CN103537172B - A kind of eddy flow distillation desorber and application - Google Patents
A kind of eddy flow distillation desorber and application Download PDFInfo
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- CN103537172B CN103537172B CN201310477524.5A CN201310477524A CN103537172B CN 103537172 B CN103537172 B CN 103537172B CN 201310477524 A CN201310477524 A CN 201310477524A CN 103537172 B CN103537172 B CN 103537172B
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- desorber
- section
- tower body
- eddy flow
- swirl vane
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- 238000004821 distillation Methods 0.000 title claims abstract description 25
- 239000007788 liquid Substances 0.000 claims abstract description 64
- 239000004744 fabric Substances 0.000 claims abstract description 17
- 238000003795 desorption Methods 0.000 claims abstract description 13
- 239000006260 foam Substances 0.000 claims abstract description 12
- 239000012530 fluid Substances 0.000 claims abstract description 4
- 238000009434 installation Methods 0.000 claims abstract description 4
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 3
- 238000010276 construction Methods 0.000 claims description 3
- 239000003546 flue gas Substances 0.000 claims description 3
- 238000005262 decarbonization Methods 0.000 claims description 2
- 239000007921 spray Substances 0.000 claims description 2
- 238000007789 sealing Methods 0.000 claims 1
- 230000000694 effects Effects 0.000 abstract description 11
- 238000006243 chemical reaction Methods 0.000 abstract description 6
- 239000000463 material Substances 0.000 abstract description 4
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 20
- 238000000034 method Methods 0.000 description 13
- 229910002092 carbon dioxide Inorganic materials 0.000 description 10
- 239000001569 carbon dioxide Substances 0.000 description 8
- 239000007789 gas Substances 0.000 description 8
- 238000010521 absorption reaction Methods 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- 230000002745 absorbent Effects 0.000 description 3
- 239000002250 absorbent Substances 0.000 description 3
- 239000000945 filler Substances 0.000 description 3
- 230000008901 benefit Effects 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 238000001704 evaporation Methods 0.000 description 2
- 230000008020 evaporation Effects 0.000 description 2
- 238000011049 filling Methods 0.000 description 2
- 230000005484 gravity Effects 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- BGOFCVIGEYGEOF-UJPOAAIJSA-N helicin Chemical compound O[C@@H]1[C@@H](O)[C@H](O)[C@@H](CO)O[C@H]1OC1=CC=CC=C1C=O BGOFCVIGEYGEOF-UJPOAAIJSA-N 0.000 description 2
- PVXVWWANJIWJOO-UHFFFAOYSA-N 1-(1,3-benzodioxol-5-yl)-N-ethylpropan-2-amine Chemical compound CCNC(C)CC1=CC=C2OCOC2=C1 PVXVWWANJIWJOO-UHFFFAOYSA-N 0.000 description 1
- QMMZSJPSPRTHGB-UHFFFAOYSA-N MDEA Natural products CC(C)CCCCC=CCC=CC(O)=O QMMZSJPSPRTHGB-UHFFFAOYSA-N 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000006194 liquid suspension Substances 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000000725 suspension Substances 0.000 description 1
- 238000010792 warming Methods 0.000 description 1
Landscapes
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The present invention relates to a kind of eddy flow distillation desorber, the tower body of this desorber is the vertical tower of hollow, installation one leakage fluid dram is communicated with in the bottom of tower body, one liquid storage section is installed bottom the tower body of desorber, one heater is installed in liquid storage section, eddy flow section logical in is set in the tower body above liquid storage section, the cloth liquid section of a hollow is set in the tower body above eddy flow section, arrange a foam removal section in tower body above cloth liquid section, in the tower body above foam removal section, top arranges a desorber outlet.The eddy flow section of desorber of the present invention comprises whirl cylinder and cyclone, cyclone comprises swirl vane axle and swirl vane, novel desorber internals installed by this desorber, this desorber utilizes eddy flow principle, add the intensity of distillation desorb, reduce the height of reaction tower, save space and material, gas-liquid mass transfer intensity is high, improves the desorption effect of reaction tower.
Description
Technical field
The invention belongs to chemical industry, environmental technology field, relate to distillation desorb reaction tower, especially a kind of eddy flow distillation desorber and application.
Background technology
Research shows, the excessive emissions of carbon dioxide, is the major reason causing the environmental problems such as global warming.China is also increasingly strict to the control of CO2 emission.In many CO2 emission sources, the most concentrated with the carbon dioxide of burning and exhausting, and concentration is higher, more for the benefit of absorbs.
For the improvement of carbon dioxide, adopting more method at present, is absorb the carbon dioxide in combustion product gases, then the absorbing liquid of enrichment is resolved, by carbon dioxide collection higher for purity, carry out corresponding after-treatment, reach the target of the comprehensive regulation.
The technological process of carbon dioxide absorption and desorb is ripe and realizes the technology of commercial Application, employing MEA or MDEA is absorbent, containing the carbon dioxide of about 20% in solution after absorption, this solution is claimed to be rich solution, rich solution is passed in stripping apparatus, carry out distillation desorb, isolate carbon dioxide, in solution under residue, gas concentration lwevel is about 7%, claims this solution to be lean solution.Lean solution passes in absorption equipment, recycles as absorbent.
In whole flow process, distillation desorption process is the key that can this technology recycle absorbent, and the height of its desorption efficiency directly affects the effect of absorption and the energy consumption height of desorb simultaneously, and different desorption methods directly affects the cost of operation.Distillation desorption process mainly relies on steam and liquid comes into contact, and the heat of steam, by the material evaporation to be separated in solution, forms gaseous material and enters in follow-up flow process, to reach the object of solute and separated from solvent.Therefore, the size of gas liquid interfacial area, the power of gas-liquid exchange directly affects the efficiency of distillation desorb.
Distillation desorption apparatus is generally desorber, and desorber form conventional at present mainly contains packed tower and plate column, and plate column is divided into again sieve-plate tower, valve tray tower etc.Packed tower utilizes the surface area of filler large, the principle that gas liquid interfacial area is large realizes desorb, treat that stripping workshop flows through filling surface from top to bottom, steam flows through filler from bottom to top, and two media contacts at filling surface, realize still-process, its gas-liquid contact face is large, but its gas-liquid mass transfer intensity is more weak, causes packed tower volume huger, from great, and easily there is the problems such as blocking in filler.Plate column utilizes solution to flow through tray surfaces, and on plate, device is to strengthen gas-liquid mass transfer intensity, thus realizes the turriform of still-process, wherein arranges multilayer column plate, and template has multiple pattern optional.On column plate tower, height of liquid layer needs more strictly to control, and the situation of flooding easily occurs, and individual layer plate efficiency is lower, needs series connection to compare multilayer column plate and just can reach target efficiency.
According to the principle of existing distillation desorption apparatus, increase gas-liquid contact surface area or increase gas-liquid mass transfer intensity, the effect of distillation desorb can be improved, improving desorption efficiency.
By retrieval, not yet find the patent publication us relevant to patent application of the present invention.
Summary of the invention
The object of the invention is to overcome the deficiencies in the prior art part, provide a kind of new desorber form, this desorber is provided with novel desorber internals, and this desorber utilizes the work of eddy flow principle, and gas-liquid mass transfer intensity is high, effectively improves the desorption effect of reaction tower.
The object of the invention is to be achieved through the following technical solutions:
A kind of eddy flow distillation desorber, the tower body of this desorber is the vertical tower of hollow, installation one leakage fluid dram is communicated with in the bottom of tower body, one liquid storage section is installed bottom the tower body of desorber, one heater is installed in liquid storage section, eddy flow section logical in one is coaxially set in the tower body above liquid storage section, the cloth liquid section of one hollow is coaxially set in the tower body above eddy flow section, coaxially arrange a foam removal section in tower body above cloth liquid section, in the tower body above foam removal section, top arranges a desorber outlet;
Described eddy flow section comprises whirl cylinder and cyclone, the coaxial whirl cylinder installing a hollow in eddy flow section, on the outer surface of this whirl cylinder top and bottom, co-axial seal installs the inner edge of shrouding, the outer rim co-axial seal of this shrouding is installed on inside tower body, in this whirl cylinder, cyclone is installed in bottom, cyclone comprises swirl vane axle and swirl vane, swirl vane circularizes arrangement around swirl vane axle, tilts to be installed on swirl vane axle, swirl vane axle is coaxial with whirl cylinder, installs swirl vane between whirl cylinder and swirl vane axle.
And, bottom in the tower body of desorber is coaxially shaped with the liquid storage section of a hollow, a side bottom liquid storage section installs a heater, or, described liquid storage section is installed on outside the tower body of desorber, utilizes communicating pipe to be connected with desorber, top communicating pipe delivering vapor, bottom communicating pipe delivered solution, the side bottom liquid storage section installs a heater.
And, coaxial series multistage eddy flow section in the tower body above described liquid storage section.
And described heater is electric heater, steam heater or hot oil heater.
And the cloth liquid mode of described cloth liquid section takes the parallel connection of tree-shaped primary branch, pipe network, overflow launder, nozzle evenly spray a kind of cloth liquid mode in solution.
And described foam removal section adopts wire mesh demister or deflector-type separator.
And described swirl vane is the blade construction that propeller type tilts, and its angle of inclination becomes 30-60 degree with axis, and adopt the blade shape of plane or curved surface, its perspective plane is rectangle or fan-shaped.
Eddy flow as above distillation desorber is as the application in the desorption apparatus in flue gas decarbonization system.
Advantage of the present invention and good effect are:
1, the eddy flow section of desorber of the present invention comprises whirl cylinder and cyclone, cyclone comprises swirl vane axle and swirl vane, swirl vane circularizes arrangement around swirl vane axle, tilts to be installed on swirl vane axle, novel desorber internals installed by this desorber, and this desorber utilizes eddy flow principle, add the intensity of distillation desorb, reduce the height of reaction tower, save space and material, gas-liquid mass transfer intensity is high, improves the desorption effect of reaction tower.
2, desorber of the present invention is a kind of pattern of distillation desorber newly, and relative packed tower volume is less, deadweight is lighter, and tower internals circulation diameter is comparatively large, should not block; Relative plate column, individual layer mass transfer effect is stronger, does not also have the situation of flooding to occur, uses more convenient.
Accompanying drawing explanation
Fig. 1 is structure partial sectional view of the present invention;
Fig. 2 is the structure enlarged diagram of eddy flow section in Fig. 1;
Fig. 3 is the top view of Fig. 2;
Fig. 4 is the axle side schematic diagram of cyclone of the present invention.
Detailed description of the invention
For accompanying drawing embodiment, the invention will be further described below, and following examples are descriptive, is not determinate, can not limit protection scope of the present invention with this.
A kind of eddy flow distillation desorber, as shown in Figure 1, the tower body 5 of this desorber is the vertical tower of hollow, in the bottom of tower body, supporting leg 1 is installed, installation one leakage fluid dram 2 is communicated with in the bottom of tower body, bottom in the tower body of desorber coaxially arranges the liquid storage section 3 of a hollow, can storing solution in this liquid storage section, the amount of solution stored in liquid storage section can be set to the evaporation capacity of satisfied ten minutes, at liquid storage section one side, one heater 4 is installed, heater can use electric heater, steam heater or heat conduction wet goods heater, heating power is according to institute's calorific requirement configuration in desorb, or, liquid storage section and heater also can be installed on beyond desorb tower body as independently equipment, communicating pipe is utilized to be connected with desorber, top communicating pipe delivering vapor, bottom communicating pipe delivered solution, a side bottom liquid storage section installs a heater, logical eddy flow section 6 is coaxially set in the tower body above liquid storage section in one, also can coaxial series multistage eddy flow section in the tower body above liquid storage section, the upper and lower three swirler section that is coaxially installed in series successively in the tower body in the present embodiment above liquid storage section, the cloth liquid section 7 of one hollow is coaxially set in the tower body above eddy flow section, takes single tube end that the cloth liquid mode of nozzle is installed in the present embodiment, also can take the various ways such as the parallel connection of tree-shaped primary branch, pipe network, overflow launder.Coaxially arrange a foam removal section 8 in tower body above cloth liquid section, this foam removal section can adopt wire mesh demister or deflector-type separator.In tower body above foam removal section, top arranges a desorber outlet 9.
As in Figure 2-4, described eddy flow section comprises whirl cylinder 13 and cyclone (in figure non-label), the coaxial whirl cylinder installing a hollow in eddy flow section, this whirl cylinder height 300mm-1000mm, on the outer surface of this whirl cylinder top and bottom, co-axial seal installs the inner edge of shrouding 10, and the outer rim co-axial seal of this shrouding is installed on inside tower body, and this shrouding can prevent flue gas short circuit, by the enclosed cross of the desorber tower body beyond whirl cylinder, this shrouding can be welded on whirl cylinder.In this whirl cylinder, cyclone is installed in bottom, cyclone comprises swirl vane axle 12 and swirl vane 11, swirl vane circularizes arrangement around swirl vane axle, tilts to be installed on swirl vane axle, swirl vane axle is coaxial with whirl cylinder, install swirl vane between whirl cylinder and swirl vane axle, the internal diameter of whirl cylinder is identical with the external diameter of swirl vane.Swirl vane is the blade construction that propeller type tilts, and its angle of inclination becomes 30-60 degree with axis, and the quantity of swirl vane can be determined as the case may be, arranges six swirl vanes in the present embodiment; In the present embodiment, the angle of inclination of swirl vane and axis direction is 30 degree; Swirl vane can take plane or curve form, and the present embodiment is plane blade; The profile of projecting blade can be rectangle or fan-shaped, and the present embodiment is fan-shaped.
The operation principle of desorber of the present invention is as follows:
Treat that the solution of desorb enters in desorber by the pipeline of cloth liquid section 7, flow in liquid storage section 3 from top to bottom under gravity, keep certain liquid level in liquid storage section, at least will exceed heater 4.Heater heats the solution in liquid storage section, and the heating continued to boiling is to produce the steam of stable quantity.Steam flows through eddy flow section 6 from bottom to top, spiral helicine air-flow is formed under the effect of swirl vane 11, upwards flow along whirl cylinder 13, it more than cyclone is cloth liquid section, to treat that the distribution mode of stripping workshop by different process demand passes in desorber, some layers of cyclone are flowed through from top to bottom after solution enters, spiral helicine air-flow contacts with top-down solution in whirl cylinder, solution is broken and is divided into droplet under the effect of swirling eddy, the drop that diameter is less than dividing diameter can move upward with air-flow from bottom to top, and in motion process, aggregate into the drop of larger particles gradually, fall under gravity, this process can ceaselessly move in circles, macroscopically will form one section of gas-liquid suspension section in whirl cylinder, there is violent effect of mass transmitting in gas-liquid two-phase in this suspension section, achieve the distilling effect taken out of by steam by the solute in solution.Solute gas and steam move upward jointly, and through foam removal section 8, the drop carried by gas catches removing, and to reach the object of purification desorption gas, purified gas discharges desorber through desorber outlet 9, enters follow-up equipment and processes further.
Claims (7)
1. an eddy flow distillation desorber, the tower body of this desorber is the vertical tower of hollow, installation one leakage fluid dram is communicated with in the bottom of tower body, it is characterized in that: a liquid storage section is installed bottom the tower body of desorber, one heater is installed in liquid storage section, eddy flow section logical in one is set in the tower body above liquid storage section, the cloth liquid section of one hollow is set in the tower body above eddy flow section, arrange a foam removal section in tower body above cloth liquid section, in the tower body above foam removal section, top arranges a desorber outlet;
Described eddy flow section comprises whirl cylinder and cyclone, the whirl cylinder of one hollow is installed in eddy flow section, on the outer surface of this whirl cylinder top and bottom, the inner edge of shrouding is installed in sealing, the outer fringe seal of this shrouding is installed on inside tower body, in this whirl cylinder, cyclone is installed in bottom, cyclone comprises swirl vane axle and swirl vane, swirl vane circularizes arrangement around swirl vane axle, tilts to be installed on swirl vane axle, swirl vane axle is coaxial with whirl cylinder, installs swirl vane between whirl cylinder and swirl vane axle;
Bottom in the tower body of desorber is shaped with the liquid storage section of a hollow, one heater is installed bottom liquid storage section, or, described liquid storage section is installed on outside the tower body of desorber, communicating pipe is utilized to be connected with desorber, top communicating pipe delivering vapor, bottom communicating pipe delivered solution, a heater is installed bottom liquid storage section.
2. eddy flow distillation desorber according to claim 1, is characterized in that: series multistage eddy flow section in the tower body above described liquid storage section.
3. eddy flow distillation desorber according to claim 1, is characterized in that: described heater is electric heater, steam heater or hot oil heater.
4. eddy flow according to claim 1 distillation desorber, is characterized in that: the cloth liquid mode of described cloth liquid section takes the parallel connection of tree-shaped primary branch, pipe network, overflow launder, nozzle evenly spray a kind of cloth liquid mode in solution.
5. eddy flow distillation desorber according to claim 1, is characterized in that: described foam removal section adopts wire mesh demister or deflector-type separator.
6. eddy flow distillation desorber according to claim 1, is characterized in that: described swirl vane is the blade construction that propeller type tilts, and its angle of inclination becomes 30-60 degree with axis, and adopt the blade shape of plane or curved surface, its perspective plane is rectangle or fan-shaped.
7. the eddy flow distillation desorber as described in any one of claim 1 to 6 is as the application in the desorption apparatus in flue gas decarbonization system.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310477524.5A CN103537172B (en) | 2013-10-14 | 2013-10-14 | A kind of eddy flow distillation desorber and application |
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| Application Number | Priority Date | Filing Date | Title |
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| CN201310477524.5A CN103537172B (en) | 2013-10-14 | 2013-10-14 | A kind of eddy flow distillation desorber and application |
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| CN103537172A CN103537172A (en) | 2014-01-29 |
| CN103537172B true CN103537172B (en) | 2016-01-13 |
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| CN201310477524.5A Expired - Fee Related CN103537172B (en) | 2013-10-14 | 2013-10-14 | A kind of eddy flow distillation desorber and application |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| MX2019014327A (en) * | 2017-06-15 | 2020-02-05 | Exxonmobil Upstream Res Co | Fractionation system using compact co-current contacting systems. |
| CN107088314B (en) * | 2017-06-27 | 2022-08-09 | 山东鼎裕生物能源有限公司 | Rectifying tower |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| SU580868A1 (en) * | 1976-07-20 | 1977-11-25 | Всесоюзный Научно-Исследовательский И Проектно-Конструкторский Институт Нефтяного Машиностроения | Heat-mass exchange apparatus |
| JPS5633006A (en) * | 1979-08-25 | 1981-04-03 | Mitsui Petrochem Ind Ltd | Tray apparatus of distilling column and the like |
| CN1671451A (en) * | 2002-07-29 | 2005-09-21 | 科克－格利奇有限公司 | Vapor-liquid contact trays and method employing same |
| CN1695768A (en) * | 2005-06-06 | 2005-11-16 | 天津大学 | Pyramidal laying liquid typed high performance mass transfer tray with central downcast pipe |
| CN201411449Y (en) * | 2009-06-19 | 2010-02-24 | 刘明学 | Spiral stripping tower |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN203610019U (en) * | 2013-10-14 | 2014-05-28 | 航天环境工程有限公司 | Cyclone distillation desorption column |
-
2013
- 2013-10-14 CN CN201310477524.5A patent/CN103537172B/en not_active Expired - Fee Related
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| SU580868A1 (en) * | 1976-07-20 | 1977-11-25 | Всесоюзный Научно-Исследовательский И Проектно-Конструкторский Институт Нефтяного Машиностроения | Heat-mass exchange apparatus |
| JPS5633006A (en) * | 1979-08-25 | 1981-04-03 | Mitsui Petrochem Ind Ltd | Tray apparatus of distilling column and the like |
| CN1671451A (en) * | 2002-07-29 | 2005-09-21 | 科克－格利奇有限公司 | Vapor-liquid contact trays and method employing same |
| CN1695768A (en) * | 2005-06-06 | 2005-11-16 | 天津大学 | Pyramidal laying liquid typed high performance mass transfer tray with central downcast pipe |
| CN201411449Y (en) * | 2009-06-19 | 2010-02-24 | 刘明学 | Spiral stripping tower |
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| CN103537172A (en) | 2014-01-29 |
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Effective date of registration: 20161125 Address after: 100074 room No. A, zone, No. 7 Ash Road, Beijing, Fengtai District Patentee after: BEIJING AEROSPACE ENVIRONMENTAL ENGINEERING CO.,LTD. Address before: 300384 Mei Nankai District Huayuan Industrial District of Tianjin City, No. 9, No. 1 Court Road, building 1 unit 801 Patentee before: AEROSPACE ENVIRONMENTAL ENGINEERING Co.,Ltd. |
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