CN2503959Y - Catalyst distillation plant - Google Patents
Catalyst distillation plant Download PDFInfo
- Publication number
- CN2503959Y CN2503959Y CN 01262281 CN01262281U CN2503959Y CN 2503959 Y CN2503959 Y CN 2503959Y CN 01262281 CN01262281 CN 01262281 CN 01262281 U CN01262281 U CN 01262281U CN 2503959 Y CN2503959 Y CN 2503959Y
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- catalytic distillation
- epimere
- distillation tower
- catalysis
- lifting tube
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Abstract
The utility model relates to a catalytic distillation equipment. A reaction rectifying area comprises a liquid dropping pipe, a liquid containing plate, a liquid sealing pipe, a material sealing plate, a material receiving plate, a fractionation element and catalyst bed layers. The utility model is characterized in that an air rising pipe is arranged between the catalyst bed layers, the fractionation element is arranged at the top part of the air rising pipe or inside the air rising pipe; and a gap is provided between the bottom part of the air rising pipe and the liquid containing plate, a channel is arranged between the material receiving plate and the bottom part of the catalyst bed layer, and a space is left between the material receiving plate and the liquid containing plate below. The device is favorable to the gas and liquid mass transfer, and is favorable to the reaction, and the efficiency of catalyzing and fractionation is high. The catalytic distillation equipment of the utility model can also be formed by the upper section of a catalytic distillation tower and the lower section of the catalytic distillation tower connected in series, and the upper section and the lower section are separated by a separation plate, the upper section and the lower section of the catalytic distillation tower both comprise the reaction rectifying area, and the upper section and the lower section are mutually connected through an outside pipeline. The production process is simplified, the investment in the equipment is reduced and the energy consumption is reduced.
Description
Technical field
The utility model relates to a kind of catalysis-distillation equipment that is used for catalytic reaction distillation technology.
Background technology
Traditional petroleum hydrocarbon hydrogenation desulfurization technology adopts fixed-bed process, because reaction mass is all by beds, the easy hydro-conversion of alkene is an alkane.Chinese patent ZL96196515.0 is disclosed in the mercaptan that removes respectively in two catalytic distillation towers in the light component and the sulfide of heavy ends, and this two tower is respectively equipped with reboiler, condenser, equipment investment is big, energy consumption is high.
Catalytic distillation technology successfully is used for technologies such as etherificate, hydrogenation, in order to solve catalyst filling structure problem, bibliographical information multiple catalyst filling structure, as: USP3,434,534 adorn system with catalyst fills out in the downspout of conversion zone plate, because the loadings of catalyst is restricted in the downspout, is difficult to carry out industrial applications.UPS4,471,154 are contained in catalyst in the sack of definite shape, place then on the plate of conversion zone,, influenced separation because catalyst has accounted for certain space on tower tray, and in order to increase the loadings of catalyst, the tower tray downflow weir of this structure is higher, thereby the pressure of tower tray is bigger, is difficult to stable operation; Similar structure such as Chinese patent ZL89104752, ZL90103696.USP4, the packing method of 215,011 catalyst that disclose be catalyst packing in the special sack of glass wool cloth, and be rolled into bundle, be contained in the middle part conversion zone of tower then, the packaging structure complexity of catalyst.EP448 and for example, 884 catalyst that disclose are seated in the interlayer of two-layer ripple web plate, and another layer is the path of vapour-liquid; The filling structure complexity of catalyst.
The utility model content
Technical problem to be solved in the utility model provides a kind of catalysis-distillation equipment, helps vapour, liquid mass transfer, catalysis, fractionating efficiency height.The utility model also has the simplification technical process, reduces equipment investment, the characteristics that cut down the consumption of energy.
Catalysis-distillation equipment of the present utility model, the reactive distillation district comprises downspout, seal pot, liquid sealing pipe, material shrouding, rewinding plate, fraction elements, beds, it is characterized in that steam lifting tube being set at the catalyst bed interlayer, in steam lifting tube top or its fraction elements is set, gapped between steam lifting tube bottom and liquid-receiving plate, leave passage between rewinding plate and beds bottom, leave the space between the seal pot of rewinding plate and its underpart.
This catalysis-distillation equipment is with the pairing position of fraction elements that is arranged in the prior art on the column plate (the utility model is a seal pot), design has steam lifting tube, fraction elements is arranged on the steam lifting tube top, can be float valve, or sieve aperture, cap, ligulate injection etc., or in steam lifting tube the fractionation filler of dress certain altitude.Steam lifting tube quantity determines according to the vapour phase load in the tower, its area be tower sectional area 3～90%, the cross sectional shape of steam lifting tube be a circle, or the shape of rectangle, square, triangle and other processing.Steam lifting tube be arranged as rounded projections arranged, or bar shaped arranges, the mode of arrangement depend on to reaction, separate all favourable.The height of steam lifting tube depends primarily on the loadings of catalyst, and the loadings of catalyst is big more, and steam lifting tube is high more, is generally 100～4000mm.Liquid phase material between the bottom of steam lifting tube and liquid-receiving plate certain clearance arranged, so that can flow in the steam lifting tube.The liquid that the downflow weir gap of liquid sealing pipe can be satisfied on the tower tray flows in the downspout, and its width is generally 5～100mm.The height of downflow weir depends on the height of beds, should can be immersed in the liquid phase material to keep catalyst a little more than beds.
Generally speaking, the material shrouding seals, and can flow downward to guarantee the vapour-liquid material, and pass beds.Certain clearance is arranged at the bottom of the bottom of liquid sealing pipe, rewinding plate and beds, flow in the liquid sealing pipe the general 30～200mm of the height in this gap so that pass vapor-phase material, the liquid phase material of beds.
Carry out heat, matter transmission under the effect that the vapor-phase material and the liquid phase material of steam lifting tube rising are being located at the fraction elements in the steam lifting tube, vapour, liquid phase material after heat, the matter transmission pass beds, and carry out catalytic reaction under catalyst action.This catalytic structure helps vapor-phase material and liquid phase material passes beds simultaneously, and the reaction mass in the vapor-phase material has increased the concentration of reaction mass constantly to the catalyst surface diffusion when passing beds, helps the carrying out that reacts.
Catalysis-distillation equipment of the present utility model can also be to be in series by catalytic distillation tower epimere and catalytic distillation tower hypomere, epimere is separated by dividing plate with intersegmental down, the epimere of catalytic distillation tower and hypomere include the reactive distillation district, and epimere communicates with following intersegmental pipeline by the outside.The heavy of catalytic distillation tower epimere and high boiling component enter into the catalytic distillation tower hypomere by pipeline, and the light components of hypomere enters into the catalytic distillation tower epimere by pipeline, control valve.
The epimere of catalytic distillation tower and hypomere preferably all should comprise stripping zone, reactive distillation district, rectification zone, the heavy sulfide of epimere stripping zone and high boiling component communicate by the rectification zone of pipeline with the catalytic distillation tower hypomere, on pipeline, be added with pump, so that the liquid phase material of catalytic distillation tower epimere stripping zone flows to the rectification zone of the hypomere of catalytic distillation tower.The light components of the rectification zone of catalytic distillation tower hypomere communicates with the stripping zone of catalytic distillation tower epimere by pipeline, control valve.On pipeline, add control valve, so that the vapor-phase material of catalytic distillation tower hypomere rectification zone flows to the stripping zone of the epimere of catalytic distillation tower, and the pressure of keeping the catalytic distillation tower hypomere is higher than epimere, makes the bottom of delivering to the catalytic distillation tower epimere from the vapor-phase material that contains light components of catalytic distillation tower hypomere.
The catalytic distillation tower hypomere is connected with reboiler outward and provides heat for catalytic distillation tower, be provided with condenser and stripping jar outside the top of catalytic distillation tower epimere, the rectification zone of condenser, stripping jar and epimere forms and refluxes, and also has the outlet of gas phase and liquid phase material on the stripping jar respectively.
This in-line catalysis-distillation equipment of the utility model has overcome the shortcoming that patent 96196515.0 is established the operating procedure of two towers, has not only simplified technical process, and has saved a cover reboiler, condenser, has reduced equipment investment, has saved energy consumption.
For this in-line catalysis-distillation equipment, the reactive distillation district also can adopt various catalytic distillation beds in the prior art.No matter the utility model is the improvement to the reactive distillation district, still in-line catalysis-distillation equipment, and except description of the present utility model, all the other are basic with existing catalysis-distillation equipments.
Advantage of the present utility model:
The reactive distillation district of catalysis-distillation equipment helps vapour, liquid mass transfer, helps the carrying out, catalysis and the fractionating efficiency height that react.This equipment is suitable for petroleum hydrocarbon hydrogenation desulfurization, is applicable to that also the petroleum hydrocarbon hydrogenation takes off the hydrolysis of the esterification of diolefin and alkynes, alcohol and acid, ester, olefin hydration reaction, and C
4～C
8Tertiary olefin and C
1～C
4The synthetic corresponding ether product of aliphatic hydrocarbon reaction.Series-mode frame of the present utility model has been simplified production process, has reduced equipment investment, has reduced energy consumption.
Description of drawings
Fig. 1 is a reactive distillation plot structure schematic diagram;
Fig. 2 is a structural representation of the present utility model;
The specific embodiment
In conjunction with the accompanying drawings 2, the catalytic distillation technology that the utility model is used for petroleum hydrocarbon hydrogenation desulfurization describes.
Catalytic distillation tower is divided into two sections of serial operation: the hypomere a of catalytic distillation tower, catalytic distillation tower epimere b, and by dividing plate 14 separately.The epimere b of catalytic distillation tower is divided into: go up rectification zone 2, go up reactive distillation district 3 and last stripping zone 4; The hypomere a of catalytic distillation tower is divided into: following rectification zone 17, following reactive distillation district 18 and following stripping zone 19.Petroleum hydrocarbon enters the top of last stripping zone 4 of the epimere b of catalytic distillation tower through pipeline 1, in last stripping zone 4 and tower on the vapor-phase material that flows carry out the caloic transmission, the light component vaporization enters reactive distillation district 3 and carries out heat, matter transmission and catalytic reaction with the liquid phase material that flows downward, contained diolefin and thiol reactant in the light component removes mercaptan wherein.The vapor-phase material that leaves reactive distillation zone carries out heat, matter transmission with the liquid phase material that refluxes in last rectification zone 2, enter in the stripping jar 10 unreacted H then through pipeline 7, control valve 8, condenser 9
2With the H that generates
2S through stripping after pipeline 11 goes out device; Liquid phase material part behind the stripping is back to the top of catalytic distillation tower epimere b through pipeline 13, and another part goes out device through pipeline 12, can be used as light-end products, or further refining as the synthetic raw material of ether product.Heavy product is entered the top of catalytic distillation tower hypomere a through pipeline 5, pump 22 and pipeline 23 by the bottom of catalytic distillation tower epimere b.
React required H
2Enter the top of the following stripping zone 19 of catalytic distillation tower hypomere a through pipeline 16, and with tower in be mixed into down in the reactive distillation district 18 to last mobile vapor-phase material, the liquid phase material of rectification zone 17 carries out caloic transmission and catalytic reaction with coming from down then, is converted into H behind the contained sulfide hydrogenation in the petroleum hydrocarbon
2S, and remove wherein sulphur.The vapor-phase material that leaves down reactive distillation district 18 is carrying out the caloic transmission with liquid phase material in the rectification zone 17 down, and then through pipeline 20, control valve 21 and pipeline 6 enter the bottom of catalytic distillation tower epimere b.Liquid phase material through descending stripping zone 19 is behind pipeline 24, and a part is through the bottom that reboiler 25 is vaporized, pipeline 26 returns catalytic distillation tower hypomere a, and another part goes out device as heavy product through pipeline 27.
The technology that above-mentioned distillation equipment embodied has overcome the shortcoming that patent 96196515.0 is established the operating procedure of two towers, has not only simplified technical process, and has saved a cover reboiler, condenser, has reduced equipment investment, has saved energy consumption.The epimere of catalytic distillation tower is the light component desulfurizing tower, and hypomere is the heavy ends desulfurizing tower.Generally speaking, the operating pressure of the epimere of control catalytic distillation tower is that the operating pressure of 0.2～2.3Mpa, hypomere is 1.2～3.0Mpa, to keep suitable reaction temperature.
In conjunction with Fig. 1, the reactive distillation district of catalysis-distillation equipment of the present utility model is further specified.
The last reactive distillation district 3 of catalytic distillation tower, the characteristics in following reactive distillation district 18: the plate 30 of the loading catalyst of at least two overlapping settings and plate 31, plate comprise downspout 32 (material inlet pipe) and downspout 35 (material goes out pipe), seal pot 33, steam lifting tube 34, fraction elements 36, catalyst filling zone 37, liquid sealing pipe 38, material shrouding 39 and rewinding plate 40.
Generally speaking, material shrouding 39 seals, and can flow downward, and pass beds to guarantee vapour, liquid phase material.The bottom of liquid sealing pipe 38, rewinding plate 39 has certain clearance with the bottom of beds, flow in the liquid sealing pipe the general 30～200mm of the height in this gap so that pass vapor-phase material, the liquid phase material of beds.
The liquid phase material that comes from downspout 32 is behind seal pot 33, be carried into the top of steam lifting tube with vapor-phase material and stream, and under the effect of the fraction elements 36 at the top of steam lifting tube, carry out the caloic transmission, vapor-phase material after the caloic transmission, liquid phase material and stream pass beds 3, react under catalyst action.Carrying out along with reaction, reactant continues to the liquid phase material transmission in the vapour phase, promote the carrying out of reaction, reacted vapour, liquid phase material flow to then and carry out caloic transmission and catalytic reaction on next fractionating tray through receiving liquid plate 40, liquid sealing pipe 38 inflow downspouts 35.
Embodiment:
Catalytic distillation tower is totally 40 theoretical plates, and dividing plate is between 15 and 16 blocks of plates, and the gasoline feeding plate is at the 10th block of plate, and hydrogen feed is at the 37th block of plate.The catalytic distillation tower epimere is adorned a kind of nickel-containing catalyst and is used for removal of mercaptans, and the catalytic distillation tower hypomere is adorned a kind of cobalt, molybdenum series catalyst, is used for hydrodesulfurization.
FCC gasoline (catalytically cracked gasoline) 1 inlet amount is 10Kg/h, 40 ℃ of feeding temperatures, hydrogen 16 inlet amount 0.86Kg/h.
Catalytic distillation tower hypomere pressure 2.5Mpa, 305 ℃ of tower still temperature, catalytic distillation tower epimere pressure 0.35Mpa, tower top temperature 65C.
The amount of tower still discharging 27 is 6.02Kg/h, and the amount of cat head vapour phase discharging 11 is 0.96Kg/h, and the amount of cat head liquid phase discharging 12 is 3.894Kg/h.
Adopt this technology, equipment, the sulphur in the FCC gasoline is 1500ppm, and the sulfur content of after the hydrodesulfurization light component of cat head being mixed with the heavy ends of tower still in the gasoline of back is 111ppm.
Shown in the quality of material table composed as follows
| Logistics | C3～C5 ％m/m | C6 ％m/m | C7 ％m/m | C8～C12 ％m/m | Hydrogen %m/m | Sulphur %m/m |
| FCC gasoline | 14.80 | 21.74 | 19.04 | 44.42 | 0 | 1500pmm |
| The heavy ends of tower still | 0.00067 | 0.00036 | 25.499 | 74.5 | 0 | 138pmm |
| The cat head fixed gas | 8.51 | 0.83 | 0 | 0 | 89.51 | 1.45 |
| The cat head light component | 35.89 | 55.60 | 9.47 | 2.44 | 1.52 | 70pmm |
Claims (8)
1, a kind of catalysis-distillation equipment, the reactive distillation district comprises downspout, seal pot, liquid sealing pipe, material shrouding, rewinding plate, fraction elements, beds, it is characterized in that steam lifting tube being set at the catalyst bed interlayer, in steam lifting tube top or its fraction elements is set, gapped between steam lifting tube bottom and liquid-receiving plate, leave passage between rewinding plate and beds bottom, leave the space between the seal pot of rewinding plate and its underpart.
2, catalysis-distillation equipment according to claim 1 is characterized in that the height of the downflow weir of liquid sealing pipe is higher than the height of beds.
3, catalysis-distillation equipment according to claim 1, it is characterized in that the steam lifting tube area be tower section long-pending 3～90%, highly be 100～4000 millimeters.
4, catalysis-distillation equipment according to claim 1 is characterized in that fraction elements is arranged on the steam lifting tube top, can spray for float valve, sieve aperture, cap, ligulate.
5, catalysis-distillation equipment according to claim 1 is characterized in that being equipped with the fractionation filler in steam lifting tube.
6, catalysis-distillation equipment according to claim 1, it is characterized in that being in series by catalytic distillation tower epimere and catalytic distillation tower hypomere, epimere is separated by dividing plate with intersegmental down, the epimere of catalytic distillation tower and hypomere include the reactive distillation district, and epimere communicates with following intersegmental pipeline by the outside.
7, catalysis-distillation equipment according to claim 6, it is characterized in that catalytic distillation tower epimere and hypomere include stripping zone, reactive distillation district, rectification zone, the heavy sulfide of epimere stripping zone and high boiling component communicate by the rectification zone of pipeline with the catalytic distillation tower hypomere, be added with pump on pipeline, the light components of the rectification zone of catalytic distillation tower hypomere communicates with the stripping zone of catalytic distillation tower epimere by pipeline, control valve.
8, catalysis-distillation equipment according to claim 6, it is characterized in that the catalytic distillation tower hypomere is connected with reboiler outward, be provided with condenser and stripping jar outside the top of catalytic distillation tower epimere, the rectification zone of condenser, stripping jar and epimere forms and refluxes, and also has the outlet of gas phase and liquid phase material on the stripping jar respectively.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 01262281 CN2503959Y (en) | 2001-10-20 | 2001-10-20 | Catalyst distillation plant |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 01262281 CN2503959Y (en) | 2001-10-20 | 2001-10-20 | Catalyst distillation plant |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN2503959Y true CN2503959Y (en) | 2002-08-07 |
Family
ID=33670051
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 01262281 Expired - Lifetime CN2503959Y (en) | 2001-10-20 | 2001-10-20 | Catalyst distillation plant |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN2503959Y (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110172013A (en) * | 2019-06-24 | 2019-08-27 | 中国石油化工股份有限公司 | A kind of technique based on catalytic distillation solvent method synthesis tert-pentyl alcohol |
| WO2022083688A1 (en) * | 2020-10-21 | 2022-04-28 | 中国石油化工股份有限公司 | Catalytic reaction unit and reactive distillation column |
| CN116059926A (en) * | 2021-10-29 | 2023-05-05 | 中国石油化工股份有限公司 | Hydrofractionation reactor and combined reactor |
-
2001
- 2001-10-20 CN CN 01262281 patent/CN2503959Y/en not_active Expired - Lifetime
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110172013A (en) * | 2019-06-24 | 2019-08-27 | 中国石油化工股份有限公司 | A kind of technique based on catalytic distillation solvent method synthesis tert-pentyl alcohol |
| CN110172013B (en) * | 2019-06-24 | 2023-06-16 | 中国石油化工股份有限公司 | Process for synthesizing tertiary amyl alcohol based on catalytic distillation solvent method |
| WO2022083688A1 (en) * | 2020-10-21 | 2022-04-28 | 中国石油化工股份有限公司 | Catalytic reaction unit and reactive distillation column |
| CN116059926A (en) * | 2021-10-29 | 2023-05-05 | 中国石油化工股份有限公司 | Hydrofractionation reactor and combined reactor |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| ASS | Succession or assignment of patent right |
Owner name: CHINA PETROLEUM & CHEMICAL CORPORATION; PATENTEE Free format text: FORMER OWNER: QILU PETROCHEMICAL GROUP CO., CHINA PETROCHEMICAL CORP. Effective date: 20070608 |
|
| C41 | Transfer of patent application or patent right or utility model | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20070608 Address after: 100029, No. 6, Xin Xin Street East, Beijing, Chaoyang District Co-patentee after: Qilu Petrochemical Co., China Petrochemical Group Corp. Patentee after: Sinopec Corp. Address before: 124 box 255400, Linzi District, Shandong, Zibo Patentee before: Qilu Petrochemical Co., China Petrochemical Group Corp. |
|
| ASS | Succession or assignment of patent right |
Owner name: CHINA PETROLEUM & CHEMICAL CORPORATION Free format text: FORMER OWNER: CHINA PETROLEUM + CHEMICAL CORPORATION; PATENTEE Effective date: 20080104 |
|
| C41 | Transfer of patent application or patent right or utility model | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20080104 Address after: No. 6, Xin Xin Street East, Beijing, Chaoyang District, China: 100029 Patentee after: Sinopec Corp. Address before: No. 6, Xin Xin Street East, Beijing, Chaoyang District, China: 100029 Co-patentee before: Qilu Petrochemical Co., China Petrochemical Group Corp. Patentee before: China Petroleum Chemical Co |
|
| C17 | Cessation of patent right | ||
| CX01 | Expiry of patent term |
Expiration termination date: 20111020 Granted publication date: 20020807 |