CN103100291A - Gas-liquid mass transfer device - Google Patents
Gas-liquid mass transfer device Download PDFInfo
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- CN103100291A CN103100291A CN2013100534339A CN201310053433A CN103100291A CN 103100291 A CN103100291 A CN 103100291A CN 2013100534339 A CN2013100534339 A CN 2013100534339A CN 201310053433 A CN201310053433 A CN 201310053433A CN 103100291 A CN103100291 A CN 103100291A
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Abstract
Belonging to the field of gas-liquid mass transfer devices, the invention discloses a gas-liquid mass transfer device. The device comprises: a tower body, two or more mass transfer unit groups, an independent liquid collector and an independent liquid receiving disc. The top of the tower body is provided with a gas outlet and a liquid inlet, and the bottom is provided with a liquid outlet and a gas inlet. The independent liquid collector and the independent liquid receiving disc are positioned at the bottom of the tower body. Each mass transfer unit group consists of a liquid collector, a liquid receiving disc, a liquid distributor and a mass transfer area from top to bottom, and the mass transfer unit groups are in up-down arrangement inside the tower body. The bottom of each liquid receiving disc is provided with small holes. When the device operates, the gas-liquid two-phase flow direction shows overall counter-flow and local co-current flow, that is to say, a gas flows into the tower body from the bottom and flows out from the top, while a liquid flows into the tower body from the top and flows out from the bottom. And in each mass transfer area, the gas and the liquid are in top-down co-current contact for mass transfer. The special flow state combines respective advantages of counter-flow and co-current flow, a large mass transfer driving force and complete and stable gas-liquid contact can be realized simultaneously, the mass transfer rate can be improved, and the mass transfer effect can be ensured.
Description
Technical field
The present invention relates to a kind of gas-liquid mass transfer device, be specifically related to a kind of gas-liquid mass transfer device that comprises distillation, absorbs (or desorb) mass transport process, belong to gas-liquid mass transfer device field.
Background technology
The separation of homogeneous mixture is the significant process that chemical engineering industry is produced, and separates according to being based in system the difference of certain physical property between different component, make wherein certain component or some component from a phase transfer to another mutually to reach the purpose of separation.Distillation is the typical chemical engineering unit operation that realization separates with absorbing (or desorb).Although both are based on the separation process of different principle, the difference that is the distillation procedure volatility that is based on system is carried out, difference that (or desorb) operation is based on the solubility of system realizes and absorb, but the angle from gas-liquid mass transfer, distillation and absorption (or desorb) operation common ground in essence both arranged again, so can be carried out in same equipment.
Tower is the mass transfer apparatus of realizing distillation and absorbing (or desorb) operation.Be divided three classes according to the Gas-Liquid Contacting form.To be gas be dispersed in plate column, bubble tower in liquid phase with bubble shape to the first kind; Equations of The Second Kind is liquid with membranaceous packed tower and the falling-film tower that flows with the gas phase contact mass transfer; To be liquid be dispersed in spray tower, injector, Venturi tube in gas phase with droplet-like to the 3rd class.Wherein plate column and packed tower are the common equipments of realizing distillation and absorbing (or desorb) lock out operation.
The type of flow of the interior gas-liquid two-phase of tower can be adverse current and also can be and flow, and two kinds flow to each tool pluses and minuses.Under identical operating condition, the full tower absorption driving force of counter-current operation is even, and the average motive force of mass transfer is large, and separative efficiency is high, and the absorbent utilization rate is high, so the counter-current operations that adopt in Chemical Manufacture more.But during counter-current operation from top to bottom flowing liquid can be subject to the effect of the gas that upwards flows, cause entrainment and air-teturning mixed phenomenon, also can cause Concerning Flooding Phenomenon when serious, the degradation that causes mass-transfer efficiency, so can keep normal operating effect in order to guarantee tower, the flow of the gas-liquid two-phase during counter-current operation in tower is limited, and this has just limited the further raising of equipment capacity.And gas flows from top to bottom during cocurrent cooling operation, can eliminate the Concerning Flooding Phenomenon in counter-current operation, and entrainment and air-teturning mixed phenomenon also can obviously reduce, and have guaranteed mass transfer effect.In addition, during due to cocurrent cooling operation, gas speed is not subjected to the liquid flow restriction, so can improve the production capacity of equipment by improving operating gas velocity, reduces the equipment investment expense.In addition, pressure drop is one of important indicator of tower performance, and gas has determined the power consumption of tower by the size of the pressure drop of column plate or packing layer, and the pressure drop during the gas and liquid flowing operation is less, this just means that also cocurrent cooling operation is capable of reducing energy consumption, saves operating cost.
The exploitation of the optimization of conventional tower equipment and Novel tower equipment normally is based upon single two phase flow on the basis, even adverse current or and stream.And due to adverse current cocurrent cooling operation intrinsic defective separately, the further lifting of tower performance has been subject to the restriction that is difficult to go beyond.
Summary of the invention
The object of the present invention is to provide a kind of gas-liquid mass transfer device, described device combines adverse current and flows both advantages, can realize simultaneously larger mass transfer force and abundant stable gas-liquid contact, improves mass transfer rate, guarantees mass transfer effect.
Purpose of the present invention is realized by following technical scheme:
A kind of gas-liquid mass transfer device, described device comprises: tower body, two or more mass transfer unit groups, independent liquid trap and independent seal pot; The tower body top is provided with gaseous phase outlet and liquid phase import, and the bottom is provided with liquid-phase outlet and gas phase import; Independent liquid trap and independent seal pot are positioned at bottom tower body;
Described mass transfer unit group comprises liquid trap, seal pot, liquid distributor, mass-transfer zone from top to bottom, and the mass transfer unit group is arranged above and below in tower body inside; Liquid trap in the mass transfer unit group and seal pot are combined with the head height of setting, form fluid-tight when operation, the head height of fluid-tight is greater than the equivalent pressure loss reduced heal height of two mass-transfer zones, make gas phase can not pass through the fluid-tight of liquid trap and seal pot formation and form short circuit, guarantee the cocurrent cooling operation of realizing that mass-transfer zone is interior; Can unload the liquid of leaving with storage during in addition for equipment downtime, seal pot bottom has aperture;
Described mass-transfer zone is column plate, random packing or structured packing;
Described independent liquid trap is identical with liquid trap in the mass transfer unit group, and independent seal pot is identical with seal pot in the mass transfer unit group;
During operation, gas-liquid two-phase flows to and is overall adverse current, local also flowing, and namely gas phase enters from tower bottom flow, and tower top flows out, and liquid phase flows into from tower top, and tower bottom flow goes out, but in each mass-transfer zone, gas-liquid two-phase is all from top to bottom and flows contact mass transfer.
Beneficial effect
Device of the present invention is compared with absorption (or desorb) tower with traditional distillation, in tower, gas-liquid two-phase has formed a kind of special fluidised form, be that gas phase enters from tower bottom flow, tower top flows out, liquid phase flows into from tower top, tower bottom flow goes out, but in each mass-transfer zone, gas-liquid two-phase is all from top to bottom and flows contact mass transfer.This special fluidised form combines adverse current and flows both advantages, can realize simultaneously larger mass transfer force and abundant stable gas-liquid contact, improve mass transfer rate, reduce entrainment and back-mixing, eliminate Concerning Flooding Phenomenon, guarantee mass transfer effect, also for further production capacity and the reduction pressure loss of raising equipment provide new approaches and possibility.
Description of drawings
Fig. 1 is the schematic diagram of gas-liquid mass transfer device of the present invention;
Wherein, 1-tower body, 2-mass-transfer zone, 3-liquid distributor, 4-seal pot, 5-liquid trap, A-liquid phase import, B-gas phase import, C-liquid-phase outlet, D-gaseous phase outlet, hollow arrow represents liquid phase, filled arrows represents gas phase.
The specific embodiment
Below in conjunction with accompanying drawing in detail the present invention is described in detail, but is not limited to this.
As shown in Figure 1, a kind of gas-liquid mass transfer device, described device comprises: tower body 1, two or more mass transfer unit groups, independent liquid trap and independent seal pot; Tower body 1 top is provided with gaseous phase outlet D and liquid phase import A, and the bottom is provided with liquid-phase outlet C and gas phase import B; Independent liquid trap and independent seal pot are positioned at tower body 1 bottom;
Described mass transfer unit group comprises liquid trap 5, seal pot 4, liquid distributor 3, mass-transfer zone 2 from top to bottom, and the mass transfer unit group is arranged above and below in tower body 1 inside; Liquid trap 5 in the mass transfer unit group and seal pot 4 are combined with the head height of setting, form fluid-tight when operation, the head height of fluid-tight is greater than the equivalent pressure loss reduced heal height of two mass-transfer zones 2, make gas phase can not pass through the fluid-tight of liquid trap 5 and seal pot 4 formation and form short circuit, guarantee the cocurrent cooling operation of realizing that mass-transfer zone 2 is interior; Can unload the liquid of leaving with storage during in addition for equipment downtime, seal pot 4 bottoms have aperture;
Described mass-transfer zone 2 is column plate, random packing or structured packing;
Described independent liquid trap is identical with liquid trap 5 in the mass transfer unit group, and independent seal pot is identical with seal pot 4 in the mass transfer unit group;
The deionized water for the treatment of deoxygenation enters described gas-liquid mass transfer device from the liquid phase import A of tower top, air lift steam enters from the gas phase import B of described device bottom sidepiece, surmount below mass-transfer zone 2 along uprising gas passage fast rise when described bottom of device steam after, be subject to the stopping of fluid-tight of liquid trap 5 and seal pot 4, turn back rapidly, mix entering in the mass-transfer zone 2 of below with the liquid that descends from seal pot 4 overflows from top to bottom.When mass-transfer zone 2 adopted column plate, gas was because the pressure of self sprays from top to bottom at the tapping of column plate.Because the direction of gas ejection is consistent with liquid flow direction, then can eliminate the Concerning Flooding Phenomenon in counter-current operation, the kinetic energy that also can take full advantage of gas promotes the contact between gas-liquid two-phase, mass transfer enhancement, and gas is no longer bubbling by thicker liquid layer, so reduced plate pressure drop, reduced mist entrainment, improved mass transfer effect.When mass-transfer zone 2 adopts filler, the gas cocurrent flow descending in the fluid channel that liquid forms between the packing area of carrying under one's arms, and liquid is pulled into liquid film be distributed in filling surface, the contact area between gas-liquid two-phase increased thus, and reduced mist entrainment and pressure drop, eliminated liquid flooding.After gas-liquid mixture arrives mass-transfer zone 2 bottoms, below, because fluid-tight and the pressure in whole tower of bottom are controlled, gas-liquid two-phase will separate, liquid will continue descending, enter independent liquid trap and independent seal pot overflow at the bottom of the tower, then the liquid-phase outlet C from described bottom of device draws, gas turn back enter in gas passage up surmount top mass-transfer zone 2 after, be subject to stopping of liquid trap 5 and seal pot 4, again turn back, mix entering in the mass-transfer zone 2 of top with the liquid that descends from seal pot 4 overflows from top to bottom, carry out mass transfer next time.After gas-liquid mixture arrives mass-transfer zone 2 bottoms, top, because the pressure in fluid-tight and whole tower is controlled, gas-liquid two-phase will separate, liquid will continue descending, enter fluid-tight, then overflow is to below mass-transfer zone 2, and gas is again turned back and entered tower top by the uprising gas passage, then discharges from top gaseous phase outlet D.
In specific implementation process, the column plate in the structure of the quantity of mass-transfer zone 2, seal pot 4, liquid trap 5 and liquid distributor 3, mass-transfer zone 2 or the specification of filler and size all need to calculate according to actual conditions rear selected.
The present invention includes but be not limited to above embodiment, every any being equal to of carrying out under the principle of spirit of the present invention, replace or local improvement, all will be considered as within protection scope of the present invention.
Claims (2)
1. gas-liquid mass transfer device, it is characterized in that: described device comprises: tower body (1), two or more mass transfer unit groups, independent liquid trap and independent seal pot; Tower body (1) top is provided with gaseous phase outlet (D) and liquid phase import (A), and the bottom is provided with liquid-phase outlet (C) and gas phase import (B); Independent liquid trap and independent seal pot are positioned at bottom tower body (1);
Described mass transfer unit group comprises liquid trap (5), seal pot (4), liquid distributor (3), mass-transfer zone (2) from top to bottom, and the mass transfer unit group is arranged above and below in tower body (1) inside; Liquid trap in the mass transfer unit group (5) and seal pot (4) are combined with the head height of setting, form fluid-tight when operation, and the head height of fluid-tight is greater than the equivalent pressure loss reduced heal height of two mass-transfer zones (2); Seal pot (4) bottom has aperture;
During described device operation, gas-liquid two-phase flows to the also stream for overall adverse current, part, and namely gas phase enters from tower bottom flow, and tower top flows out, and liquid phase flows into from tower top, and tower bottom flow goes out; In each mass-transfer zone (2), gas-liquid two-phase is from top to bottom and flows contact mass transfer.
2. a kind of gas-liquid mass transfer device according to claim 1 is characterized in that: described mass-transfer zone (2) is column plate, random packing or structured packing.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2013100534339A CN103100291A (en) | 2013-02-19 | 2013-02-19 | Gas-liquid mass transfer device |
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| CN2013100534339A CN103100291A (en) | 2013-02-19 | 2013-02-19 | Gas-liquid mass transfer device |
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| CN103100291A true CN103100291A (en) | 2013-05-15 |
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104028008A (en) * | 2014-05-28 | 2014-09-10 | 天津佑华科技有限公司 | Multistage gas-liquid parallel flow devolatilization technology as well as devolatilization device |
| CN107569978A (en) * | 2017-08-31 | 2018-01-12 | 深圳市瑞升华科技股份有限公司 | A kind of indirect steam aeration tower for MVR systems |
| CN107890758A (en) * | 2017-11-09 | 2018-04-10 | 中海油天津化工研究设计院有限公司 | A kind of outer circulation type electrochemistry sewage treatment plant deodoration system and method |
| CN109589879A (en) * | 2018-12-29 | 2019-04-09 | 中国船舶重工集团公司第七八研究所 | A kind of gas-liquid mass transfer device |
| CN114684988A (en) * | 2022-03-04 | 2022-07-01 | 信丰华锐钨钼新材料有限公司 | High-efficiency resource utilization method for high-concentration ammonia nitrogen wastewater containing carbonate |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB2145012A (en) * | 1983-08-16 | 1985-03-20 | Shell Int Research | Gas/liquid contact apparatus |
| CN1378872A (en) * | 2002-01-25 | 2002-11-13 | 蓝仁水 | Tower plate for gas baffling |
| CN1402647A (en) * | 1999-10-07 | 2003-03-12 | 苏舍化学技术美国有限公司 | Vapor-liquid contact apparatus |
| EP1923119A1 (en) * | 2006-10-23 | 2008-05-21 | Frans Verdroncken | Apparatus and method for the purification of a gas stream containing solid or liquid particles. |
| JP2011183259A (en) * | 2010-03-05 | 2011-09-22 | Tadayoshi Nagaoka | Gas-liquid contact mechanism in apparatus for performing mass transfer or the like |
-
2013
- 2013-02-19 CN CN2013100534339A patent/CN103100291A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB2145012A (en) * | 1983-08-16 | 1985-03-20 | Shell Int Research | Gas/liquid contact apparatus |
| CN1402647A (en) * | 1999-10-07 | 2003-03-12 | 苏舍化学技术美国有限公司 | Vapor-liquid contact apparatus |
| CN1378872A (en) * | 2002-01-25 | 2002-11-13 | 蓝仁水 | Tower plate for gas baffling |
| EP1923119A1 (en) * | 2006-10-23 | 2008-05-21 | Frans Verdroncken | Apparatus and method for the purification of a gas stream containing solid or liquid particles. |
| JP2011183259A (en) * | 2010-03-05 | 2011-09-22 | Tadayoshi Nagaoka | Gas-liquid contact mechanism in apparatus for performing mass transfer or the like |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104028008A (en) * | 2014-05-28 | 2014-09-10 | 天津佑华科技有限公司 | Multistage gas-liquid parallel flow devolatilization technology as well as devolatilization device |
| CN107569978A (en) * | 2017-08-31 | 2018-01-12 | 深圳市瑞升华科技股份有限公司 | A kind of indirect steam aeration tower for MVR systems |
| CN107890758A (en) * | 2017-11-09 | 2018-04-10 | 中海油天津化工研究设计院有限公司 | A kind of outer circulation type electrochemistry sewage treatment plant deodoration system and method |
| CN107890758B (en) * | 2017-11-09 | 2020-11-24 | 中海油天津化工研究设计院有限公司 | External circulation type electrochemical sewage treatment plant deodorization system and method |
| CN109589879A (en) * | 2018-12-29 | 2019-04-09 | 中国船舶重工集团公司第七八研究所 | A kind of gas-liquid mass transfer device |
| CN114684988A (en) * | 2022-03-04 | 2022-07-01 | 信丰华锐钨钼新材料有限公司 | High-efficiency resource utilization method for high-concentration ammonia nitrogen wastewater containing carbonate |
| CN114684988B (en) * | 2022-03-04 | 2024-01-02 | 信丰华锐钨钼新材料有限公司 | Efficient recycling method for high-concentration ammonia nitrogen wastewater containing carbonate |
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Application publication date: 20130515 |