CN106693432B - Centrifugal rotational flow defoaming type gas-liquid mixed phase feeding distributor - Google Patents
Centrifugal rotational flow defoaming type gas-liquid mixed phase feeding distributor Download PDFInfo
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- CN106693432B CN106693432B CN201710171649.3A CN201710171649A CN106693432B CN 106693432 B CN106693432 B CN 106693432B CN 201710171649 A CN201710171649 A CN 201710171649A CN 106693432 B CN106693432 B CN 106693432B
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- annular
- annular sleeve
- tower
- gas
- liquid mixed
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- 239000007788 liquid Substances 0.000 title claims abstract description 53
- 238000012856 packing Methods 0.000 claims abstract description 32
- 239000000945 filler Substances 0.000 claims abstract description 21
- 238000005406 washing Methods 0.000 claims abstract description 21
- 239000012071 phase Substances 0.000 claims description 30
- 239000012808 vapor phase Substances 0.000 claims description 14
- 238000005191 phase separation Methods 0.000 claims description 11
- 238000005728 strengthening Methods 0.000 claims description 3
- 238000007872 degassing Methods 0.000 abstract 1
- 230000000694 effects Effects 0.000 description 9
- 238000004939 coking Methods 0.000 description 6
- 239000007791 liquid phase Substances 0.000 description 5
- 238000000926 separation method Methods 0.000 description 4
- 238000009826 distribution Methods 0.000 description 3
- 239000006096 absorbing agent Substances 0.000 description 2
- 230000000903 blocking effect Effects 0.000 description 2
- 239000000571 coke Substances 0.000 description 2
- 230000007547 defect Effects 0.000 description 2
- 239000008258 liquid foam Substances 0.000 description 2
- 238000000034 method Methods 0.000 description 2
- 230000008569 process Effects 0.000 description 2
- 230000000630 rising effect Effects 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical group [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 230000001174 ascending effect Effects 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 238000004581 coalescence Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 230000004907 flux Effects 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 229910001385 heavy metal Inorganic materials 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
- 230000000087 stabilizing effect Effects 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000009827 uniform distribution Methods 0.000 description 1
- 238000005292 vacuum distillation Methods 0.000 description 1
- 238000009736 wetting Methods 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/008—Liquid distribution
Landscapes
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Physical Or Chemical Processes And Apparatus (AREA)
Abstract
A centrifugal rotational flow defoaming gas-liquid mixed phase feeding distributor is characterized in that a gas-liquid mixed phase feeding port is of a tangential rectangular feeding structure and is communicated with an annular sleeve in a tower; the lower end of the annular sleeve is provided with an opening, an annular grid filler for decelerating, absorbing energy and degassing is arranged 200-1500mm away from the lower end of the annular sleeve, the height is 50-100mm, and the width is 0.3-2.5 times of the width of the annular sleeve; the middle part of the annular sleeve is closed to form an annular oil collecting tank; the upper end of the annular sleeve is connected with a steady flow defoaming self-washing parallel flow packing layer; the connecting lines of the inner edge and the outer edge of the parallel flow packing layers are umbrella-shaped structures, and the annular width of the packing layers is 3-500 times of the interval between the packing plates.
Description
1. Technical field
The invention provides a centrifugal rotational flow defoaming type gas-liquid mixed phase feeding distributor, and relates to the field of separation towers.
2. Background art
The tower internals are important components of the packed tower or the plate tower, and form a complete packed tower or plate tower together with the tower body and the tower plates or the packing, and all the tower internals have the functions of enabling gas-liquid two phases to be better contacted in the tower so as to exert the maximum efficiency and the maximum production capacity of the packing or the tower plates, and the performance of the packing or the tower plates and the performance of the whole packed tower or the plate tower are directly influenced by the design of the tower internals.
In the process of chemical homogeneous phase separation, gas-liquid mixed phase feeding is the most commonly encountered working condition of a distillation tower, such as an atmospheric and vacuum distillation tower. The gas-liquid mixed phase feeding distributor is used for effectively separating the gas phase from the liquid phase in the feeding, and meanwhile, the vapor phase is well distributed along the section of the tower, and the liquid phase also has good collecting and distributing effects. The good tower feeding section structure not only can stabilize the operation of the tower, but also can improve the separation effect of the tower.
There are various types of gas-liquid miscible feed distributors: the device is typically provided with a double tangential circulation type, a single tangential circulation type, a double-row vane type, a tangential horn type, a radial air inlet distributor with an umbrella-shaped deflector, a radial air inlet distributor with a liquid capturing energy absorber and the like, and is respectively suitable for different feeding environments. The gas-liquid two-phase separation effect of some feeding distributors is good, and the feeding distributor can meet the requirement of the large-scale tower, such as single tangential circulation, but the vapor phase is unevenly distributed along the section of the tower, and a vortex airflow is generated in the center of the tower; the vapor phase of the feeding distributor is uniformly distributed along the section of the tower, the entrainment of liquid foam in the rising vapor flow is not much, the requirement of the tower on large-scale can be met, but the descending liquid entrains the vapor phase, and the content of light components in the tower bottom product, such as a double tangential circulation type distributor, can be influenced; the vapor phase of the feed distributor is uniformly distributed along the section of the tower, so that the requirement of the tower on large-scale can be met, but the gas-liquid two-phase separation effect is poor, such as a tangential horn type distributor; the radial air inlet distributor with the umbrella-shaped flow guider, in particular to the radial air inlet distributor with the liquid-capturing energy absorber, has better gas-liquid two-phase separation effect and more uniform vapor phase distribution along the section of the tower, but cannot meet the requirement of the tower on large size.
In addition, more or less entrainment of liquid foam is inevitably caused in the rising steam flow of the gas-liquid mixed-phase feeding distributor, and a washing section is often arranged above the feeder in order to ensure the quality of side products. If a washing section is arranged on the feeding section of the vacuum tower, the washing oil washes liquid, coke, asphaltene, carbon residue, heavy metal and the like entrained in the vapor by contacting with the ascending material flow on one hand, and on the other hand, heavy wax oil and residual oil can be well separated by the mass transfer function of vapor phase and liquid phase, and the dry point of the heavy wax oil is controlled, which is the key of the vacuum tower to ensure the quality of the heavy wax oil. In addition, the amount of wash oil must meet the requirements of wetting the filler surface to prevent coking of the filler surface. Advanced washing section structure and necessary washing oil amount (minimum flow control) are adopted to avoid coking and reduce energy consumption. For a vacuum tower requiring the minimum pressure drop, the phenomenon that the surface of local packing is not wetted easily occurs because the liquid spray density of a washing section is smaller, and the operation temperature of a packing bed layer is high, so that coking easily occurs. Therefore, a filler with high coking resistance, especially the middle and lower part of the filler bed layer, must be selected, and a filler with high flux and smooth surface must be used. In addition, in order to ensure that the surface of the filler can be fully wetted, the liquid distributor of the washing section can adopt a gravity distributor or a power distributor, but because the operation temperature of the washing section is high, the liquid spraying density is low, washing oil is easy to coke and block, and the structure and parameters of the liquid distributor are difficult to select, which is the biggest bottleneck for restricting the long-period safe operation of the washing section.
3. Summary of the invention
The invention aims to overcome the defects and defects of the existing gas-liquid mixed phase feeding distributor and washing section structure, and discloses a centrifugal rotational flow defoaming gas-liquid mixed phase feeding distributor, which is used for eliminating liquid phase and vapor phase entrainment, reducing feeder pressure drop, realizing good gas-liquid two-phase separation effect, uniformly distributing vapor phase along the section of a tower, meeting the distribution requirement of a large gas-liquid mixed phase feeding tower, avoiding the coking and blocking phenomenon of a filler and an oil collecting tank, eliminating the maximum bottleneck restricting the long-period safe operation of a washing section, and achieving the good feeder aim of improving the tower separation effect while stabilizing the operation of the tower.
The technical scheme of the invention is as follows:
the invention provides a centrifugal rotational flow defoaming gas-liquid mixed phase feeding distributor, which is characterized in that a gas-liquid mixed phase feeding port is of a tangential rectangular feeding structure and is communicated with an annular sleeve in a tower; the lower end of the annular sleeve is provided with an opening, the distance from the lower end of the annular sleeve to 200-1500mm is provided with annular grid packing for guiding and decelerating and strengthening the vapor phase separation function, the height is 50-100mm, the width is 0.3-2.5 times of the width of the annular sleeve, the interval between packing plates is 3-50mm, and the horizontal inclination of the packing plates is 30-90 degrees; the middle part of the annular sleeve is sealed to form an annular oil collecting tank, the outer wall of the bottom of the annular oil collecting tank is communicated with the lower part of the annular grid filler through an external connecting pipe, or the inner wall of the annular oil collecting tank is uniformly provided with tear holes with equivalent diameters of 5-30 mm; the upper end of the annular sleeve is connected with a parallel flow packing layer with steady flow defoaming self-washing function; the connecting lines of the inner edge and the outer edge of the parallel flow packing layers are umbrella-shaped structures, the annular width of the packing layers is 3-500 times of the spacing of the packing plates, and the spacing of the packing plates is 1-30mm.
Wherein the ratio of the height to the width of the gas-liquid mixed phase feeding port is 2-15:1, the ratio of the height of the gas-liquid mixed phase feeding port to the height of the inner annular sleeve in the tower is 1:1-10, and the ratio of the width of the gas-liquid mixed phase feeding port to the width of the inner annular sleeve in the tower is 1:1-1.5.
The annular cross section of the annular sleeve in the tower accounts for 5-80% of the cross section of the tower, and the inner wall of the annular sleeve in the height direction is of a cylindrical or conical structure.
The present invention will be described in detail with reference to examples.
4. Description of the drawings
Fig. 1 is a schematic structural view of the present invention.
The diagram of fig. 1 is illustrated as follows:
1. the tower body 2, the gas-liquid mixed phase feeding port 3, the annular sleeve 4, the annular grid filler 5, the annular oil collecting tank 6, the parallel flow filler layer 7 and the external connecting pipe
The process features of the present invention are described in detail below with reference to the accompanying drawings and examples.
5. Detailed description of the preferred embodiments
Examples
A centrifugal rotational flow defoaming gas-liquid mixed phase feeding distributor is formed by integrating the following structures: the gas-liquid mixed phase feeding port (2) is of a tangential rectangular feeding structure and is communicated with the annular sleeve (3) in the tower body (1); the lower end of the annular sleeve (3) is provided with an opening, an annular grating filler (4) which is used for guiding speed reduction and strengthening the entrained vapor phase separation function is arranged 200-1500mm away from the lower end of the annular sleeve (3), the height is 50-100mm, the width is 0.3-2.5 times of the width of the annular sleeve (3), the plate spacing of the annular grating filler (4) is 3-50mm, and the horizontal inclination of the filler plate is 30-90 degrees; the middle part of the annular sleeve (3) is closed to form an annular oil collecting tank (5), the outer wall of the bottom of the annular oil collecting tank (5) is communicated with the lower part of the annular grid filler (4) through an external connecting pipe (7), or the inner wall of the annular grid filler is uniformly provided with tear holes with equivalent diameters of 5-30 mm; the upper end of the annular sleeve (3) is connected with a parallel flow packing layer (6) with steady flow defoaming self-washing function; the connecting lines of the inner edge and the outer edge of the parallel flow packing layer (6) are umbrella-shaped structures, the annular width of the packing layer is 3-500 times of the spacing of the packing plates, and the spacing of the packing plates is 1-30mm.
The ratio of the height to the width of the gas-liquid mixed phase feeding port (2) is 2-15:1, the ratio of the height of the gas-liquid mixed phase feeding port (2) to the height of the annular sleeve (3) in the tower body (1) is 1:1-10, and the ratio of the width of the gas-liquid mixed phase feeding port (2) to the width of the annular sleeve (3) in the tower body (1) is 1:1-1.5.
The annular cross section of the annular sleeve (3) in the tower body (1) accounts for 5-80% of the cross section of the tower, and the inner wall of the annular sleeve (3) is of a cylindrical or conical structure along the height direction.
The centrifugal cyclone defoaming type gas-liquid mixed phase feeding distributor provided by the invention reasonably utilizes the advantages of good gas-liquid two-phase separation and suitability for large-scale, small liquid volume of the annular oil collecting tank, timely and convenient downward discharge, high gas-liquid synclastic flow speed of the parallel flow filler, easy coalescence separation, guide deceleration of the annular grating filler and enhanced entrained vapor phase separation of the centrifugal cyclone, and reasonably integrates to form an integral effect, thereby not only realizing good gas-liquid two-phase separation effect, uniform distribution of vapor phases along the section of the tower, but also meeting the distribution requirement of the large-scale gas-liquid mixed phase feeding tower; the gas and liquid in the parallel flow filler flow obliquely downwards in the same direction, entrained liquid separated from the washing oil collecting tank can be kept at a low liquid level to be operated and can be timely discharged into a main liquid phase below the distributor, the liquid residence time is short, and the coking and blocking phenomena of the filler and the oil collecting tank are avoided; in addition, the annular space structure of the centrifugal cyclone and the umbrella-shaped structure of the parallel flow packing layer ensure that the steam flow passage area of the feeding distributor is more than 50 percent, and the pressure drop of the feeding distributor is less than 100Pa, which is important for feeding of the vacuum tower; in addition, the parallel flow packing steady flow defoaming self-washing simplifies the structure of the washing section, solves the selection difficulty of the liquid distributor of the washing section, and eliminates the maximum bottleneck which restricts the long-period safe operation of the washing section.
Claims (3)
1. The centrifugal rotational flow defoaming gas-liquid mixed phase feeding distributor is characterized in that a gas-liquid mixed phase feeding port is of a tangential rectangular feeding structure and is communicated with an annular sleeve in a tower; the lower end of the annular sleeve is provided with an opening, the distance from the lower end of the annular sleeve to 200-1500mm is provided with annular grid packing for guiding and decelerating and strengthening the vapor phase separation function, the height is 50-100mm, the width is 0.3-2.5 times of the width of the annular sleeve, the interval between packing plates is 3-50mm, and the horizontal inclination of the packing plates is 30-90 degrees; the middle part of the annular sleeve is sealed to form an annular oil collecting tank, the outer wall of the bottom of the annular oil collecting tank is communicated with the lower part of the annular grid filler through an external connecting pipe, or the inner wall of the annular oil collecting tank is uniformly provided with tear holes with equivalent diameters of 5-30 mm; the upper end of the annular sleeve is connected with a parallel flow packing layer with steady flow defoaming self-washing function; the connecting lines of the inner edge and the outer edge of the parallel flow packing layers are umbrella-shaped structures, the annular width of the packing layers is 3-500 times of the spacing of the packing plates, and the spacing of the packing plates is 1-30mm.
2. The centrifugal cyclone defoaming gas-liquid mixed phase feeding distributor according to claim 1, wherein the ratio of the height to the width of the gas-liquid mixed phase feeding port is 2-15:1, the ratio of the height of the gas-liquid mixed phase feeding port to the height of the annular sleeve in the tower is 1:1-10, and the ratio of the width of the gas-liquid mixed phase feeding port to the width of the annular sleeve in the tower is 1:1-1.5.
3. The centrifugal cyclone defoaming type gas-liquid mixed phase feeding distributor according to claim 1, wherein the annular cross section of the annular sleeve in the tower accounts for 5% -80% of the cross section of the tower, and the inner wall of the annular sleeve in the height direction is of a cylindrical or conical structure.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710171649.3A CN106693432B (en) | 2017-03-22 | 2017-03-22 | Centrifugal rotational flow defoaming type gas-liquid mixed phase feeding distributor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710171649.3A CN106693432B (en) | 2017-03-22 | 2017-03-22 | Centrifugal rotational flow defoaming type gas-liquid mixed phase feeding distributor |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN106693432A CN106693432A (en) | 2017-05-24 |
| CN106693432B true CN106693432B (en) | 2023-12-12 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201710171649.3A Active CN106693432B (en) | 2017-03-22 | 2017-03-22 | Centrifugal rotational flow defoaming type gas-liquid mixed phase feeding distributor |
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| Country | Link |
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| CN (1) | CN106693432B (en) |
Citations (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0132193A1 (en) * | 1983-07-18 | 1985-01-23 | Montedison S.p.A. | Falling-film apparatus for the equicurrent evaporation of a solution |
| CN2054370U (en) * | 1989-06-15 | 1990-03-14 | 天津大学 | Combined liquid distributing unit |
| CN1172699A (en) * | 1996-07-05 | 1998-02-11 | 艾里希普费弗工程师有限公司 | Dispensor for media |
| US6682633B1 (en) * | 2000-12-22 | 2004-01-27 | Uop Llc | Apparatus for cocurrent fractional distillation |
| TW587162B (en) * | 2001-05-29 | 2004-05-11 | Tecan Trading Ag | Device for processing samples, use of the device, and method for producing the device |
| WO2007139056A1 (en) * | 2006-06-01 | 2007-12-06 | Shimadzu Corporation | Dispensing tip, reaction kit using the same, and dispensing tip drive mechanism |
| CN204121795U (en) * | 2014-09-25 | 2015-01-28 | 中国石油化工股份有限公司 | A kind of novel packed tower suppressing gas fractionation unit to block liquid |
| CN104428665A (en) * | 2012-07-05 | 2015-03-18 | 安捷伦科技有限公司 | Single-piece with undercut tapering part |
| CA2974700A1 (en) * | 2015-01-23 | 2016-07-28 | Technip Process Technology, Inc. | Gas distributor for heat exchange and/or mass transfer column |
| CN206793075U (en) * | 2017-03-22 | 2017-12-26 | 中国石油大学(华东) | A kind of centrifugal cyclone foam removal type gas-liquid mixed phase feed distributor |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2003084630A1 (en) * | 2002-04-03 | 2003-10-16 | Koch-Glitsch, Lp | Method and apparatus for facilitating more uniform vapor distribution in mass transfer and heat exchange columns |
| US7802985B2 (en) * | 2007-10-25 | 2010-09-28 | Alan Cross | Direct fired heater utilizing particulates as a heat transfer medium |
-
2017
- 2017-03-22 CN CN201710171649.3A patent/CN106693432B/en active Active
Patent Citations (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0132193A1 (en) * | 1983-07-18 | 1985-01-23 | Montedison S.p.A. | Falling-film apparatus for the equicurrent evaporation of a solution |
| CN2054370U (en) * | 1989-06-15 | 1990-03-14 | 天津大学 | Combined liquid distributing unit |
| CN1172699A (en) * | 1996-07-05 | 1998-02-11 | 艾里希普费弗工程师有限公司 | Dispensor for media |
| US6682633B1 (en) * | 2000-12-22 | 2004-01-27 | Uop Llc | Apparatus for cocurrent fractional distillation |
| TW587162B (en) * | 2001-05-29 | 2004-05-11 | Tecan Trading Ag | Device for processing samples, use of the device, and method for producing the device |
| WO2007139056A1 (en) * | 2006-06-01 | 2007-12-06 | Shimadzu Corporation | Dispensing tip, reaction kit using the same, and dispensing tip drive mechanism |
| CN104428665A (en) * | 2012-07-05 | 2015-03-18 | 安捷伦科技有限公司 | Single-piece with undercut tapering part |
| CN204121795U (en) * | 2014-09-25 | 2015-01-28 | 中国石油化工股份有限公司 | A kind of novel packed tower suppressing gas fractionation unit to block liquid |
| CA2974700A1 (en) * | 2015-01-23 | 2016-07-28 | Technip Process Technology, Inc. | Gas distributor for heat exchange and/or mass transfer column |
| CN206793075U (en) * | 2017-03-22 | 2017-12-26 | 中国石油大学(华东) | A kind of centrifugal cyclone foam removal type gas-liquid mixed phase feed distributor |
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| Publication number | Publication date |
|---|---|
| CN106693432A (en) | 2017-05-24 |
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