CN201855587U - Catalytic rectifying tower component - Google Patents
Catalytic rectifying tower component Download PDFInfo
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- CN201855587U CN201855587U CN2010205427477U CN201020542747U CN201855587U CN 201855587 U CN201855587 U CN 201855587U CN 2010205427477 U CN2010205427477 U CN 2010205427477U CN 201020542747 U CN201020542747 U CN 201020542747U CN 201855587 U CN201855587 U CN 201855587U
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- calotte
- tower member
- plate
- liquid
- catalytic distillation
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Abstract
The utility model relates to a catalytic rectifying tower component which is formed by fixing a catalyst at the middle upper part in a cylindrical cap through silk screens, the tower component comprises a tower plate, a downcomer is fixed at one side of the tower plate, a liquid-sealed tank is fixed at the lower part of the downcomer penetrating through the tower plate, a round gas-lifting hole is drilled in the middle of the tower plate, the cylindrical cap is fixed at the upper middle part of the tower plate, the gas-lifting hole and the cylindrical cap are concentrically arranged, small round holes in regular arrangement are drilled at the middle upper part of the cap, a liquid-passing passage is arranged between the bottom of the cap and the tower plate, a baffle plate is arranged at the upper end of the cap, the baffle plate is in the shape of an upwards-protruded arc, the silk screens are fixed at intervals at the middle upper part of the cap, and a catalyst bed layer is arranged between the two layers of silk screens. The rectifying tower component simultaneously has the characteristics of a vertical sieving plate and a catalytic rectifying tower plate and has the characteristics of simple structure, pressure reduction, small entrainment, high catalyst utilization ratio, simultaneous reaction and separation and low cost.
Description
Technical field
The utility model relates to the gas-liquid mass transfer (contact) equipment in the field of chemical engineering catalytic distillation process, is a kind of simple in structure concretely, and pressure drop is low, catalyst utilization height, the catalytic distillation tower member that reaction and rectifying are efficiently carried out simultaneously.
Background technology
Catalytic distillation is a kind of novel separating technology with wide application prospect.The reaction fractionating tower design of a success must have rational tower member simultaneously.Though existing tower member part has obtained commercial Application in reactions such as etherificate, alkylation, all have certain defective.Usually way is divided following two kinds substantially: the porous material that a kind of usefulness can encase catalyst encases catalyst makes the filler basket, be placed on the column plate or downspout in the place flow through of liquid, this kind method is because the structure of column plate causes loaded catalyst little, it is big to take up room, and fluid can not well contact with catalyst; May cause fluid radial distribution inequality, even channel etc.; Another kind method is to be placed between a plurality of stereo-spray calottes after the direct placement of solid catalyst also can be tied up, this method is owing to the liquid that sprays between the calotte liquidates mutually, and transfer upwards, more liquid foam is carried secretly to the upper strata column plate, thereby mist entrainment is bigger, causes plate efficiency to reduce.In a word, existing technology causes catalytic distillation efficient to reduce, and fails to bring into play the advantage of catalytic distillation, thereby has limited the large-scale application of these tower members.
Summary of the invention
In order to solve the deficiency that exists in the background technology, the utility model provides a kind of catalytic distillation tower member, and that this rectifying column member has is simple in structure, pressure drop is low, entrainment is little, catalyst utilization is high, react with separating and carry out simultaneously and characteristics that cost is low.
The technical solution of the utility model is: this catalytic distillation tower member is fixed in the cylindrical cap cover middle and upper part to catalyst with porous material and constitutes.Tower member comprises column plate, one side of column plate is fixed with downspout, downspout passes column plate its underpart and is fixed with liquid seal trough, column plate middle part opened round air rising hole, be fixed with cylindrical cap cover on the air rising hole, air rising hole is provided with cylindrical cap cover is concentric, between calotte bottom and the column plate liquid passage was arranged, plate washer is established in the calotte upper end, plate washer is the lonely shape that raises up, calotte middle and upper part fixed interval has silk screen, is beds between the two-layer silk screen, has regularly arranged circular port on the calotte wall of beds top.
The utlity model has following beneficial effect: the utility model effectively combines the advantage of catalytic rectifying tower and plate column with catalyst and calotte combination.At first novel tower member has kept vertical sieve tray and has had king-sized disposal ability, higher efficient, and it is simple in structure, cost is lower, advantages such as pressure drop is steady, and the utility model proposes catalyst is placed on the special catalyst loading pattern in calotte middle and upper part, increased the solid contact area of gas-liquid, the catalyst filling is simple, improved the space availability ratio in the tower greatly, when the gas phase that upwards flows on the column plate is passed beds, catalyst is in fluidized state, increased the voidage of bed, increased the time of staying of fine drop, so catalyst utilization improves in the tower member space, the tower member leaking liquid amount reduces, mass transfer effect is good; Liquid phase is repeatedly promoted by gas phase in individual layer member cocycle campaign, and reactant contacts with catalyst and carries out catalytic reaction and remove product continuously, has improved conversion ratio and selectivity.Liquid flow has been strengthened in the extracting effect of gas, and reaction heat can in time be released, and helps rectifying separation and guard catalyst, and reaction and separative efficiency all improve.Gas phase is not passed liquid layer by column plate the time, it is lower therefore to operate pressure drop; Because catalyst is seated in the vertical sieve tray cylindrical cap cover, the four sides all is subjected to good protection, the not fragile and loss of catalyst.In addition because the design of the curved baffle at calotte top, when gas-liquid mixture upwards rushes at top cover, because the reflex liquid foam of curved baffle has a downward component velocity, so can further reduce entrainment from covering the hole when outwards spraying.
Description of drawings:
Fig. 1 is a structure cutaway view of the present utility model;
Fig. 2 is a fundamental diagram of the present utility model;
Fig. 3 is a workflow diagram of the present utility model.
1-column plate, 2-are crossed the liquid passage, the 3-calotte, and the 4-beds, the 5-hole, the 6-baffle plate, the 7-air rising hole, the 8-downspout, the 9-liquid seal trough, the 10-water inlet pipe, the 11-air inlet pipe, 12-silk screen, B-are crossed the liquid channel height, C-calotte height, A-catalyst bed layer height.
The specific embodiment:
The utility model is described in further detail below in conjunction with example: this catalytic distillation tower member comprises column plate 1, one side of column plate 1 is fixed with downspout 8, downspout 8 passes column plate 1 its underpart and is fixed with liquid seal trough 9, liquid seal trough 9 can prevent that gas from entering the upper strata column plate by downspout 8, excessive velocities in the time of can preventing again that liquid from flowing into lower floor's column plate by downspout 8.Open air rising hole 7 on column plate 1 middle part is axial, be used for the injection channel of gas-liquid mixture.The middle part is fixed with calotte 3, calotte 3 and air rising hole 7 concentric settings on the column plate 1.For liquid can enter in the tower member, between calotte 3 bottoms and the column plate 1 liquid passage 2 was arranged, plate washer 6 is established in calotte 3 upper ends, and plate washer 6 reduces entrainment simultaneously for the lonely shape that raises up can more effectively be separated gas-liquid two-phase.Calotte 3 middle and upper part fixed interval have silk screen 12, are beds 4 between the two-layer silk screen 12, and silk screen 12 is used for fixing beds 4.Beds is used to carry out gas-liquid-solid three phase catalytic reaction, has increased the contact area of gas-liquid simultaneously.Have regularly arranged circular port 5 on calotte 3 walls of beds 4 tops, hole 5 is the gas-liquid separation hole, is the passage of gas-liquid mixture ejection tower member.Opening diameter can be 2mm, 2.5mm, 3mm, and perforate quantity makes percent opening in 7～10% according to aperture adjustment, and reason is that the calotte percent opening can not form effective liquid less than 7% and spray, and causes opereating specification to diminish; And the calotte percent opening can excessively easily produce liquid flooding greater than 10% o'clock because of liquid sprays under bigger liquid flowing strength.
The radian of described baffle plate 6 is 1.57rad, and the reflex of arc can further reduce entrainment.
The calotte height C of described tower member is 13～25 with crossing liquid channel height B ratio.
Described open ratio of plate is 12～40%.
The diameter ratio of described tower member air rising hole 7 diameters and calotte 3 is 0.3～1, and it is excessive that gas entered the calotte resistance when ratio was lower than this scope, causes pressure drop excessive, and entering the interior liquid of calotte can not fully be promoted, and fragmentation increases leaking liquid amount.
Beds 4 loading heights in the described tower member are 3～10mm.
Described calotte height C and beds height A ratio are 4～6, and the catalyst that uses is the particle of the different shape of diameter 2～5mm.
Described calotte 3 can be rectangle, ladder type or back taper.
Gas-liquid contact condition of the present utility model: as shown in Figure 2:
(1) enters calotte 3 from the gas phase of following one deck column plate from the hole 5 of tower member; Liquid phase from the last layer column plate flows on the column plate by downspout 8, and then crosses liquid passage 2 by tower member and enter calotte 3.The gas-liquid two-phase that enters in the calotte 3 vertically meets at the tower member bottom section.
(2) gas phase that contacts with liquid phase at the tower member bottom section along calotte 3 directions with liquid phase lifting, membrane, be broken into the uneven drops of countless sizes.
(3) gas-liquid mixture contact mass transfer and separation in beds 4 of rising along calotte 3 inwalls.
(4) gas-liquid mixture that rises along calotte 3 inwalls collides baffle plate 6 has part to turn back again, they with riser 3 in go up the gas-liquid mixture fiercenesses of spraying at a high speed collisions, and then liquid phase is broken into more tiny drop.
(5) gas-liquid mixture that rises along calotte 3 inwalls is ejected into outside the calotte 3 with the direction under slightly oblique after baffle plate 6 changes direction by beds 4, and is simultaneously that liquid phase is further broken.
(6) behind the gas-liquid mixture ejection riser 3, the last layer column plate that gas phase rises, liquid phase can fall back on the column plate 1, and part is carried out secondary cycle, enters calotte 3 again.
By top flow process as can be known, the contact condition of gas-liquid two-phase will be through vertically meeting, lifting, membrane, rupture of membranes, carrying out mass transfer at beds 4 and separate, eject calotte 3, gas-liquid separation etc. and recur process on the tower member.The gas-liquid two-phase contact is carried out in all processes, liquid phase is fractured into countless tiny drops in contact process, because the design of catalyst of the present utility model loading position has increased the time of staying of fine drop in the tower member space, the mist entrainment of gas phase significantly reduces, thereby the gas-liquid contact is very abundant, make full use of the space between column plate, improved tower member efficient.
Laboratory experiment: experiment exists
Carry out in 40 * 300 * 4/mm lucite experiment tower, this tower is provided with three column plates, gas distribution grid, brassboard and liquid distributing boards altogether.The experimental provision flow process adopts air-water as the test system as shown in Figure 3.Running water at first through being injected from cat head after the metering of liquid spinner flowmeter by water inlet pipe 10 after the head tank voltage stabilizing, because three blocks of column plates are flow through in the effect of gravity from top to bottom successively, is gone into wet seal area from tower bottom flow at last.Air from compressor come out through purify, after the voltage stabilizing by air inlet pipe 11 at the bottom of entering tower after the gas rotameter metering, under the effect of pressure difference, constantly rise, successively by three blocks of column plates, finally in cat head emptying.Gas-liquid two-phase fully contact on each layer column plate, also stream injection, mass transfer.Wherein, the intermediate layer tower member is a brassboard, and two-layer up and down is respectively liquid distributing board and gas distribution grid.
Under identical experimental implementation condition, in this experiment tower, carried out the utility model and with the performance test of the vertical sieve plate column of the utility model same size and common rectifying tower and compare with it and draw to draw a conclusion:
1, the tower member plate pressure drop does not make plate pressure drop than common vertical sieve tray pressure drop significant change be arranged because add beds in the calotte, just works as the void tower kinetic energy factor at 0.0025～0.01 (m/s) (kg/m
3)
1/2Be slightly higher than vertical sieve tray pressure drop 1.2～2% in the low gas flow scope, and still maintain than in the low pressure drop scope.So novel tower member has kept the low advantage of original vertical sieve tray pressure drop.
2, the tower member leaking liquid amount reduces 35～50% than vertical sieve plate column leaking liquid amount, when plate supernatant layer height is 32mm, the void tower kinetic energy factor be lower than the leakage point (
) time, the tower member leaking liquid amount increases rapidly.
3, the entrainment of tower member is than low about 8 times of existing conventional distillation column plate.
4, be that catalyst fills in the calotte outside and compares with the catalyst loading pattern of existing tower member, catalyst fills in calotte inside makes the tower member space availability ratio obviously improve.
5, catalyst is fixed in the calotte with two-layer silk screen, and the four sides all is protected, and is difficult for running off, so the loss of tower member inner catalyst is very little.
Claims (9)
1. catalytic distillation tower member, comprise column plate (1), it is characterized in that: a side of column plate (1) is fixed with downspout (8), downspout (8) passes column plate (1), downspout (8) bottom is fixed with liquid seal trough (9), column plate (1) middle part has circular air rising hole (7), be fixed with cylindrical cap cover (3) on the column plate (1), calotte (3) covers on the air rising hole (7), air rising hole (7) and the concentric setting of calotte (3), between calotte (3) bottom and the column plate (1) liquid passage (2) was arranged, plate washer (6) is established in calotte (3) upper end, the lonely shape of plate washer (6) for raising up, and calotte (3) middle and upper part fixed interval has silk screen (12), be beds (4) between the two-layer silk screen (12), have regularly arranged circular port (5) on the wall of the calotte (3) of beds (4) top.
2. catalytic distillation tower member according to claim 1 is characterized in that: hole (5) percent opening on the calotte (3) is 7～10%.
3. catalytic distillation tower member according to claim 2 is characterized in that: beds (4) loading height in the tower member is between 3～10mm.
4. catalytic distillation tower member according to claim 3 is characterized in that: the radian of described baffle plate (6) is 1.57rad.
5. catalytic distillation tower member according to claim 4 is characterized in that: the calotte height (C) of described tower member and mistake liquid channel height (B) ratio are between 13～25.
6. catalytic distillation tower member according to claim 5 is characterized in that: the percent opening that described column plate (1) is gone up air rising hole (7) is between 12～40%.
7. catalytic distillation tower member according to claim 6 is characterized in that: the ratio of described tower member air rising hole (7) diameter and calotte (3) diameter is between 0.3～1.
8. catalytic distillation tower member according to claim 7 is characterized in that: calotte height (C) and catalyst bed layer height (A) ratio are between 4～6, and the catalyst that uses is the particle between diameter 2～4m.
9. catalytic distillation tower member according to claim 8 is characterized in that: calotte (3) is rectangle, ladder type or back taper.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010205427477U CN201855587U (en) | 2010-09-27 | 2010-09-27 | Catalytic rectifying tower component |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010205427477U CN201855587U (en) | 2010-09-27 | 2010-09-27 | Catalytic rectifying tower component |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN201855587U true CN201855587U (en) | 2011-06-08 |
Family
ID=44101406
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2010205427477U Expired - Fee Related CN201855587U (en) | 2010-09-27 | 2010-09-27 | Catalytic rectifying tower component |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN201855587U (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101940848A (en) * | 2010-09-27 | 2011-01-12 | 大庆油田飞马有限公司 | Catalytic rectification column member |
| CN104096375A (en) * | 2014-07-23 | 2014-10-15 | 安庆市东徽机械有限公司 | Tower skirt for rectifying tower |
| CN108043061A (en) * | 2017-12-25 | 2018-05-18 | 万华化学集团股份有限公司 | It is a kind of can more catalyst changeout online catalytic distillation column plate |
-
2010
- 2010-09-27 CN CN2010205427477U patent/CN201855587U/en not_active Expired - Fee Related
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101940848A (en) * | 2010-09-27 | 2011-01-12 | 大庆油田飞马有限公司 | Catalytic rectification column member |
| CN104096375A (en) * | 2014-07-23 | 2014-10-15 | 安庆市东徽机械有限公司 | Tower skirt for rectifying tower |
| CN108043061A (en) * | 2017-12-25 | 2018-05-18 | 万华化学集团股份有限公司 | It is a kind of can more catalyst changeout online catalytic distillation column plate |
| CN108043061B (en) * | 2017-12-25 | 2021-03-09 | 万华化学集团股份有限公司 | Catalytic distillation column plate capable of replacing catalyst on line |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C17 | Cessation of patent right | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20110608 Termination date: 20120927 |