CN113413731A - Gas-liquid contact device - Google Patents
Gas-liquid contact device Download PDFInfo
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- CN113413731A CN113413731A CN202110716300.XA CN202110716300A CN113413731A CN 113413731 A CN113413731 A CN 113413731A CN 202110716300 A CN202110716300 A CN 202110716300A CN 113413731 A CN113413731 A CN 113413731A
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/18—Absorbing units; Liquid distributors therefor
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D1/00—Evaporating
- B01D1/0011—Heating features
- B01D1/0041—Use of fluids
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D1/00—Evaporating
- B01D1/14—Evaporating with heated gases or vapours or liquids in contact with the liquid
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D1/00—Evaporating
- B01D1/30—Accessories for evaporators ; Constructional details thereof
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- 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
- B01D3/16—Fractionating columns in which vapour bubbles through liquid
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1456—Removing acid components
- B01D53/1481—Removing sulfur dioxide or sulfur trioxide
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/048—Purification of waste water by evaporation
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/16—Nitrogen compounds, e.g. ammonia
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/34—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32
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- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Organic Chemistry (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The invention relates to a device for heat and mass transfer by gas-liquid contact, wherein a liquid film is formed by an inclined plate provided with fluid circulation holes, and gas passes through the liquid film to promote the gas-liquid high-efficiency contact; through the liquid circulation channel arranged between the component units, the smooth descending of liquid is realized, and the blockage is prevented; the baffle plate of the liquid circulation channel is reserved at the lower part of the liquid circulation channel arranged between the component units, so that the liquid flow is controlled to flow straight down, the liquid forms a liquid holding layer, the flow direction of the liquid is changed, the circulation time is prolonged, the gas-liquid contact time is prolonged, smooth descending of the liquid can be realized, the blockage is prevented, and the device investment with high efficiency and low heat and mass transfer efficiency is realized.
Description
Technical Field
The invention relates to a device for heat and mass transfer by gas-liquid contact, in particular to a device for heat and mass transfer by gas-liquid contact, which can carry out high-efficiency and low-resistance gas-liquid heat and mass transfer, realize liquid-phase component separation or gas absorption and prevent blockage under the conditions of liquid-phase component separation, gas-liquid absorption or gas cooling, and belongs to the field of chemical process equipment and environmental management.
Background
In the fields of chemical engineering and environmental management, there are many unit operations for separating liquid phase components or absorbing gas and liquid by applying gas-liquid contact such as distillation, gas absorption or gas cooling, etc., and these unit operations require the places for heat and mass transfer between gas and liquid by gas-liquid contact devices such as distillation tower or absorption tower, etc. The gas-liquid contact device not only needs to have high-efficiency gas-liquid mass transfer efficiency and small gas phase resistance, but also needs to be anti-blocked, and has simple structure and low investment cost. Therefore, the performance of the gas-liquid contacting device directly affects the efficiency of gas-liquid heat and mass transfer and the operational stability. Hitherto, the internal components such as sieve plate tower, bubble cap tower and packed tower are widely used in industry, and the components are respectively suitable for different process requirements to obtain good effects. However, it is difficult to satisfy the industrial demand completely in terms of compatibility such as separation performance, clogging prevention, and investment cost. The invention provides a gas-liquid contact device which is high in mass transfer efficiency, simple in structure and anti-blocking, and provides a novel contact device for industrial gas-liquid heat and mass transfer.
Disclosure of Invention
The invention aims to provide equipment which can increase the gas-liquid contact area, improve the heat and mass transfer efficiency, avoid impurities in a solution from blocking a device and save energy and cost. A liquid film is formed by the inclined plate with fluid flowing holes, and gas passes through the liquid film to promote the efficient contact of gas and liquid; through the liquid circulation channel arranged between the inner component units, the smooth descending of liquid is realized, and the blockage is prevented; the transverse baffle plate of the liquid circulation channel is reserved at the lower part of the liquid circulation channel arranged between the component units, so that the liquid is controlled to flow straight down, a liquid holding layer is formed by the liquid, the flow direction of the liquid is changed, the circulation time is prolonged, the gas-liquid contact time is prolonged, the smooth downward movement of the liquid can be realized, and the blockage is prevented; the inner component layers are arranged in a multilayer mode in the vertical direction of the device, the component layers are not in direct contact in the vertical direction, and exchange of a gas-liquid flow field is formed to promote gas-liquid contact. The equipment has simple structure, high heat and mass transfer efficiency and low investment cost.
The invention is realized by adopting the following scheme:
a gas-liquid contact device is characterized in that in the flow path of gas from bottom to top and liquid from top to bottom, an inner member unit consisting of two side panels is arranged, the lower part of the inner member unit is provided with an opening, the upper part of the inner member unit is closed, the side panels are provided with pores with any shapes, and fluid can pass through the pores; the included angle between the side panel of the inner member unit and the horizontal plane is 45-85 degrees; the inner member units are arranged in parallel in the horizontal plane to form an inner member layer, and liquid flow channels are reserved between the inner member units in the inner member layer.
The device is characterized in that a liquid flow channel reserved between the inner member units is of a fluid deflection type, a transverse baffle is arranged below a space between the inner member units, and a gap is reserved between the transverse baffle and the inner member units.
The device is characterized in that the inner member layers are arranged in a plurality of layers in the vertical direction of the device, the inner member layers are not in direct contact in the vertical direction, and the symmetry axes of the inner member units among the layers are on the same straight line.
The device is characterized in that a liquid flow channel reserved between the inner component units is of a liquid direct type; the inner member layers are arranged in a plurality of layers in the vertical direction of the device, and the inner member layers are not in direct contact in the vertical direction; the middle line of the liquid circulation channel between the internal component units of the upper layer is in the same straight line with the symmetry axis of the internal component units of the lower layer.
The concrete description is as follows:
in the flow path of gas from bottom to top and liquid from top to bottom, the liquid flows from top to bottom from the outer wall of a side panel with a lower opening and an upper closed part to form a thin-layer liquid film, the side panel is provided with pores in any shape to form a fluid channel, and the side panel is obliquely arranged and forms an angle of 45-85 degrees with the horizontal plane; the gas enters the inner member unit from the lower part, then passes through the side pores and breaks the liquid film to leave the inner member unit, and the gas and the liquid film are in gas-liquid contact in the process to carry out heat and mass transfer. Because the liquid film layer is thin, the resistance of gas passing through the liquid film is small, and the gas passing through the liquid film has transverse component force, so that the liquid film is easily flushed to the momentum direction of the gas flow in a liquid drop mode, the liquid is changed into dispersed liquid drops, the contact surface and the contact time of gas-liquid mass transfer are greatly increased, and the heat and mass transfer effect is greatly improved. The included angle between the side panel of the inner member unit and the horizontal plane is 45-85 degrees, the side panel is provided with a pore with any shape, and the side panel can flow fluid, and different air flow and mass transfer load can be optimized according to the inclination angle and the pore of the side panel. The inner component units are arranged in parallel in the horizontal plane direction to form an inner component layer, liquid circulation channels are reserved among the component units in the inner component layer, the inner component units can be arranged in the inner component layer through different treatment amounts, the liquid circulation channels arranged among the inner component units can guarantee the smoothness of downward flow of liquid, and impurities in the liquid, particularly tar and the like in residual ammonia water in the coal chemical industry and the like, can be prevented from being blocked.
The liquid flow passage between the inner member units is provided in a fluid deflection type, and a transverse baffle plate is provided below the space between the inner member units, and a gap is left between the transverse baffle plate and the inner member units. Therefore, the liquid has the effect similar to liquid seal, the siphoning is prevented from being formed along with the downward flow of the liquid, the mat-rolling gas flows downwards to form mixed flow, and the gas-liquid heat and mass transfer effects are reduced; and liquid can be guided to the gas ascending channel to increase the gas-liquid contact chance and promote the gas-liquid heat and mass transfer. The gap between the transverse baffle and the inner member unit is determined according to the gas-liquid load.
The inner component layers are arranged in a multilayer mode in the vertical direction of the device, and the component layers are not in direct contact in the vertical direction, so that a gas-liquid separation space is formed, liquid flooding is prevented, and gas-liquid redistribution among all layers is realized to improve heat and mass transfer efficiency. The symmetrical axes of the interlayer internals units are on the same straight line, so that the upper layer liquid falls to the tops of the lower layer internals units under the action of the transverse baffles, a better liquid film arrangement is formed, and the heat and mass transfer effects of the internals are greatly improved.
The liquid flow channels left between the inner component units are of a liquid direct type, the inner component layers are arranged in a plurality of layers in the vertical direction of the device, the component layers are not directly contacted in the vertical direction, and the middle line of the liquid flow channels between the inner component units in the previous layer is in the same straight line with the symmetry axis of the inner component units in the next layer (as shown in figure 2). The liquid direct-downward channels are arranged among the inner member units, the inner member layer without the transverse baffle is more suitable for the condition that solid bonding substances exist in liquid, and under the condition, the middle line of the liquid circulation channel between the upper layer of inner member units and the symmetrical axis of the lower layer of inner member units are on the same straight line, so that the upper layer of liquid falls to the top of the lower layer of inner member, better liquid film arrangement is formed, and the heat and mass transfer effects of the inner member are greatly improved.
The invention has the advantages that the invention provides the equipment which can increase the gas-liquid contact area, improve the heat and mass transfer efficiency, avoid the impurity in the solution from blocking the device and save the energy and the cost; liquid film gas is formed to penetrate through the liquid film through the inclined side panel with the fluid circulation holes, and efficient contact of the gas and the liquid is promoted; through the liquid circulation channel arranged between the component units, the smooth descending of liquid is realized, and the blockage is prevented; the transverse baffle plate of the liquid circulation channel is reserved at the lower part of the liquid circulation channel arranged between the component units, so that the liquid is controlled to flow straight down, a liquid holding layer is formed by the liquid, the flow direction of the liquid is changed, the circulation time is prolonged, the gas-liquid contact time is prolonged, the smooth downward movement of the liquid can be realized, and the blockage is prevented; the inner component layers are arranged in a multilayer mode in the vertical direction of the device, the component layers are not in direct contact in the vertical direction, and exchange of a gas-liquid flow field is formed to promote gas-liquid contact. The equipment has simple structure, high heat and mass transfer efficiency and low investment cost.
Drawings
FIG. 1: a schematic diagram of a gas-liquid contact device with transverse baffles arranged between the inner member units;
FIG. 2: a schematic view of a gas-liquid contact device without transverse baffles between inner member units.
Wherein: 1-mass transfer tower, 2-mass transfer inner member side panel, 3-mass transfer inner member top, 4-mass transfer inner member lower gas inlet, 5-mass transfer inner member side panel pore, 6-mass transfer inner member unit liquid transverse baffle, 7-mass transfer inner member side panel bottom and liquid transverse baffle gap, 8-mass transfer inner member unit liquid flow channel, 9-mass transfer inner member unit symmetry axis, 10-liquid, 11-gas, 12-mass transfer inner member unit liquid flow channel middle line, beta-inner member unit side panel and horizontal plane included angle.
Detailed Description
Example 1:
the embodiment is an application example of a device for an ammonia distillation process of ammonia-containing wastewater in the coking industry, and is shown in figure 1. The ammonia-containing wastewater (liquid 10) flows from top to bottom in the ammonia still (mass transfer tower 1) and forms a liquid film (not marked in the figure) along the side panel 2 of the mass transfer inner member, and the ammonia still steam (gas 11) moves from bottom to top in the ammonia still and enters the inside of the mass transfer inner member from the gas inlet 4 at the lower part of the mass transfer inner member. Because the top 3 of the mass transfer inner member is a sealed structure, the mass transfer inner member can only penetrate through the side panel pores 5 of the mass transfer inner member arranged on the side panel 2 of the mass transfer inner member to further break a liquid film formed on the side panel, gas and liquid are in good contact to carry out heat transfer and mass transfer, and ammonia in the liquid is volatilized and transferred into steam, so that the aim of removing the ammonia in the wastewater is fulfilled. The side panels of the inner element unit are at an angle beta of 65 deg. to the horizontal.
Liquid flowing down from the side panel 2 of the mass transfer inner member enters a liquid flow channel 7 between the mass transfer inner member units, passes through a gap 8 between the bottom of the side panel of the mass transfer inner member and a liquid baffle, which is formed by the bottom of the side panel 2 of the mass transfer inner member and a liquid transverse baffle 6 between the mass transfer inner member units, and flows to the lower mass transfer inner member layer for further ammonia distillation; the steam further enters the upper mass transfer inner component layer to realize the ammonia distillation process.
The two side panels 2 of the mass transfer inner member form a mass transfer inner member unit, the symmetrical axis 9 of the mass transfer inner member unit determines the installation position, the symmetrical axes of the mass transfer inner member units of the upper layer and the lower layer are on the same line, so that liquid can fall to the top area of the lower layer inner member unit after passing through the liquid baffle 6 between the mass transfer inner member units, and the liquid of the lower layer can be well distributed on the inner member layer panels, thereby realizing high-efficiency gas-liquid heat and mass transfer. Therefore, liquid and steam realize good gas-liquid contact, and the liquid forms a good water sealing effect under the action of the transverse liquid baffle plate between the mass transfer inner member units, so that the steam is prevented from directly passing through the liquid flow channel 7 between the mass transfer inner member units to flow upwards to form a short circuit. And the gap 8 between the bottom of the side panel of the mass transfer inner member and the liquid baffle can not be blocked by tar and the like under the reasonable design.
Through the ammonia distillation of this device can realize efficient ammonia distillation, stable operation, equipment structure is simple, and the cost is low.
Example 2
This embodiment is an example of the apparatus application of the gas absorption process, as shown in fig. 2. The desulfurization absorption liquid (liquid 10) flows from top to bottom in the absorption tower (mass transfer tower 1) and forms a liquid film (not shown in the figure) along the side panel 2 of the mass transfer inner member, and the liquid film contains S42Waste gas (gas 11) moves from bottom to top in the absorption tower and enters the interior of the mass transfer inner member from a gas inlet 4 at the lower part of the mass transfer inner member. Because the top 3 of the mass transfer inner member is a sealed structure, the gas-liquid separator can only penetrate through the side plate pores 5 of the mass transfer inner member arranged on the side plate 2 of the mass transfer inner member to further break a liquid film formed on the side plate, and the gas and the liquid are in good contact with each other to perform heat transfer and mass transfer to remove SO in the waste gas2Dissolving and transferring into absorption liquid to remove SO in waste gas2The purpose of (1).
Liquid flowing down from the side panel 2 of the mass transfer inner member enters a liquid flow channel 7 between the mass transfer inner member units and flows to the lower mass transfer inner member layer for further absorption; the waste gas further enters the upper mass transfer inner component layer to realize the gas absorption and purification process.
Two side panels 2 of the mass transfer inner member form mass transfer inner member units, the middle line 12 of a liquid flow channel between the upper layer inner member units and the symmetrical axis 9 of the lower layer inner member units are on the same straight line, the top 3 of the lower layer mass transfer inner member unit is positioned right below the liquid flow channel 7 between the upper layer mass transfer inner member units, so that liquid can fall to the top area of the lower layer inner member units after passing through the liquid flow channel 7 between the mass transfer inner member units, the lower layer liquid can be well distributed on the inner member layer panels, and high-efficiency gas-liquid heat transfer mass transfer is realized. Therefore, the absorption liquid and the waste gas are in good gas-liquid contact. Because solid particles exist in the absorption liquid and are easy to scale and block, the structure without the transverse liquid baffle among the mass transfer inner member units can better avoid the precipitation of scaling substances on a plane, and is favorable for preventing blocking. In order to prevent the liquid flow channel 7 between the gas mass transfer inner member units from directly rising to form a short circuit, the distance between the upper layer and the lower layer can be shortened, and the top 3 of the lower mass transfer inner member unit can form a suspected liquid seal effect on liquid to form a certain water seal effect. The side panels of the inner element unit are at an angle beta of 85 deg. to the horizontal.
The gas absorption through this device can realize efficient exhaust purification, stable operation, and equipment structure is simple, and the cost is low.
Example 3
The embodiment is also an application example of the ammonia distillation process of ammonia-containing wastewater in the coking industry, and adopts an ammonia distillation tower with the structure shown in figure 2, and the included angle beta between the side panel of the inner member unit and the horizontal plane is 45 degrees.
Example 4
The embodiment is an application example of a device for a process for absorbing and recovering dissolved volatile gas in the chemical industry, and adopts an absorption tower with the structure shown in fig. 1, and an included angle beta between a side panel of an inner member unit and a horizontal plane is 72 degrees.
Claims (4)
1. A gas-liquid contact device is characterized in that in the flow path of gas from bottom to top and liquid from top to bottom, an inner member unit consisting of two side panels is arranged, the lower part of the inner member unit is provided with an opening, the upper part of the inner member unit is closed, the side panels are provided with pores with any shapes, and fluid can pass through the pores; the included angle between the side panel of the inner member unit and the horizontal plane is 45-85 degrees; the inner member units are arranged in parallel in the horizontal plane to form an inner member layer, and liquid flow channels are reserved between the inner member units in the inner member layer.
2. The apparatus of claim 1, wherein the fluid communication channel defined between the inner structural units is of a fluid baffle type, and wherein a transverse baffle is disposed below the space defined between the inner structural units, the transverse baffle being spaced from the inner structural units.
3. The device of claim 2, wherein the inner member layers are arranged in a plurality of layers in a vertical direction of the device, the inner member layers are not in direct contact in the vertical direction, and the symmetry axes of the inner member units in the layers are aligned.
4. The apparatus of claim 1, wherein the fluid communication path between the inner member units is of a liquid-down type; the inner member layers are arranged in a plurality of layers in the vertical direction of the device, and the inner member layers are not in direct contact in the vertical direction; the middle line of the liquid circulation channel between the internal component units of the upper layer is in the same straight line with the symmetry axis of the internal component units of the lower layer.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202110716300.XA CN113413731B (en) | 2021-06-28 | 2021-06-28 | Gas-liquid contact device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202110716300.XA CN113413731B (en) | 2021-06-28 | 2021-06-28 | Gas-liquid contact device |
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| Publication Number | Publication Date |
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| CN113413731A true CN113413731A (en) | 2021-09-21 |
| CN113413731B CN113413731B (en) | 2022-11-01 |
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| CN202110716300.XA Active CN113413731B (en) | 2021-06-28 | 2021-06-28 | Gas-liquid contact device |
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Citations (8)
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| KR20100115291A (en) * | 2009-04-17 | 2010-10-27 | 사다오 시노하라 | A seperating disc type centrifugal seperator, and seperating disc for the centrifugal seperator, and a seperating method of the solid and liquid |
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| CN202410502U (en) * | 2011-12-22 | 2012-09-05 | 福建省亿利达环保工程有限公司 | Automatic gas and liquid mixed gas-impact spray desulfurizing and dedusting tower |
| US20150085600A1 (en) * | 2011-08-10 | 2015-03-26 | Albert Van Duijn | Apparatus and Method for Contacting a Gas and a Liquid |
| CN205517227U (en) * | 2016-01-26 | 2016-08-31 | 中钢集团武汉安全环保研究院有限公司 | Desulfurizing tower suitable for ultra -clean discharges |
| CN209865339U (en) * | 2019-03-01 | 2019-12-31 | 盘锦百事达新材料有限公司 | Chemical industry distillation column liquid collecting device |
-
2021
- 2021-06-28 CN CN202110716300.XA patent/CN113413731B/en active Active
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2001046802A (en) * | 1999-06-03 | 2001-02-20 | Nippon Shokubai Co Ltd | Method and apparatus for refining of organic compound containing easily blockable substance |
| KR20100115291A (en) * | 2009-04-17 | 2010-10-27 | 사다오 시노하라 | A seperating disc type centrifugal seperator, and seperating disc for the centrifugal seperator, and a seperating method of the solid and liquid |
| CN101721828A (en) * | 2010-01-15 | 2010-06-09 | 天津大学 | Liquid guide flow type vertical sieve tray device |
| CN202173849U (en) * | 2011-07-26 | 2012-03-28 | 杭州潜阳科技有限公司 | Gas-liquid separator |
| US20150085600A1 (en) * | 2011-08-10 | 2015-03-26 | Albert Van Duijn | Apparatus and Method for Contacting a Gas and a Liquid |
| CN202410502U (en) * | 2011-12-22 | 2012-09-05 | 福建省亿利达环保工程有限公司 | Automatic gas and liquid mixed gas-impact spray desulfurizing and dedusting tower |
| CN205517227U (en) * | 2016-01-26 | 2016-08-31 | 中钢集团武汉安全环保研究院有限公司 | Desulfurizing tower suitable for ultra -clean discharges |
| CN209865339U (en) * | 2019-03-01 | 2019-12-31 | 盘锦百事达新材料有限公司 | Chemical industry distillation column liquid collecting device |
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| CN113413731B (en) | 2022-11-01 |
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