CN1256999C - Extraction method and apparatus of a bubbling sieve plate tower - Google Patents
Extraction method and apparatus of a bubbling sieve plate tower Download PDFInfo
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- CN1256999C CN1256999C CN 03105346 CN03105346A CN1256999C CN 1256999 C CN1256999 C CN 1256999C CN 03105346 CN03105346 CN 03105346 CN 03105346 A CN03105346 A CN 03105346A CN 1256999 C CN1256999 C CN 1256999C
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- tower
- phase liquid
- gas
- bubbling
- sieve
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- 238000000605 extraction Methods 0.000 title claims abstract description 46
- 230000005587 bubbling Effects 0.000 title claims abstract description 40
- 239000007788 liquid Substances 0.000 claims abstract description 87
- 238000000034 method Methods 0.000 claims abstract description 23
- 230000004907 flux Effects 0.000 claims abstract description 15
- 239000007789 gas Substances 0.000 claims description 61
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 6
- 239000011261 inert gas Substances 0.000 claims description 5
- 229910052757 nitrogen Inorganic materials 0.000 claims description 3
- 238000012856 packing Methods 0.000 abstract description 7
- 238000012546 transfer Methods 0.000 abstract description 7
- 230000002708 enhancing effect Effects 0.000 abstract 1
- 230000002349 favourable effect Effects 0.000 abstract 1
- 239000012071 phase Substances 0.000 description 52
- WPYMKLBDIGXBTP-UHFFFAOYSA-N benzoic acid group Chemical group C(C1=CC=CC=C1)(=O)O WPYMKLBDIGXBTP-UHFFFAOYSA-N 0.000 description 24
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 18
- 230000008676 import Effects 0.000 description 17
- 239000003350 kerosene Substances 0.000 description 13
- 239000005711 Benzoic acid Substances 0.000 description 11
- 235000010233 benzoic acid Nutrition 0.000 description 11
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 description 9
- FUZZWVXGSFPDMH-UHFFFAOYSA-N hexanoic acid Chemical compound CCCCCC(O)=O FUZZWVXGSFPDMH-UHFFFAOYSA-N 0.000 description 8
- 238000000926 separation method Methods 0.000 description 8
- DKPFZGUDAPQIHT-UHFFFAOYSA-N Butyl acetate Natural products CCCCOC(C)=O DKPFZGUDAPQIHT-UHFFFAOYSA-N 0.000 description 7
- 241000282326 Felis catus Species 0.000 description 7
- 238000005516 engineering process Methods 0.000 description 4
- 239000003595 mist Substances 0.000 description 4
- 238000013461 design Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000002360 explosive Substances 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 230000000630 rising effect Effects 0.000 description 2
- 238000003756 stirring Methods 0.000 description 2
- QTBSBXVTEAMEQO-UHFFFAOYSA-M Acetate Chemical compound CC([O-])=O QTBSBXVTEAMEQO-UHFFFAOYSA-M 0.000 description 1
- 229910000831 Steel Inorganic materials 0.000 description 1
- 230000002950 deficient Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 238000009854 hydrometallurgy Methods 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 238000009527 percussion Methods 0.000 description 1
- 238000005191 phase separation Methods 0.000 description 1
- 230000035939 shock Effects 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
Landscapes
- Gas Separation By Absorption (AREA)
- Extraction Or Liquid Replacement (AREA)
- Physical Or Chemical Processes And Apparatus (AREA)
Abstract
The present invention relates to an extraction method of a bubbling sieve-plate tower and a device thereof. The extraction method comprises that heavy phase liquid flows in a tower from the upper part and flows out of the tower from the bottom part through a plurality of pieces of sieve plates; light phase liquid flows in the tower from the bottom part, and flows out of the tower from the upper part through a plurality of pieces of sieve plates; gas enters the bottom of each extraction tower uniformly through the distributors arranged on the bottom of the tower, and flows out of the tower from the upper part after passing through the sieve plates. The device comprises a light phase liquid inlet, a gas inlet, a heavy phase liquid outlet, a light phase liquid outlet, a heave phase liquid inlet, a gas outlet, a gas distributor, sieve plates, a packing layer and a defogging facility, wherein the light phase liquid inlet, the gas inlet and the heavy phase liquid outlet are arranged on the bottom part of the tower; the a light phase liquid outlet, the heave phase liquid inlet and the gas outlet are arranged on the upper part of the tower; the gas distributor, the sieve plates, the packing layer and the defogging facility are arranged inside the chamber of the tower. The extraction method of the bubbling sieve-plate tower achieves the aims of enhancing the contact and the mass transfer of the liquid-liquid two-phase liquid, and prompts the two-phase liquid to swimmingly pass through screen meshes to substantially raise work efficiency and processing capacity of the extraction towers. The device of the present invention has the advantages of large flux, high efficiency, simple implementation method and good operating flexibility, and particularly has favorable anti-blocking performance when a griddle plate is adopted; besides, the present invention is suitable for various normal-pressure extraction systems, middle-pressure extraction systems and high-pressure extraction.
Description
Technical field
The present invention relates to the method for production processes such as petrochemical industry, hydrometallurgy, atomic energy chemical industry, particularly a kind of bubbling sieve-plate tower extracting process and equipment thereof of in perforated-plate extraction tower, introducing gas bubbling technology.
Background technology
Industrial, abstraction technique has obtained extensively usefulness, and the performance of extraction equipment directly has influence on the energy consumption of production process and economic benefit etc.The disposal ability of extraction equipment and device efficiency are to weigh two most important indexs of equipment performance, and the two often is difficult to take into account.Such as, device efficiency height such as pulsed packed tower, pulsed perforated-plate tower, but flux is little, has limited its range of application; Vibrating sieve plate tower is used widely with its outstanding high flux, high efficiency.But owing to have mechanical shock and mechanical wear in the vibrating sieve plate tower, mechanical strength there is specific (special) requirements, has also brought difficulty simultaneously to device maximization design and maintenance.
Summary of the invention
The objective of the invention is to overcome the defective of prior art and a kind of perforated-plate extraction tower that utilizes is provided, adopt gas bubbling technology from bottom to top, the contact and the mass transfer of one side forced fluid-liquid two-phase, increase substantially extraction process efficient, utilize on the other hand to drive light phase liquid in the gas uphill process, enlarge markedly the bubbling sieve-plate tower extracting process of the disposal ability of perforated-plate extraction tower smoothly by sieve aperture.
Another object of the present invention provides a kind of above-mentioned bubbling sieve-plate tower extracting process device therefor.
Bubbling sieve-plate tower extracting process of the present invention comprises: in the bubbling perforated-plate extraction tower, heavy-phase liquid is flowed into from the top of tower, flow out through the below from tower behind the some sieve plates; Light phase liquid flows into from the below of tower, flows out through the top from tower behind the some sieve plates; Make gas at the bottom of tower, enter the bubbling perforated-plate extraction tower, enter bubbling perforated-plate extraction tower bottom equably, flow out through the top from tower behind the some sieve plates by distributor with the empty tower gas velocity of 0.5～80mm/s.In the process that gas rises rapidly, on the one hand liquid layer is carried out intense impact and stirring in tower, and make dispersed phase drop constantly broken, the surface is brought in constant renewal in, and strengthens the contact and the mass transfer of two-phase, significantly improves the extraction process mass-transfer efficiency; Utilize the rising percussion of gas on the other hand, drive light phase liquid and overcome surface tension effects, make it pass sieve aperture smoothly, thereby enlarge markedly the disposal ability of bubbling perforated-plate extraction tower.
Wherein, described gas can be air or inert gas.Described inert gas is preferably nitrogen.Promptly, can use air to make bubbled gas to non-inflammable and explosive system; To inflammable and explosive system, should use inert gases such as nitrogen.
The density of described light phase liquid should be 30～95% of heavy-phase liquid density.
Described heavy-phase liquid is 10～100m with the light total flux of liquid mutually
3/ m
2H.
Bubbling sieve-plate tower extracting process device therefor of the present invention is the bubbling perforated-plate extraction tower, and it comprises tower body, and the tower body bottom is provided with the import of light phase liquid, and tower body top is provided with light phase liquid outlet; Below light phase liquid outlet, be provided with the heavy-phase liquid import, be provided with the heavy-phase liquid outlet in the tower body bottom; Also be provided with gas feed in the tower body bottom, and link to each other with gas feed be located at gas distributor in the tower, be provided with gas vent at cat head; Be provided with some sieve plates in the tower between gas distributor and heavy-phase liquid import; Also be provided with packing layer in the tower between light phase liquid outlet and heavy-phase liquid import.
Bubbling sieve-plate tower extracting process device therefor of the present invention can also comprise that the light phase liquid import of described tower body bottom and gas feed are same import, and is provided with the liquid distribution trough that is attached thereto in tower.During extraction, earlier gas is mixed with light liquid mutually before tower,, enter the extraction tower bottom equably from the tower bottom through light phase liquid distribution trough together then through same inlet.Described liquid distribution trough can be the calandria liquid distribution trough.
Bubbling sieve-plate tower extracting process device therefor of the present invention can also comprise when gas speed hour, reserve the gas-liquid separation space of 0.05-0.5m height at cat head, can realize gas-liquid separation; This is that the liquid that gas is taken away from cat head is considerably less because used gas speed is less, does not generally need to dispose special drop recvery facility.
When gas phase is carried secretly seriously, establish a demist facility that is used to catch, reclaim light phase drop in the tower between described light phase liquid outlet and described gas vent, grind the mesh mist eliminator of metal packing associating process plants as Beijing steel,, reduce liquid entrainment to impel gas-liquid separation.Described demist facility height is 0.05～0.5m.
Wherein, the distance between plates of described sieve plate can be 20～500mm; Allow to exist the gap of 0～3mm between described column plate periphery and the tower wall, but its gap is the smaller the better.
Described sieve plate can comprise the sieve plate of no downspout and the sieve plate of band downspout.The sieve diameter of the sieve plate of described no downspout is φ 6～20mm, and percent opening is 20～70%; The described sieve diameter that has the sieve plate of downspout is φ 1～10mm, percent opening is 1～40%, distance between the sieve plate of described downspout bottom and below is 10～50% of a distance between plates, and downspout or claim the sectional area of overflow pipe account for tower section long-pending 5～35%.
Bubbling sieve-plate tower extracting process of the present invention has reached contact purpose with mass transfer of forced fluid-liquid two, impels two-phase smoothly by sieve aperture, thereby has increased substantially heightening efficiency and disposal ability.The bubbling perforated-plate extraction tower of the present invention's design, it promptly is the bubbling technology that in perforated-plate extraction tower, adopts, make gas enter the perforated-plate extraction tower bottom equably and rising rapidly in extraction tower through tower spirit body distributor, on the one hand, liquid layer is carried out intense impact and stirring, impel dispersed phase drop constantly broken, the surface is brought in constant renewal in, strengthen two and contact and mass transfer, increase substantially the mass-transfer efficiency in the extraction process; On the other hand, gas drives light phase liquid and overcomes surface tension effects, makes it to pass smoothly sieve aperture, thereby enlarges markedly the disposal ability of perforated-plate extraction tower.This equipment flux is big, the efficient height; Implementation method is simple, and operating flexibility is good; When particularly adopting macroporous plate, anti-clogging is good.
Further describe the present invention below in conjunction with drawings and Examples.
Description of drawings
Fig. 1 is the overall structure schematic diagram of the bubbling perforated-plate extraction tower used when advancing tower separately of gas.
Fig. 2 is a gas and the overall structure schematic diagram of the light bubbling perforated-plate extraction tower of using when liquid is mixed into tower mutually.
Description of reference numerals: 1 tower body; 2 light phase liquid outlets; 3 gas vents; 4 mesh mist eliminators; 5 are convenient to realize the packing layer of weight two liquid phase separation; 6 heavy-phase liquids inlet; 7 sieve plates and sieve aperture thereof; 8 gas distributors; 9 light phase liquid imports; The outlet of 10 heavy-phase liquids; 11 overhead gas and the light space of fluid separation applications mutually; 12 gas feeds; 13 downspouts and outlet damper thereof; 14 gases and the light shared liquid distribution trough of liquid mutually; 15 are used for gas and the light shared import of liquid mutually; The sieve plate of 16 band downspouts.
The specific embodiment
A kind of bubbling sieve-plate tower extracting process device therefor as shown in Figure 1 is the bubbling perforated-plate extraction tower that gas enters separately, and it comprises tower body 1, and the tower body bottom is provided with light phase liquid import 9, and tower body top is provided with light phase liquid outlet 2; Below light phase liquid outlet, be provided with heavy-phase liquid import 6, be provided with heavy-phase liquid outlet 10 in the tower body bottom; Also be provided with gas feed 12 in the tower body bottom, and link to each other with gas feed be located at gas distributor 8 in the tower, be provided with gas vent 3 at cat head; Establish a mesh mist eliminator 4 that is used to catch, reclaim light phase drop in the tower between described light phase liquid outlet 2 and described gas vent 3; Being provided with several piece in the tower between gas distributor and heavy-phase liquid import does not have the sieve plate 7 of downspout; Also be provided with packing layer 5 in the tower between light phase liquid outlet and heavy-phase liquid import.
A kind of bubbling sieve-plate tower extracting process device therefor as shown in Figure 2 is that gas is mixed after the bubbling perforated-plate extraction tower of same import with light liquid mutually before tower, it comprises tower body 1, the tower body bottom is provided with the same import 15 of light phase liquid and gas, is provided with the liquid distribution trough 14 that is attached thereto in tower; Tower body top is provided with light phase liquid outlet 2; Below light phase liquid outlet, be provided with heavy-phase liquid import 6, be provided with heavy-phase liquid outlet 10 in the tower body bottom; Be provided with gas vent 3 at cat head; And in cat head reservation 0.05-0.5m gas-liquid separation space 11 highly; Be provided with the sieve plate 16 that several piece has downspout in the tower between gas distributor and heavy-phase liquid import; Also be provided with packing layer 5 in the tower between light phase liquid outlet and heavy-phase liquid import.
Wherein, when gas phase is carried secretly seriously, adopt the perforated-plate extraction tower shown in the accompanying drawing 1, increasing by one section high on the light phase liquid outlet in tower is the mesh mist eliminator 4 of 0.2m, to impel gas-liquid separation, the minimizing liquid entrainment.
When gas speed hour, adopt the perforated-plate extraction tower shown in the accompanying drawing 2, reserve the gas-liquid separation space 11 of 0.2m at cat head, can realize gas-liquid separation.This be because, used gas speed is less, the light phase amount of liquid that gas is taken away from the extraction tower top is considerably less, does not generally need to dispose special light phase liquid withdrawal system.
Embodiment:
Embodiment 1: kerosene/benzoic acid-water-air system, kerosene, water proportion are respectively 0.80,1.0, system interfacial tension 37.5mN/m, the bubbling perforated-plate extraction tower of internal diameter Φ 50, the sieve diameter of sieve plate is φ 10mm, percent opening 48%, no downspout, distance between plates 50mm has the gap of 0.5mm between column plate and the tower.When gas speed is 0,10.19,20.37,30.56,40.74,50.95m/h, oil/water volume flow-rate ratio=1.1: 1 o'clock, the benzoic acid mass concentration is 0.0018 in the kerosene, the flux of tower can reach 36,57,65,62,55 respectively, 52m/h, the flux (36m/h) of the flux peak when promptly bubbling being arranged during all greater than no bubbling (gas speed is 0).Kerosene, water volume flow velocity are respectively 22.63,20.37m/h, the benzoic acid mass concentration is 0.001839kg (benzoic acid)/kg (kerosene) in the kerosene, water does not have solute, gas speed is 0,10.19,20.37,30.56,40.74, during 50.95m/h, water outlet benzoic acid mass concentration is respectively 0.00017,0.00028,0.00050,0.00061,0.00070,0.00076, promptly along with gas speed increases, concentration of benzoic acid is more and more higher in the water, illustrates that extraction efficiency becomes better and better.
Embodiment 2: kerosene/benzoic acid-water-air system, kerosene, water proportion are respectively 0.80,1.0, system interfacial tension 37.5mN/m, the bubbling perforated-plate extraction tower of internal diameter Φ 50, the sieve diameter of sieve plate is φ 14mm, percent opening 50%, no downspout, distance between plates 50mm has the gap of 0.5mm between column plate and the tower.When gas speed is 0,10.19,20.37,30.56,40.74,50.95m/h, kerosene/water volume flow-rate ratio=1.1: 1 o'clock, the benzoic acid mass concentration is 0.0018 in the kerosene, the flux of tower can reach 50,80,90,86,77 respectively, 72m/h, the flux (50m/h) of the flux peak when promptly bubbling being arranged during all greater than no bubbling (gas speed is 0).Kerosene, water volume flow velocity are respectively 14.0,12.73m/h, concentration of benzoic acid is 0.001817kg (benzoic acid)/kg (kerosene) in the kerosene, water does not have solute, gas speed is 0,10.19,20.37,30.56,40.74, during 50.95m/h, water outlet benzoic acid mass concentration is respectively 0.000131,0.0001834,0.000296,0.000463,0.000518,0.000613, promptly along with gas speed increases, concentration of benzoic acid is more and more higher in the water, illustrates that extraction efficiency becomes better and better.
Embodiment 3: butyl acetate/acetic acid-water-air system, butyl acetate, water proportion are respectively 0.87,1.0, system interfacial tension 9.6mN/m, the bubbling perforated-plate extraction tower of internal diameter Φ 50, the sieve diameter of sieve plate is φ 10mm, percent opening 48%, no downspout, distance between plates 50mm has the gap of 0.5mm between column plate and the tower.When gas speed is 0,10.19,20.37,30.56,40.74,50.95m/h, butyl acetate/water volume flow-rate ratio=1.1: 1 o'clock, the acetic acid mass concentration is 0.0303 in the butyl acetate, the flux of tower can reach 45,58.5,54,54,54 respectively, 49.5m/h, the flux (45m/h) of the flux peak when promptly bubbling being arranged during all greater than no bubbling (gas speed is 0).Butyl acetate, water volume flow velocity are respectively 20.16,7.13m/h, the acetic acid mass concentration is 0.0303kg (acetic acid)/kg (butyl acetate) in the butyl acetate, water does not have solute, gas speed is 0,10.19,20.37,30.56,40.74, during 50.95m/h, water outlet benzoic acid mass concentration is respectively 0.0322,0.0449,0.0470,0.0488,0.0502,0.0520, promptly along with gas speed increases, acetate concentration is more and more higher in the water, illustrates that extraction efficiency becomes better and better.
Claims (5)
1, a kind of bubbling perforated-plate extraction tower extracting process is characterized in that in the bubbling perforated-plate extraction tower, and heavy-phase liquid is flowed into from the top of tower, flows out through the below from tower behind the some sieve plates; Light phase liquid flows into from the below of tower, flows out through the top from tower behind the some sieve plates; Make gas at the bottom of tower, enter the bubbling perforated-plate extraction tower, enter bubbling perforated-plate extraction tower bottom equably, flow out through the top from tower behind the some sieve plates by distributor with the empty tower gas velocity of 0.5～80mm/s.
2, the method for claim 1 is characterized in that described gas is air or inert gas.
3, method as claimed in claim 2 is characterized in that described inert gas is a nitrogen.
4, the method for claim 1, the density that it is characterized in that described light phase liquid is 30～95% of heavy-phase liquid density.
5, the method for claim 1 is characterized in that described heavy-phase liquid is 10～100m with the light total flux of liquid mutually
3/ m
2H.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 03105346 CN1256999C (en) | 2003-02-25 | 2003-02-25 | Extraction method and apparatus of a bubbling sieve plate tower |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 03105346 CN1256999C (en) | 2003-02-25 | 2003-02-25 | Extraction method and apparatus of a bubbling sieve plate tower |
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| Publication Number | Publication Date |
|---|---|
| CN1524602A CN1524602A (en) | 2004-09-01 |
| CN1256999C true CN1256999C (en) | 2006-05-24 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 03105346 Expired - Lifetime CN1256999C (en) | 2003-02-25 | 2003-02-25 | Extraction method and apparatus of a bubbling sieve plate tower |
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| CN (1) | CN1256999C (en) |
Families Citing this family (9)
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| CN102491275B (en) * | 2011-11-24 | 2015-10-28 | 贵州大学 | A kind of Large-scale iodine extraction plant |
| CN102512848B (en) * | 2011-12-07 | 2014-09-24 | 中国科学院过程工程研究所 | Large phase ratio liquid-liquid two-phase continuous extraction apparatus |
| CN102921288B (en) * | 2012-10-31 | 2014-07-16 | 浙江天蓝环保技术股份有限公司 | Y-shaped absorption tower and method for performing flue gas desulfurization by using Y-shaped absorption tower |
| CN103752036B (en) * | 2014-01-20 | 2015-07-01 | 中国科学院青岛生物能源与过程研究所 | Bubble-assisted organic liquid film generator |
| CN104709957B (en) * | 2015-02-16 | 2016-03-30 | 吉林大学 | The device and method of extracting and separating Organic Chemicals In Groundwater and tensio-active agent |
| CN105194951A (en) * | 2015-10-29 | 2015-12-30 | 徐州天正活性炭厂 | Activated carbon production tail gas purification device and purification method |
| CN107828961B (en) * | 2017-11-02 | 2024-04-05 | 中国科学院过程工程研究所 | Extraction method of rare earth element ions and obtained rare earth enrichment liquid |
| CN109224528B (en) * | 2018-11-14 | 2021-02-02 | 北京工业大学 | Connected continuous extraction device with same pressure and controllable size of bubbles of gas-assisted solvent |
| CN113350976A (en) * | 2021-06-07 | 2021-09-07 | 南京师范大学 | Tail gas treatment and recovery method |
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2003
- 2003-02-25 CN CN 03105346 patent/CN1256999C/en not_active Expired - Lifetime
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| CN1524602A (en) | 2004-09-01 |
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Effective date of registration: 20090313 Address after: Yunnan Qujing Yuexiu Shuicheng Zhongyi Coal Chemical Co., Ltd. zip code: 655003 Co-patentee after: BEIJING INSTITUTE OF PETROCHEMICAL TECHNOLOGY Patentee after: QUJING ZHONGYI COAL INDUSTRY C Address before: Department of chemical engineering, Beijing Petrochemical University: 102617 Patentee before: BEIJING INSTITUTE OF PETROCHEMICAL TECHNOLOGY |
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Address after: 655003 Yunnan city of Qujing Province Yue Zhou Zhen Shuicheng coal Ltd. Zhong Yi Co-patentee after: BEIJING INSTITUTE OF PETROCHEMICAL TECHNOLOGY Patentee after: QUJING ZHONGYI FINE CHEMICAL INDUSTRY Co.,Ltd. Address before: 655003 Yunnan city of Qujing Province Yue Zhou Zhen Shuicheng coal Ltd. Zhong Yi Co-patentee before: BEIJING INSTITUTE OF PETROCHEMICAL TECHNOLOGY Patentee before: QUJING ZHONGYI COAL INDUSTRY C |
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