CN1895715A - Catalytic rectification tower plate - Google Patents
Catalytic rectification tower plate Download PDFInfo
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- CN1895715A CN1895715A CN 200610013530 CN200610013530A CN1895715A CN 1895715 A CN1895715 A CN 1895715A CN 200610013530 CN200610013530 CN 200610013530 CN 200610013530 A CN200610013530 A CN 200610013530A CN 1895715 A CN1895715 A CN 1895715A
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- plate
- rectification tower
- riser
- catalytic rectification
- catalyst
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- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
- Feeding, Discharge, Calcimining, Fusing, And Gas-Generation Devices (AREA)
Abstract
A catalytically rectifying 3D tower plate with high space utilization rate, low pressure loss and long stay time of liquid on the surface of catalyst is composed of tower plate, gas lifting-up tubes on said tower plate, combined spray unit installed to said gas lifting-up tubes and consisting of 3D spray cap and solid catalyst, down-flow plate, and liquid collecting tray.
Description
Technical field
The present invention relates to the gas-liquid mass transfer (contact) equipment in the Chemical Engineering catalytic distillation process, is a kind of big flux, catalytic rectification tower plate efficiently specifically.
Background technology
Catalytic distillation is a kind of novel separating technology with wide application prospect.Use heterogeneous catalysis in the tower, reaction and separation process are finished in catalytic rectifying tower simultaneously, can break the restriction of chemical balance, obtain higher selectivity, and process efficiency is improved, and equipment investment and operating cost are reduced.But the degree that the length of the loadings of catalyst and liquid and catalyst surface time of contact and uniformity coefficient decision reaction is carried out on the column plate.Past normally encases catalysis or make catalyst basket with the porous material that can encase catalyst, be placed on the column plate or downspout in etc. the place flow through of liquid, but, catalytic distillation efficient, disposal ability are reduced because the loadings of the structural limitations catalyst of column plate and time and the uniformity coefficient that liquid contacts with catalyst all are restricted.
Summary of the invention
The object of the present invention is to provide a kind of big flux catalytic rectification tower plate efficiently, can overcome the shortcoming of prior art.The loadings of the height of liquid layer, catalyst can be adjusted in very big altitude range according to technological requirement on the space availability ratio height of this column plate, the column plate.Liquid on the column plate is under the effect of the gas that is risen by following one deck column plate simultaneously, and the solid catalyst of can repeatedly flowing through equably is improved the efficient of catalytic reaction, rectifying simultaneously.Advantages such as this column plate also has liquid in addition and catalyst surface time of contact is long, operating flexibility is big, plate pressure drop is low can satisfy the technological requirement of catalytic distillation well, can also improve the disposal ability of catalytic rectifying tower, reduce equipment investment.
Catalytic rectification tower plate provided by the invention mainly comprises column plate, riser, combined jet unit, down-flow plate and seal pot; Regularly arranged riser is installed on described column plate, the combined jet unit cooperate to be installed on riser, the combinations of injections unit is combined by stereo-spray calotte and solid catalyst, be on the column plate rectifying with react the main place of carrying out.
Described riser be shaped as rectangle, trapezoidal or circular; Folded angle is 45-135 ° between described riser and the column plate.Described riser height 0～400mm (0 expression riser upper end flushes with plane on the column plate), row's number in hole is 1-20.
Liquid lifting channel width is 2-50mm between the stereo-spray calotte of described combinations of injections unit and the riser, and the height of the loading catalyst of catalyst is 20～500mm between the stereo-spray calotte.Described combinations of injections unit be full tower section combination, according to the piecemeal situation of column plate by every column plate combination or single existence.
Described down-flow plate height of weir plate is 20-400mm.
Described open ratio of plate 1～20%.
Every 1-5 stereo-spray is covered with puts a draining plate.
Described stereo-spray calotte base plate is screen, porous plate or web plate, can add silk screen or filter cloth above, and silk screen filter cloth and base plate step up; Solid catalyst is placed after can directly placing and also can tying up, and the catalyst top is provided with screen, porous plate or silk screen and impingement baffle, prevents that catalyst is subjected to impact grinding and runs off.
Characteristics of the present invention are to leave the slit between calotte and the riser to promote passage as liquid, the gas that following one deck column plate rises elevates the liquid of liquid layer bottom on the column plate by this passage, filling solid catalyst between the calotte, liquid that draining plate the elevates calotte catalyst of flowing through is equably installed in the top of calotte, the liquid of flowing through behind the catalyst falls after rise on this layer column plate, can control the amount of liquid of the catalyst of flowing through by the physical dimension of control calotte, generally can be by the lifting capacity of control liquid, make the 0.5-20 of this layer column plate amount of liquid of the flowing through catalyst of doubly flowing through, on column plate, make a liquid circulation artificially.The design of arranging on column plate in the combinations of injections unit in addition, the height that can make the combinations of injections unit be between the two-layer column plate distance 90%, and the part filling solid catalyst that accounts for full tower section long-pending 80%.Therefore the space availability ratio of column plate is very high, has strengthened the renewal of catalyst surface, has prolonged the time of staying of liquid at catalyst surface, and the efficient of catalytic distillation is improved.
The present invention uses under the tray spacing condition of 450～1000mm usually.Described down-flow plate height of weir plate can be adjusted in the 20-400mm scope; Have regularly arranged rectangle, trapezoidal or circular plate hole on the described column plate, row's number in hole is 1-20; Open ratio of plate 1～20%; Described riser height 0～400mm; The form fit of described stereo-spray calotte and riser.Described solid catalyst loading height is 20～500mm.
The present invention has following advantage, the space availability ratio of column plate is very high, when tray spacing is 450～1000mm of routine, column plate supernatant layer height can be adjusted arbitrarily in the 20-400mm scope, the loading height of catalyst can be adjusted arbitrarily in 50～500mm scope, account for the long-pending part of full tower section and can be used to filling solid catalyst, to satisfy the requirement of catalytic distillation loaded catalyst and liquid and catalyst surface time of contact and uniformity coefficient up to 80%.In this height of liquid layer and catalyst packing height scope, individual layer column plate pressure falls less than 0.6KPa simultaneously, and the void tower kinetic energy factor reaches 2.0Pa
0.5More than, operating flexibility, column plate separative efficiency all are higher than common column plate.
Description of drawings
Fig. 1 is a structural representation of the present invention.
Fig. 2 is Fig. 1 vertical view.
Fig. 3 is Fig. 1 side view.
The specific embodiment
Specific embodiments of the present invention are described in detail as follows with reference to accompanying drawing:
As shown in the figure, 1 tower body, 2 down-flow plates, 3 seal pots, 4 column plates, 5 riseies, 6 combinations of injections unit, 7 fluid passages, 8 liquid promote passage, 9 solid catalysts, 10 stereo-spray calottes, 11 draining plates.Symbol H among the figure
T: be tray spacing, E: be the combinations of injections cell height, hw is the downspout height of weir plate.
The structure of catalytic rectification tower plate provided by the invention is: downspout, seal pot structure are identical with common column plate, and just the downspout height of weir plate can be according to the arts demand adjustment in the 20-400mm scope; The riser 5 of regular arrangement on column plate 4 (being trapezoidal among the figure), riser 5 highly can be adjusted as required, the form fit of stereo-spray calotte and riser.Installation stereo-spray calotte 10 matches with riser 5, leaving the space between stereo-spray calotte 10 and the riser 5 is that liquid promotes passage 8, solid catalyst 9 is housed between the calotte, leaving the space between stereo-spray calotte 10 and the column plate 4 is fluid passage 7, and draining plate 11 is installed in the top of stereo-spray spraying cap 10.
Described stereo-spray calotte base plate can be screen, porous plate or web plate, can add silk screen or filter cloth above, and silk screen filter cloth and base plate step up; Solid catalyst is placed after can directly placing and also can tying up, and the catalyst top is provided with screen, porous plate or silk screen and impingement baffle, prevents that catalyst is subjected to impact grinding and runs off.
The course of work of the present invention is: gas enters in the stereo-spray calotte 10 by riser 5 from the below of column plate 4, when in gas enters stereo-spray calotte 10, rising, liquid promotes passage 8 by liquid and enters in the calotte, and blown the liquid film that pulls into by gas, liquid film is broken into drop under capillary effect in by the process of gas lift.This burst gas-liquid mixed stream is by the injection channel ejection of draining plate 11 belows.The liquid part is flowed backward to the solid catalyst top between two calottes in the gas-liquid mixed stream, cross catalyst surface by gravity current, gas is partly walked around draining plate and is entered the last layer column plate, the liquid that flows through catalyst surface falls back on the column plate 4, and liquid flows through downspout along column plate and arrives one deck column plate down.
Application Example:
In φ 1000 experiment towers, under the normal pressure, adopt air, water system to carry out cold mould experiment, Ta Nei establishes the common valve plate of one deck and catalytic rectification tower plate has carried out the contrast experiment.
Common board-like tower plate structure parameter is as follows:
Down-flow plate area/tower section amasss=6.8%, open ratio of plate 9.58% (63 φ 39 holes), distance between plates 500mm, height of weir 50mm, height 50mm in crack at the bottom of the downspout.
The catalytic rectification tower plate structural parameters are as follows:
Down-flow plate area 6.8%, open ratio of plate 9.55% (6 50 * 250 rectangular openings), distance between plates 500mm, height of weir 240mm, riser height are 200mm, riser be shaped as rectangle, folded between riser and the column plate is 75 °, height 50mm in crack at the bottom of the downspout, and the loading catalyst area accounts for full tower section long-pending 68% on the column plate, catalyst is to be 001 * 7 commercially available type storng-acid cation exchange resin, combinations of injections cell height 400mm.
Regulate the gas-liquid flow, the maintenance fluid flow is 10m
3/ h measure the plate pressure drop under the different gas phase loads of two kinds of column plates, and the maximum of two kinds of column plates allows the void tower kinetic energy factor.
The contrast experiment 1, and gas flow is 2800m
3/ h, the following two kinds of plate pressure drops contrast of identical empty tower gas velocity:
| The column plate pattern | Plate pressure drop, mmH 2O |
| Common board-like column plate | 75 |
| Catalytic rectification tower plate | 54 |
The contrast experiment 2, and gas flow is 4000m
3/ h, the following two kinds of plate pressure drops contrast of identical empty tower gas velocity:
| The column plate pattern | Plate pressure drop, mmH 2O |
| Common board-like column plate | 112 |
| Catalytic rectification tower plate | 74 |
By above-mentioned contrast experiment as can be seen, under the identical operations working condition, jet tray with large liquid holdup pressure drop ratio tradition valve plate is much lower, (tests 1) during normal duty and has reduced by 28%, (tests 2) during high load capacity and has reduced by 34%.
With gas phase mist entrainment 10% is the upper limit, is 2.3 to the experimental result of the permission maximum kinetic energy factor of the catalytic rectification tower plate of air-water system.
The present invention the experiment proved that: the space availability ratio of catalytic rectification tower plate is very high, when tray spacing is the 600mm of routine, column plate supernatant layer height can be adjusted arbitrarily in the 20-400mm scope, the loading height of catalyst can be adjusted arbitrarily in 50～500mm scope, account for the long-pending part of full tower section and can be used to filling solid catalyst, can satisfy the requirement of catalytic distillation loaded catalyst and liquid and catalyst surface time of contact and uniformity coefficient up to 80%.In this height of liquid layer and catalyst packing height scope, column plate pressure reduces and common valve plate simultaneously, and the void tower kinetic energy factor reaches 2.0Pa
0.5More than, operating flexibility, column plate separative efficiency all are higher than common column plate.
Claims (10)
1, a kind of catalytic rectification tower plate, it mainly comprises column plate, riser, combined jet unit, down-flow plate and seal pot, it is characterized in that: regularly arranged riser is installed on described column plate, on riser, cooperate the combined jet unit is installed, the combinations of injections unit is combined by stereo-spray calotte and solid catalyst, is rectifying and the reaction main place of carrying out on the column plate.
2, according to the described catalytic rectification tower plate of claim 1, what it is characterized in that described riser is shaped as rectangle, trapezoidal or circular.
3,, it is characterized in that angle folded between described riser and the column plate is 45-135 ° according to the described catalytic rectification tower plate of claim 2.
4, according to the described catalytic rectification tower plate of claim 1, it is characterized in that described riser height 0～400mm, row's number in hole is 1-20.
5, according to the described catalytic rectification tower plate of claim 1, it is characterized in that between the stereo-spray calotte of described combinations of injections unit and the riser that it is 2-50mm that liquid promotes channel width, the height of the loading catalyst of catalyst is 20～500mm between the stereo-spray calotte.
6, according to the described catalytic rectification tower plate of claim 1, it is characterized in that described combinations of injections unit be full tower section combination, according to the piecemeal situation of column plate by every column plate combination or single existence.
7,, it is characterized in that described down-flow plate height of weir plate is 20-400mm according to the described catalytic rectification tower plate of claim 1.
8,, it is characterized in that described open ratio of plate 1～20% according to the described catalytic rectification tower plate of claim 1.
9,, it is characterized in that every 1-5 stereo-spray is covered with to put a draining plate according to the described catalytic rectification tower plate of claim 1.
10, according to the described catalytic rectification tower plate of claim 1, it is characterized in that described stereo-spray calotte base plate is screen, porous plate or web plate, can add silk screen or filter cloth above, silk screen filter cloth and base plate step up; Solid catalyst is placed after can directly placing and also can tying up, and the catalyst top is provided with screen, porous plate or silk screen and impingement baffle.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200610013530 CN1895715A (en) | 2006-04-25 | 2006-04-25 | Catalytic rectification tower plate |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200610013530 CN1895715A (en) | 2006-04-25 | 2006-04-25 | Catalytic rectification tower plate |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN1895715A true CN1895715A (en) | 2007-01-17 |
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ID=37608449
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 200610013530 Pending CN1895715A (en) | 2006-04-25 | 2006-04-25 | Catalytic rectification tower plate |
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102516036A (en) * | 2011-12-14 | 2012-06-27 | 河北工业大学 | Process method for preparing methyl tert-butyl ether by differential reaction rectification and equipment for same |
| CN103773494A (en) * | 2013-12-24 | 2014-05-07 | 天津市昊永化工科技有限公司 | Production process and equipment of hydrogen circulation differential catalyst distillation and desulfuration |
| CN109603185A (en) * | 2018-12-28 | 2019-04-12 | 中国二冶集团有限公司 | Pipe fitting method is crossed between two rectifying column platforms |
| CN112174868A (en) * | 2020-09-01 | 2021-01-05 | 河北工业大学 | Method for preparing ethylbenzene hydroperoxide by ethylbenzene reactive distillation and reactive distillation tower thereof |
| CN113941311A (en) * | 2020-07-15 | 2022-01-18 | 中国石油化工股份有限公司 | Vertical tower tray and gas-liquid contact mass transfer equipment with same |
-
2006
- 2006-04-25 CN CN 200610013530 patent/CN1895715A/en active Pending
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102516036A (en) * | 2011-12-14 | 2012-06-27 | 河北工业大学 | Process method for preparing methyl tert-butyl ether by differential reaction rectification and equipment for same |
| CN102516036B (en) * | 2011-12-14 | 2013-10-09 | 河北工业大学 | Process method for preparing methyl tert-butyl ether by differential reaction rectification and equipment for same |
| CN103773494A (en) * | 2013-12-24 | 2014-05-07 | 天津市昊永化工科技有限公司 | Production process and equipment of hydrogen circulation differential catalyst distillation and desulfuration |
| CN103773494B (en) * | 2013-12-24 | 2016-01-20 | 天津市昊永化工工程有限公司 | The production technique of hydrogen circulation differential catalytic distillation desulfurization and equipment |
| CN109603185A (en) * | 2018-12-28 | 2019-04-12 | 中国二冶集团有限公司 | Pipe fitting method is crossed between two rectifying column platforms |
| CN113941311A (en) * | 2020-07-15 | 2022-01-18 | 中国石油化工股份有限公司 | Vertical tower tray and gas-liquid contact mass transfer equipment with same |
| CN112174868A (en) * | 2020-09-01 | 2021-01-05 | 河北工业大学 | Method for preparing ethylbenzene hydroperoxide by ethylbenzene reactive distillation and reactive distillation tower thereof |
| CN112174868B (en) * | 2020-09-01 | 2021-10-01 | 河北工业大学 | Method for preparing ethylbenzene hydroperoxide by ethylbenzene reactive distillation and reactive distillation tower thereof |
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