain raffinate L
L (n+2)(b point) and steam V
L (n+2)(c point), raffinate L
L (n+2)Flow to downwards on the n+3 piece plate; Steam V
L (n+2)With the vapour phase V under the n+2 piece plate
(n+2)The steam Vv that fractional condensation is last
(n+2)Merge and rise under the n+1 piece plate, as vapour phase V
(n+1)Carry out the heat release fractional condensation, obtain condensate liquid Lv
(n+1)(a point) and steam Vv
(n+1)(d point), like this, the liquid phase L that a is ordered
(n+2)On n+2 piece plate, be separated into the vapour phase that liquid phase that b orders and d are ordered, reached the highest separating effect.
Compare the vapor phase movement mode difference that the liquid phase stream flowing mode that is distilled on the column plate of the present invention is constant, distillation produces with existing column plate.Be distilled liquid phase and remain, flow through each column plate from top to bottom successively by overflow mechanism; After the vapour phase cooling fractional condensation that distillation produces, obtain the higher steam of light component concentration and rise to below the last layer column plate, the liquid phase that fractional condensation produces is returned column plate and is continued distillation.
Whole process is the spitting image of a multi-effect evaporator, heat exchange mutually between fractional condensation and distillation two processes.
Be a kind of concrete technical scheme (accompanying drawing 2) that realizes the total design of the present invention below.
The principle structure of column plate is as follows.Plate hole on the existing rectifying column column plate of all kinds is removed as heat exchanger plates 1, the carrying liquid phase, 1 is provided with vapor uptake 2, and the mouth of pipe exceeds liquid level, and about 30 millimeters add a liquid collecting plate 3 under the heat exchanger plates 1, compile lime set.Heat exchanger plates, liquid collecting plate are formed one deck column plate jointly.Be fractional condensation chamber 4 between 1 below and 3 tops; Be distillery 5 between 1 top and 3 belows.The steam that produces on the heat exchanger plates 1 enters fractional condensation chamber 4 (dotted arrow) by fractional condensation from distillery 5 through liquid collecting plates 3 and passage 7 between the downspout 9, the liquid of fractional condensation generation also be flow to heat exchanger plates 4 (dash-dot arrows), fractional condensation from liquid collecting plate 3 downward folding corbel back slabs 6 by passage 7 residual steam by vapor uptake 2, enter fractional condensation chamber, upper strata (dotted arrow) by passage 7 again.
Keep the downspout 9 and the downflow weir 8 of existing column plate, make liquid phase flow through (solid arrow) from each heat exchanger plates 4 successively from top to bottom.
Above column plate can directly be used in existing essence and stay on the tower, raises the efficiency, reduces the plate number.
This column plate more can be designed the rectifying column that tower height reduces at double.Because rectifying column of the present invention does not have unfavorable phenomenons such as plate hole leakage, liquid foam entrainment, can be reduced to distance between plates very little.The general height in fractional condensation chamber between the liquid collecting plate of heat exchanger plates and its below is about the 20-80 millimeter, as long as guarantee that its vapour phase has enough time of staying, is got final product by suitable fractional condensation.About 30 millimeters of distillery height (distance between plates just) between the heat exchanger plates of liquid collecting plate and its below is as long as guarantee the diffuse normal of steam.And existing distance between plates be the 300-800 millimeter (Shanghai Medicines Design inst., State Pharmaceutical Administration, the chemical process design manual, Chemical Industry Press, 1996 the 2nd edition, p4-452 to p4-458), new tower has been reduced to below 1/10th of existing distance between plates.If existing rectifying column adopts the distance between plates of 20-80 millimeter, is not imaginabale.
Except distance between plates was little, the technical characterictic of tower of the present invention also had: must be existing normal distance between plates 300-800 millimeter (to hold a large amount of materials of pouring into suddenly in the tower) between two column plates of charging aperture; The steam that first heat exchanger plates in cat head place produces carries out fractional condensation by cooling water, and lime set is as the liquid phase in first heat exchange, and the fractional condensation residual steam is coagulated by the final set device more entirely as overhead product.
Column plate of the present invention has been compared tangible advantage and good effect with prior art.Two of existing column plate vapour-liquids directly contact are carried out mass transfer, can not reach alternate component balanced of vapour-liquid two because the alternate mass transfer force of vapour-liquid two must be greater than zero, in case and this motive force of balance equals zero; The motive force of column plate fractional condensation of the present invention and distillation is exactly the heat exchanger plates temperature difference up and down and since be the vapour-liquid contrary to flowing, kept certain temperature difference on the full plate, motive force greater than zero condition under, realized the balance of evaporation and fractional condensation, therefore, plate efficiency can reach 1.
Rectifying column of the present invention, the plate efficiency height, the plate number is few, distance between plates is little, tower height greatly reduces.
Specific embodiment
The present invention is further described below in conjunction with drawings and Examples (a plurality of embodiment can be arranged).
Every layer of column plate is exactly a tower joint (solid line of accompanying drawing 3) on the whole, and the tower joint mainly is made up of vertical post shell 10, liquid collecting plate 3 and heat exchanger plates 1.Heat exchanger plates 1 is thin (about 0.5 millimeter as far as possible, heat transfer block) thin plate, the plate face strikes out one group of trend perpendicular to " v " connected in star of downflow weir (a bit as asbestos shingle, just on big, the plate of distance planar section is arranged between the groove), and groove plays a part to strengthen that liquid phase flows, assembles condensate liquid under the plate on weight capacity, the guided plate.For making on the heat exchanger plates liquid layer thickness even, heat exchanger plates will hang down 5 millimeter (it is fixed to look the liquid phase viscosity), slope of the formation of streamwise in downflow weir one side.Liquid collecting plate can horizontal positioned, also can be convenient to condensate flow with the heat exchanger plates parallel oblique, and liquid collecting plate bends out (or being welded with) rectangular slab 6 under downspout one side direction, and the guiding lime set moves down from passage 7.Post shell 10 belows are welded with the circular band steel of twice, form circular packing groove 12, and the packing groove of upper strata Ta Jie (solid line of accompanying drawing 3) inserts for the top of the post shell of lower floor's tower joint (double dot dash line of accompanying drawing 3).All plug surfaces will be processed concordant, and under the effect of uniform axial screw lacing wire (not shown) and slot packing, each tower joint forms sealed whole outside wall.
More than being the description of tower plate structure, is the course of work of full tower below.The operation principle front of every block of column plate has been introduced clear, and what present embodiment need stress is that cat head and tower basic skill or training make process (accompanying drawing 4,5).
Liquid phase on the heat exchanger plates of ground floor column plate is evaporated the steam V that is produced
L1With remaining steam V after the fractional condensation of the fractional condensation chamber of this plate below
V2Merge to rise, with condensed water 10 heat exchange in the dephlegmator of top of the tower 11 and by fractional condensation, the liquid phase L that obtains
V1As phegma L
1, the remaining steam V of fractional condensation
V1Steam state product V as cat head
D, be sent to the outer final set device (accompanying drawing 4) of tower.
The tower bottom, secondary water steam 12 feeds reboiler 15, liquid phase in heating and the vaporization part device, the steam 14 that produces flows into the fractional condensation chamber 4 of tower bottommost, by a bottom heat exchanger plates heat release and by fractional condensation, lime set is as a part that is back to reboiler liquid 13, and residual steam enters fractional condensation chamber, upper strata 4 by vapor uptake 2.The last liquid phase of a bottom heat exchanger plates is also entered this fractional condensation chamber by the steam that the part evaporation produces by passage 7, evaporates remaining liquid phase as the another part that is back to reboiler liquid 13.Liquid is exactly tower bottom product 16 (accompanying drawing 5) by the last raffinate in part vaporization back in the reboiler.
Claims (5)
1. the tower tray device of a rectifying column is characterized in that, gas-liquid two-phase gas phase in indirect heat transfer is balanced fractional condensation while liquid phase by the equilibrium vaporization of partly vaporizing.
2. according to the tower tray device of claim 1, be provided with downspout and downflow weir, it is characterized in that, every layer of column plate is made up of the heat exchanger plates and a clotting liquid plate of a no plate hole, form distillery and fractional condensation chamber, and be provided with the gas-liquid phase passage that connects two Room, also be provided with vapor uptake.
3. rectifying column has adopted the column plate of claim 2, it is characterized in that the charging aperture place clear distance between two plates up and down is the 300-800 millimeter, and other is located this distance and is the 20-80 millimeter, and cat head has segregator and final set device.
4. according to the rectifying column of claim 3, it is characterized in that, full tower comprises several tower joints, and tower joint below is welded with the packing groove of a circle, is filled with filler in the groove, full tower has the axial screw lacing wire, each tower joint comprises post shell, liquid collecting plate and heat exchanger plates, is welded with two block-shaped differences rectangular slab parallel to each other in the post shell, and segregator is positioned at tower, cat head has the material steam outlet, and the outlet of steam state material inlet and liquid material is arranged at the bottom of the tower.
5. according to the rectifying column of claim 3, it is characterized in that, full tower comprises several tower joints, tower joint below is welded with the packing groove of a circle, be filled with filler in the groove, full tower has the axial screw lacing wire, and each tower joint comprises post shell, liquid collecting plate and heat exchanger plates, be welded with two block-shaped differences rectangular slab parallel to each other in the post shell, segregator is positioned at outside the tower.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2006100677559A CN100546688C (en) | 2006-03-16 | 2006-03-16 | The vapour-liquid separating phase transformation is imitated column plate and platelet entirely apart from rectifying column |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2006100677559A CN100546688C (en) | 2006-03-16 | 2006-03-16 | The vapour-liquid separating phase transformation is imitated column plate and platelet entirely apart from rectifying column |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101036840A true CN101036840A (en) | 2007-09-19 |
| CN100546688C CN100546688C (en) | 2009-10-07 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB2006100677559A Expired - Fee Related CN100546688C (en) | 2006-03-16 | 2006-03-16 | The vapour-liquid separating phase transformation is imitated column plate and platelet entirely apart from rectifying column |
Country Status (1)
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|---|---|
| CN (1) | CN100546688C (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102920963A (en) * | 2012-08-29 | 2013-02-13 | 华润三九（黄石）药业有限公司 | Large-scale preparation process of acute and chronic pharyngolaryngitis medicines |
| CN103678903A (en) * | 2013-12-06 | 2014-03-26 | 杭州电子科技大学 | Dynamic rectifying tower modeling method |
| CN105241181A (en) * | 2015-09-28 | 2016-01-13 | 苏州制氧机股份有限公司 | Lower tower for air separation device |
-
2006
- 2006-03-16 CN CNB2006100677559A patent/CN100546688C/en not_active Expired - Fee Related
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102920963A (en) * | 2012-08-29 | 2013-02-13 | 华润三九（黄石）药业有限公司 | Large-scale preparation process of acute and chronic pharyngolaryngitis medicines |
| CN102920963B (en) * | 2012-08-29 | 2016-02-24 | 华润三九（黄石）药业有限公司 | The preparation technology of acute and chronic pharyngitis medicine scale |
| CN103678903A (en) * | 2013-12-06 | 2014-03-26 | 杭州电子科技大学 | Dynamic rectifying tower modeling method |
| CN105241181A (en) * | 2015-09-28 | 2016-01-13 | 苏州制氧机股份有限公司 | Lower tower for air separation device |
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| Publication number | Publication date |
|---|---|
| CN100546688C (en) | 2009-10-07 |
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| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| EE01 | Entry into force of recordation of patent licensing contract |
Assignee: Huangshi 39 Pharmaceutical Co., Ltd. Assignor: Taiyuan University of Technology Contract record no.: 2010420000129 Denomination of invention: Full effective tray with separating phase transformation and small plate distance rectifying tower Granted publication date: 20091007 License type: Exclusive License Open date: 20070919 Record date: 20100825 |
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| C17 | Cessation of patent right | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20091007 Termination date: 20120316 |