WO2014086089A1 - 一种分隔流无返混喷射塔盘 - Google Patents
一种分隔流无返混喷射塔盘 Download PDFInfo
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- WO2014086089A1 WO2014086089A1 PCT/CN2013/001284 CN2013001284W WO2014086089A1 WO 2014086089 A1 WO2014086089 A1 WO 2014086089A1 CN 2013001284 W CN2013001284 W CN 2013001284W WO 2014086089 A1 WO2014086089 A1 WO 2014086089A1
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- WIPO (PCT)
- Prior art keywords
- liquid
- tank
- tray
- downcomer
- liquid receiving
- Prior art date
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- 238000005507 spraying Methods 0.000 title abstract 7
- 239000007788 liquid Substances 0.000 claims abstract description 255
- 238000012546 transfer Methods 0.000 claims description 71
- 239000007921 spray Substances 0.000 claims description 8
- 239000012528 membrane Substances 0.000 claims description 2
- 238000002347 injection Methods 0.000 claims 12
- 239000007924 injection Substances 0.000 claims 12
- 238000000034 method Methods 0.000 description 11
- 239000010410 layer Substances 0.000 description 10
- 230000008569 process Effects 0.000 description 10
- 239000003595 mist Substances 0.000 description 7
- 238000004891 communication Methods 0.000 description 6
- 230000000694 effects Effects 0.000 description 6
- 239000006260 foam Substances 0.000 description 6
- 238000000926 separation method Methods 0.000 description 6
- 238000013461 design Methods 0.000 description 5
- 238000005187 foaming Methods 0.000 description 5
- 239000007791 liquid phase Substances 0.000 description 5
- 238000010521 absorption reaction Methods 0.000 description 3
- 230000005587 bubbling Effects 0.000 description 3
- 230000004907 flux Effects 0.000 description 3
- 230000006872 improvement Effects 0.000 description 3
- 239000012071 phase Substances 0.000 description 3
- 230000008901 benefit Effects 0.000 description 2
- 238000002386 leaching Methods 0.000 description 2
- 230000014759 maintenance of location Effects 0.000 description 2
- 239000002356 single layer Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- QNRATNLHPGXHMA-XZHTYLCXSA-N (r)-(6-ethoxyquinolin-4-yl)-[(2s,4s,5r)-5-ethyl-1-azabicyclo[2.2.2]octan-2-yl]methanol;hydrochloride Chemical compound Cl.C([C@H]([C@H](C1)CC)C2)CN1[C@@H]2[C@H](O)C1=CC=NC2=CC=C(OCC)C=C21 QNRATNLHPGXHMA-XZHTYLCXSA-N 0.000 description 1
- 230000003321 amplification Effects 0.000 description 1
- 238000003889 chemical engineering Methods 0.000 description 1
- 238000001311 chemical methods and process Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000006185 dispersion Substances 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000004744 fabric Substances 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
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- 239000011148 porous material Substances 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
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Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
- B01D3/16—Fractionating columns in which vapour bubbles through liquid
- B01D3/18—Fractionating columns in which vapour bubbles through liquid with horizontal bubble plates
- B01D3/20—Bubble caps; Risers for vapour; Discharge pipes for liquid
Definitions
- the invention relates to a heat transfer and mass transfer device in chemical engineering, in particular to a split flow non-backmixing spray tray for chemical heat transfer and mass transfer separation.
- the tray is especially suitable for handling large fluid and foamy systems.
- the downflow system of the tray is often designed into multiple downcomers, and the existing multi-downcomer trays, such as foreign MD sieve plates, or domestic
- the main structural features of the DJ tray are: (1) The downcomer is a rectangular trough, arranged in the middle of the tray, and the overflow of the downcomer acts greatly, which greatly increases the length of the weir; (2) The downcomer is suspended in the gas phase space, and there is no liquid receiving tray on the tray, which increases the effective bubbling area of the tray.
- the existing multi-downcomer trays especially the problem of bias and distribution during liquid flow.
- the trays used in the fine boring and absorption processes are inefficient and are not suitable for the treatment of large liquid and easy foam systems. Part of the reason is:
- the existing multi-downcomer trays, the mass transfer units on the trays are mainly sieve plates, and there are also mass transfer units in the form of float valves, solid and wide, all of which are bubbling mass transfer.
- the main structural form when operating under high load conditions, although the mass transfer mode is switched from the bubbling state to the jet state, a large amount of foam is still generated, and the foam is often unable to be effectively separated in the conventional leaching downflow system. It is obviously gas phase back mixing, and it is easy to cause the downcomer to flood and the phenomenon of excessive mist entrainment.
- the liquids of the multi-downcomer tray and the flow-through tray are all descending from the top to the bottom.
- a large amount of foam generated during the mass transfer process is carried to the next tray to increase the flow intensity.
- the gas phase entrainment back-mixing effect reduces the mass transfer efficiency;
- the leaching process itself causes the liquid flow of the upper tray to impact the liquid level of the lower tray, creating some bubbles, and also the liquid receiving The area causes a certain impact and leakage, and can not be applied to the absorption and rectification treatment of chemical process materials with large liquid volume and easy foaming system.
- Chinese patent CN101554538A discloses a multi-downcomer tray, the main structure of which is a plurality of rectangular downcomers and extension elements, the tray is a single-layer structure, and the structure tray has a liquid phase back-mixing phenomenon, resulting in a tower The board is less efficient.
- U.S. Patent (US 6,059,934) also discloses a tray which adopts a multi-downcomer design of a single-layer tray and introduces liquid into the gas-liquid contact chamber, and the gas-liquid is simultaneously transferred to the gas.
- the shortcoming is that the gas-liquid contact time is short, the contact space of the gas-liquid dispersion is small, and when the liquid flow rate is large, the downflow tube flooding phenomenon is likely to occur.
- the three-dimensional jet mass transfer tray represented by the new vertical sieve plate has high efficiency, large flux, and is suitable for processing the system which is easy to foam and easy to block. It has been widely used in many rectification and absorption fields, but for liquid
- the industrial equipment with relatively large gas, large tower diameter and serious foaming of the system has poor application effect, and cannot solve the problem that the liquid level gradient generated during the tower diameter amplification process is too large, the gas-liquid contact is insufficient, and the liquid back-mixing Serious and other issues.
- the mass transfer unit is a spray-type mass transfer, and the droplets fall into the liquid surface of the tray after mass transfer in the tray space, which causes the liquid group to impact and the liquid surface to foam.
- the technical problem to be solved by the present invention is to provide a split flow non-backmixing jet tray.
- the tray adopts multiple downcomer structure, liquid guiding tank structure and three-dimensional jet mass transfer unit structure, which has high mass transfer efficiency, large operation flexibility, large flux, strong anti-blocking property, small mist entrainment, and realization of liquid. It has the characteristics of no back mixing, etc. It can solve a series of problems such as cross flow, bias flow, retention and liquid level gradient of the existing trays, greatly improving the efficiency of the tray, product yield and product grade, and the energy saving and environmental protection effect is obvious.
- the technical solution of the present invention to solve the technical problem is to design a split flow non-backmixing spray tray, which is composed of an upper tray and a lower tray, each of which includes a downflow tank and a descending tray.
- a liquid pipe, a liquid receiving tank, a three-dimensional jet mass transfer unit and a liquid guiding tank characterized in that a horizontal liquid receiving tank is opened at a horizontal position in the center of the tray, and the liquid receiving tank includes a central liquid receiving tank and other liquid receiving tanks The center is filled by the liquid trough on the center line of the tray, and the other liquid receiving tanks are symmetrically parallel to the left and right sides of the central liquid receiving trough.
- the length of the liquid receiving trough depends on the diameter or chord length of the position, and the center is affected by
- the length of the liquid tank is the same as the diameter of the tray, and the length of the other liquid receiving tank depends on the chord length of the position of the liquid receiving tank; a long-shaped downflow tank is opened between the adjacent two liquid receiving tanks,
- the bottom of the downcomer is designed with a downcomer, each downcomer corresponding to a downcomer, each downcomer extends through the downcomer and is fixed in the downcomer; in the downcomer and the receiver tank There is a three-dimensional jet mass transfer unit arranged between them; in the three-dimensional jet mass transfer unit cap a liquid guiding groove is arranged around, the liquid guiding groove is a baffle type liquid guiding groove, and the liquid guiding groove is arranged around the three-dimensional jet mass transfer unit cap, and the structure has three walls, one end is open, and a convex tube is arranged in the middle.
- the size and number of the convex tube are consistent with the cap on the three-dimensional jet mass transfer unit, and the height of the wall of the other end of the liquid guiding groove corresponding to the opening end is equal to the height of the cap, and the opening end of the liquid guiding groove faces the downcomer.
- the width of the liquid guiding tank is the same as the width occupied by the three-dimensional jet mass transfer unit on the horizontal tray, and one liquid guiding tank corresponds to a set of three-dimensional jet mass transfer units; the upper tray and the lower tray have the same shape and structure, the upper layer A set of downcomers below the downcomer of the tray corresponds to a liquid receiving tank of the lower tray, and is installed in a dislocated position, and is combined into a double-layered split flow without back mixing jet tray.
- the split flow non-backmixing jet tray of the present invention has the following advantages:
- the downflow tank and the liquid receiving tank are all designed with a long strip structure, and a plurality of downtake tanks and a plurality of liquid receiving tanks are arranged on the tray, and a plurality of downcomers are arranged at the bottom of each downcomer.
- the downcomer extends into the downcomer through the downcomer. Design of multiple downcomers to achieve liquid splitting and strong anti-blocking properties;
- the depth of the tank, the diameter of the downcomer, and the depth of the downcomer extending into the downcomer can adjust the thickness of the liquid layer on the tray to adjust the liquid residence time, reduce foaming, and improve gas-liquid separation efficiency.
- the downcomer is designed as a narrow strip, which has a small cross-sectional area. It is especially suitable for large liquid conditions, which can ensure the uniform flow of the whole tray and ensure the uniform liquid level on the board. Compared with the traditional multi-downcomer tray and the descending tray under the same working conditions, the liquid level is low and the pressure drop is small, which eliminates the gas-liquid bubble mass transfer mechanism.
- the setting of the liquid guiding tank separates the mass transfer and the unmassed liquid, so that the liquid which has the gas-liquid mass transfer can flow directly from the liquid guiding tank through the downcomer to the lower tray, avoiding
- the back-mixing of the liquid on the tray without gas-liquid contact causes a maximum difference between the concentration of the liquid component and the concentration of the gas component, thereby greatly improving the mass transfer driving force and the tray efficiency.
- the liquid level balance tank is connected with the downflow tank, so that the liquid in the downflow tank of each end is collected in the liquid level balance tank, and evenly distributed into the respective downtake tanks, so that the liquid distribution is uniform and the liquid level gradient is lowered.
- the design of the liquid level balance tank solves the problems of cross flow, bias flow, stagnation and liquid level gradient in the mass transfer zone, and improves the efficiency of the tray.
- the three-dimensional jet mass transfer unit makes full use of the high efficiency characteristics of gas-liquid jet mass transfer, attaches importance to the increase of gas-liquid contact time and space, reduces the entrainment of mist, and makes the gas-liquid contact in the mass transfer zone of the whole tray become
- the cloth-based, flow-free, and mass transfer-based processes eliminate the effects of bias, stagnation, and liquid level gradients, resulting in an overall improvement in tray efficiency.
- FIG. 1 is a plan view showing the structure of an upper tray of an embodiment of a split flow non-backmixing jet tray of the present invention.
- Fig. 2 is a front perspective view showing an embodiment of a split flow non-backmixing jet tray of the present invention
- Fig. 1 is a cross-sectional view taken along line A-A of Fig. 1.
- Fig. 3 is a plan view showing the structure of the lower tray of one embodiment of the split flow non-backmixing jet tray of the present invention.
- Figure 4 is a set of double-layer tray left-view knots of an embodiment of the split flow non-back mixing jet tray of the present invention. Schematic diagram.
- Fig. 5 is a schematic view showing the main structure of a set of double-layer trays of another embodiment of the split flow non-backmixing jet tray of the present invention, in which a level balance tank 8 is provided.
- Figure 6 is a schematic plan view showing the structure of the upper tray of another embodiment of the split flow non-backmixing jet tray of the present invention, in which the liquid level balance tank 8 is in communication with the downcomer 3.
- Fig. 7 is a schematic plan view showing the structure of the upper tray of another embodiment of the split flow non-backmixing jet tray of the present invention, in which the liquid level balance tank 8 communicates with the liquid receiving tank 5.
- Fig. 8 is a left side structural view of a set of double-layer trays of another embodiment of the split flow non-backmixing jet tray of the present invention, in which the level balance tank 8 is placed in the middle of the tray.
- Fig. 9 is a plan view showing the structure of a liquid guiding tank of an embodiment of the split flow non-back mixing jet tray of the present invention.
- Figure 10 is a schematic cross-sectional view of the middle B-B of Figure 9.
- the partition flow designed by the invention has no back-mixing spray tray (referred to as tray, see FIG. 1 10 ), and the tray is composed of an upper tray 1 and a lower tray 2, and each tray includes a downcomer 3 , a downcomer 4, a liquid receiving tank 5, a three-dimensional jet mass transfer unit 6 and a liquid guiding tank 9; characterized in that an elongated liquid receiving tank 5 is opened at a horizontal position in the center of the tray, and the liquid receiving tank 5 includes a center
- the length depends on the diameter or chord length of the position, the length of the central receiving tank 51 is the same as the diameter of the tray, and the length of the other elongated receiving tank 52 depends on the chord length of the position of the receiving tank 52.
- a long downcomer 3 is formed between the adjacent two receiving tanks 5, and is divided into a central downcomer 31 and other downcomers 32 according to the position of the downcomer 3, and other downcomers 32 are arranged symmetrically parallel to each other on the left and right sides of the central downtake tank 31; a certain number of liquid descending ports 7 are designed at the bottom of the downcomer 3, each downfall 7 corresponds to a downcomer 4, the downcomer 4 extends through the downcomer 7 and is fixed in the downcomer 3; one or a group of three-dimensional jet mass transfer is arranged between the downcomer 3 and the liquid receiving tank 5.
- a liquid guiding groove 9 is arranged around the cap of the three-dimensional jet mass transfer unit 6;
- the liquid guiding tank 9 is a baffle type liquid guiding trough.
- the liquid guiding trough 9 has walls on three sides, one end is open, and a convex tube 11 is arranged in the middle.
- the size and number of the convex tubes 11 are consistent with the caps on the three-dimensional jet mass transfer unit 6.
- the height of the wall 12 of the other end of the liquid guiding groove corresponding to the open end is equal to the height of the cap.
- the width of the liquid guiding tank 9 is the same as the width occupied by the three-dimensional jet mass transfer unit 6 on the horizontal tray, and is divided into a central liquid guiding tank 91 and a central liquid guiding tank 91 according to the position of the liquid guiding tank 9.
- the other liquid guiding grooves 92 are symmetrical with respect to each other; the upper tray 1 and the lower tray 2 of the present invention have substantially the same shape and structure, and a set of downcomers 4 and lower trays below the downcomers 3 of the upper tray 1
- the misaligned installation is a double-layered split flow non-back mixing jet tray, and any two adjacent trays can be combined with the double-layer tray of the invention, in other words, the tray of the invention
- the position of the upper tray and the lower tray can be interchanged.
- the tray of the present invention is further characterized in that: an elongated liquid level balance tank 8 is disposed at a position perpendicular to the liquid receiving tank 5 at the center of the tray, and the liquid level balance tank S is designed in the middle of the tray, and the liquid level balance tank 8
- the tray structures on the left and right sides are symmetric and symmetrical; according to the diameter of the tower and the amount of liquid, the liquid level balance grooves 8 are designed to be 1 to 5, and the liquid level balance grooves 8 are parallel to each other and vertically arranged with the liquid receiving tank 5;
- the balance tank 8 and the downcomer 3 are in communication; or the level balance tank 8 and the liquid receiving tank 5 are in communication.
- the three-dimensional jet mass transfer unit 6 may be a novel vertical sieve plate, a radial side guide spray tray, a membrane spray no-back mixing tray, a float valve tray or a bubble tray.
- the downcomer 3 has a depth of 10 - 300 ⁇ and a width of 50 to 400; the upper end of the downcomer 3 exceeds the horizontal tray, and the portion beyond the horizontal tray constitutes the overflow ⁇ 10 of the tray, the weir 10
- the height value is the same as the prior art.
- the number of the downcomers 4 is 2 to 20, and the number of downcomers of the upper tray 1 and the lower tray 2 is the same; the depth of the downcomer 4 extending into the downcomer 3 is 0 to 280; The diameter of the liquid pipe 4 is 20% 50% of the width of the downcomer 3; the width of the liquid receiving tank 5 is 50 to 400 mm.
- the downcomer 4 is provided with a liquid guiding hole 41, and the opening position is a portion where the downcomer 4 extends into the interior of the downcomer 3; the shape of the liquid guiding hole 41 may be circular, rectangular or elongated ( Referring to Fig. 1), according to the amount of liquid, 1-8 rows of liquid guiding holes are arranged on each downcomer, and the opening area is 20-80% of the total area of the pipe in which the downcomer 4 extends into the downcomer 3. .
- the difference between the number of the downtake tanks 3 and the liquid receiving tanks 5 is 1, that is, when the downcomers 3 are odd, the liquid receiving tanks 5 are even; the same applies; the number of the descending tanks 3 is 1 to 20 One.
- the downcomer 7 and the downcomer 4 are circular, rectangular or rhombic in cross section; the longitudinal section of the downcomer 3 is rectangular or trapezoidal; the longitudinal section of the liquid receiving tank 5 is rectangular or trapezoidal.
- the depth of the liquid level balance tank 8 is greater than the depth of the downcomer tank 3 by 20 to 300 mm ; when the liquid level balance tank 8 is in communication with the liquid receiving tank 5, the liquid level balance tank The depth of 8 is greater than the depth of the liquid receiving tank 5 by 20 to 300 ⁇ ; the width of the liquid level balancing tank is 200 to 400 ⁇ .
- the tray of the invention comprehensively adopts multiple downcomer structure, liquid guiding tank structure and three-dimensional jet mass transfer unit structure, and adopts multiple downcomer structures, which can realize liquid splitting, improve liquid residence time, avoid mist entrainment and anti-blocking property. Strong, especially suitable for large tower diameter and easy foaming system; Adopting liquid guiding tank structure, it can separate the mass transfer liquid and the non-mass liquid, and realize the liquid without back mixing; Adopt the three-dimensional jet mass transfer unit structure It can make full use of the high efficiency characteristics of gas-liquid jet mass transfer, pay attention to the increase of gas-liquid contact time and space, reduce the entrainment of mist, and make the gas-liquid contact in the mass transfer zone of the whole tray become uniform and flow-free.
- the process of jet mass transfer is the main process, and the effects of drift, stagnation and liquid level gradient are eliminated, and the efficiency of the tray is improved.
- the outstanding advantage of the tray of the invention is that it achieves a uniform concentration of gas and liquid phase in the tray, and has a good improvement effect on the gas-liquid phase bias flow; the liquid-phase phase-occupied area of the downflow zone is small, and the tower section is improved. Utilization; as the liquid flow on the tray becomes shorter, the liquid level will be correspondingly reduced, the liquid level gradient is lowered, the back mixing of the liquid phase on the tray is avoided, and the foaming is also reduced;
- the board also has the characteristics of a small pressure drop required for mass transfer separation equipment.
- a split flow non-backmixing spray tray (see Figures 1-4) is designed.
- the tray is composed of an upper tray 1 and a lower tray 2, and the upper tray 1 includes 2 downcomers 32 and 16 Downcomer 4, 1 central receiving tank 51 and 2 other receiving tanks 52, 4 sets of three-dimensional jet mass transfer unit 6, 2 sets of central liquid guiding tank 91 and 2 sets of other liquid guiding tanks 92; lower tray 2 Including 3 downcomers 3, 16 downcomers 4, 2 liquid receiving tanks 5, 4 sets of three-dimensional jet mass transfer unit 6, two sets of central liquid guiding tank 91 and two sets of other liquid guiding tanks 92; 3.
- the liquid receiving tank 5 adopts a rectangular groove structure;
- the downcomer 4 adopts a cylindrical tube structure;
- the three-dimensional jet mass transfer unit 6 is a novel vertical sieve plate.
- the working principle and process are as follows: the liquid transferred from the upper tray is passed through the downcomer 4 into the liquid receiving tank 5 in the tray, and the liquid in the liquid tank 5 overflows into the liquid.
- the layer tray enters the cap 61 through the bottom gap of the lower portion of the three-dimensional jet mass transfer unit 6, and the gas blown from the lower tray 2 in the cap 61 is in full contact with mass transfer and heat transfer, and the mass transfer liquid passes through.
- the cover hole 61 1 of the cap 61 is sprayed into the liquid guiding tank 9, and flows into the liquid descending tank 3 of the layer from the open end of the liquid guiding tank 9, and flows into the lower tray 2 through the downcomer 4 corresponding to the liquid guiding tank 3.
- the liquid in the liquid receiving tank 5 of the layer tray overflows into the three-dimensional jet mass transfer unit 6 of the tray of the layer, and the gas blown in the cap 61 and the lower tray is Contact mass transfer, heat transfer, and then flow through the liquid guiding tank 9 into the downcomer 4 into the liquid receiving tank 5 in the next set of trays to complete a mass transfer process.
- a split flow non-backmixing jet tray (see Fig. 5-6) is designed, the difference being that the tray is provided in the direction perpendicular to the liquid receiving tray in the middle position of the tray based on the main structure of the embodiment 1.
- 1 long-shaped liquid level balance tank 8 and the liquid level balance tank 8 communicates with the downcomer 3; it is basically the same as the working principle of the embodiment 1, because the liquid level balance tank 8 is provided, and the liquid level is balanced
- the tank 8 is in communication with the downcomer 3, so that the liquid in each of the end downcomers 3 can be evenly distributed into the downcomers 3 after being collected in the leveling tank 8, so that the liquid distribution is uniform and the liquid level is lowered.
- This structure is more suitable for the case where the tower diameter is larger than DN3000.
- a split flow non-backmixing spray tray (see Fig. 7) is designed.
- the structure of the tray is basically the same as that of the second embodiment. The difference is: the level balance tank 8 is connected with the liquid receiving tank 5; the working principle is: liquid level balance The tank 8 communicates with the liquid receiving tank 5, so that the liquid in each liquid receiving tank 5 can be evenly distributed into each liquid receiving tank 5 after being collected in the liquid level adjusting tank 8, so that the liquid distribution is uniform, which is favorable for lowering the liquid level. gradient.
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Abstract
一种分隔流无返混喷射塔盘，该塔盘由上层塔盘和下层塔盘组合而成，每层塔盘均包括降液槽、降液管、受液槽、立体喷射传质单元和导液槽；在塔盘中心的水平位置开有长条形的受液槽，在相邻两个受液槽之间开有长条形的降液槽，在降液槽的底部设计有降液口，每个降液口对应一根降液管，每个降液管伸入并固定在降液槽内；降液槽和受液槽之间有立体喷射传质单元；在立体喷射传质单元帽罩的周围设置导液槽，导液槽为隔流板式导液槽，一个导液槽对应一组立体喷射传质单元；所述上下层塔盘形状结构基本一致，上层塔盘降液槽下边的一组降液管与下层塔盘的一个受液槽相对应，错位安装，组合为双层的分隔流无返混喷射塔盘。
Description
说 明 书
一种分隔流无返混喷射塔盘 技术领域
本发明涉及化学工程中的传热、 传质设备， 具体为一种化工传热、 传质 分离用的分隔流无返混喷射塔盘。 该塔盘尤其适用于处理大液量、 易发泡物 系的工况。
背景技术
塔板作为重要的传质设备元件在化工分离操作中得到广泛应用。 一直以 来人们把幵发的着眼点放在了单体传质部件上， 出现了以单体部件命名的多 种形式的塔板， 如筛孔、 泡罩、 浮阀以及在此基础上改进的导向筛孔、 导向 浮阀等。 单体传质部件的改进与创新， 尽管提升了塔板的点效率， 同时对整 板效率有所改善， 但它并不能从根本上解决整个传质区因错流、 偏流、 滞流 和液面梯度等因素导致的塔板效率下降问题。 从整个塔板传质区域考虑， 错 流、 偏流、 滞流和液面梯度等因素对塔板效率的影响很大， 但至今仍未能很 好的解决。
在处理大液量的精馏或吸收工艺过程中， 往往把塔盘的降液系统设计成 多个降液管， 现有常用的多降液管塔盘， 如国外的 MD筛板， 或国内的 DJ塔 盘， 其主要结构特征是： （1 ) 降液管为矩形槽， 布置在塔盘中间， 降液管的 四周都起溢流作用， 大大增加了溢流堰的长度； （2 ) 降液管悬挂在气相空间， 塔盘上没有受液盘， 增大了塔盘的有效鼓泡面积。 但是现有的多降液管塔盘 仍然存在一些不足， 特别是液体流动过程中的偏流和分布问题比较突出。 其 应用于精熘和吸收过程的塔盘效率较低， 不适用于大液量、 易发泡物系的处 理。 其中的一部分原因是： 现有的多降液管塔盘， 其塔盘上的传质单元主要 是筛板， 也有选用浮阀、 固阔等形式的传质单元， 均为鼓泡传质为主的结构 形式， 在高负荷状态下运转时， 尽管其传质方式由鼓泡态向喷射态转换， 仍 然会产生大量的泡沫， 泡沫在传统淋降式降液系统中往往无法有效分离， 形 成明显气相返混， 而且容易导致降液管液泛， 同时有过量雾沫夹带的现象。
传统的穿流塔板， 也就是没有降液管的多孔塔板， 也称为无溢流塔板。 气液在塔板上呈逆流流动， 由于液体是穿过塔板的部分孔淋降到下一层塔板 上， 因此， 这种塔板又称为淋降塔板。 它的特点是结构简单， 造价低廉， 压 降小， 板间距小， 气体通量大。 但由于操作范围较窄， 弹性较小， 使其在工 业上的应用受到一定的限制。 如果能合理设计， 保证在高效率区运行， 其传 质效率并不低于有降液管的塔板。
多降液管塔盘和穿流塔盘的液体自上向下流动时均为淋降状态， 一方面 在传质过程中产生的大量泡沫会挟带到下一层塔盘， 增加液流强度的同时， 也由于气相夹带返混效应降低了传质效率； 另一方面淋降过程本身也会使得 上层塔盘的液流冲击下层塔盘液面， 造就一些泡沬， 同时还会对受液区造成 一定的冲击漏液， 不能应用于大液量、 易发泡物系的化工过程物料吸收、 精 馏处理。
中国专利 CN101554538A公布了一种多降液管塔盘，其主要结构是含多个 矩形的降液管与延伸元件， 塔盘为单层结构， 该结构塔盘存在液相返混现象， 致使塔板效率较低。 美国专利 （US 6, 059, 934 ) 也报道一种塔板， 它采用了 单层塔盘的多降液管设计， 并把液体导入气液接触腔内， 气液并流传质后进 入到气液分离组件中， 其不足在于气液接触时间较短， 气液分散的接触空间 较小， 当液体流量较大时， 容易出现降液管液泛现象。
以新型垂直筛板为代表的立体喷射传质塔盘具有高效率、 大通量、 适用 于处理易发泡、 易堵的物系， 己经广泛应用于诸多精馏和吸收领域， 但是对 于液气比较大、 塔径较大、 物系发泡较为严重的工业装置， 其应用效果较差， 不能解决在塔径放大过程中产生的液面梯度过大、 气液接触不充分、 液体返 混严重等问题。 另外该传质单元为喷射型传质， 液滴在塔盘空间传质后下落 到塔盘的液面上， 会导致液团冲击， 液面起泡。
上述现有技术塔板由于结构设计的缺陷， 会出现液体返混、 液位梯度大、 液体滞留和液体环流等现象， 或者雾沫夹带严重、 塔效率低下等情形， 无法 根本避免。
发明内容
针对现有技术的不足， 本发明拟解决的技术问题是， 提供一种分隔流无 返混喷射塔盘。 该塔盘综合采用了多降液管结构、 导液槽结构和立体喷射传 质单元结构， 具有传质效率高、 操作弹性大、 通量大、 抗堵性强、 雾沫夹带 小、 实现液体无返混等特点， 可解决现有塔板存在的错流、 偏流、 滞留和液 面梯度大等一系列问题， 大大提升了塔板效率、 产品收率和产品等级， 节能 环保效果明显。
本发明解决所述技术问题的技术方案是， 设计一种分隔流无返混喷射塔 盘， 该塔盘由上层塔盘和下层塔盘组合而成， 每层塔盘均包括降液槽、 降液 管、 受液槽、 立体喷射传质单元和导液槽； 其特征在于在塔盘中心的水平位 置开有长条形的受液槽， 受液槽包括中心受液槽和其他受液槽， 中心受液槽 开在塔盘的中心线上， 其他受液槽对称平行开在中心受液槽的左右两侧， 受 液槽的长度取决于其所处位置的直径或弦长， 中心受液槽的长度与塔盘直径 相同， 其他受液槽的长度取决于该受液槽所处位置的弦长； 在相邻两个受液 槽之间开有长条形的降液槽， 在降液槽的底部设计有降液口， 每个降液口对 应一根降液管， 每个降液管通过降液口伸入并固定在降液槽内； 在降液槽和 受液槽之间安排有立体喷射传质单元； 在立体喷射传质单元帽罩的周围设置 导液槽， 所述导液槽为隔流板式导液槽， 该导液槽设置在立体喷射传质单元 帽罩的周围， 其结构为三面有壁， 一端开口， 中间有凸管， 凸管的尺寸及数 量与立体喷射传质单元上帽罩相一致， 与开口 -端相对应的另一端导液槽的 板壁高度与帽罩等高， 导液槽的开口一端朝向降液槽， 导液槽的宽度与立体 喷射传质单元在水平塔板上所占的宽度相同， 一个导液槽对应一组立体喷射 传质单元； 所述上层塔盘和下层塔盘形状结构基本一致， 上层塔盘降液槽下 边的一组降液管与下层塔盘的一个受液槽相对应， 错位安装， 组合为双层的 分隔流无返混喷射塔盘。
与现有技术相比， 本发明分隔流无返混喷射塔盘具有以下优点：
1、 降液槽、 受液槽均采用长条形结构设计， 且多个降液槽、 多个受液 槽均布在塔盘上， 每个降液槽底部设有多个降液管， 降液管通过降液口伸入 到降液槽内。 多个降液管的设计， 实现液体分流， 抗堵性强； 通过调整降液
槽的深度、 降液管管径、 降液管伸入降液槽的深度可以自由调整塔板上液层 的厚度， 即可调节液体停留时间， 降低发泡， 提高气液分离效率。
2、 降液槽设计为窄条状， 所占塔截面积较小， 特别适用于大液量的工 况， 既能保证全塔板液流下降均匀， 又能保证板上液位的均匀。 与同等工况 下的传统多降液管塔盘及淋降塔板相比， 液位低， 压降小， 消除了气液鼓泡 传质机制。
3、 降液管上幵有导液孔， 其作用是增加气液在降液管中的分离时间， 增加降液管的操作弹性， 降低雾沫夹带。
4、 导液槽的设置， 将已传质和未传质的液体进行隔离， 使发生气液传质 的液体可以直接从导液槽通过降液槽流到下一层塔盘， 避免了与塔盘上的未 发生气液接触的液体返混， 使液体组分浓度与气体组分浓度之间形成最大差 值， 从而大幅提高了传质推动力和塔板效率。
5、 液位平衡槽与降液槽相连通， 使各端降液槽中的液体在液位平衡槽 汇集后， 平均分配到各降液槽中， 使得液体分布均匀， 降低液面梯度。 液位 平衡槽的设计， 解决了传质区的错流、 偏流、 滞流和液面梯度等问题， 提高 塔板效率。
6、 采用立体喷射传质单元充分利用气液喷射传质的高效率特性， 重视气 液接触时间和空间的提升， 降低雾沫夹带， 使之在整个塔板传质区的气液接 触成为均布的、 无错流的、 喷射传质为主的过程， 同时消除偏流、 滞流和液 面梯度的影响， 使塔板效率得到全面提升。
附图说明
图 1是本发明分隔流无返混喷射塔盘一种实施例的上层塔盘俯视结构示 意图。
图 2是本发明分隔流无返混喷射塔盘一种实施例的主视结构示意图， 该 图为图 1中 A-A向剖视图。
图 3是本发明分隔流无返混喷射塔盘一种实施例的下层塔盘俯视结构示 意图。
图 4是本发明分隔流无返混喷射塔盘一种实施例的一组双层塔盘左视结
构示意图。
图 5是本发明分隔流无返混喷射塔盘另一种实施例的一组双层塔盘主结 构示意图， 图中设置了液位平衡槽 8。
图 6是本发明分隔流无返混喷射塔盘另一种实施例的上层塔盘的俯视结 构示意图， 图中液位平衡槽 8与降液槽 3连通。
图 7是本发明分隔流无返混喷射塔盘另一种实施例的上层塔盘的俯视结 构示意图， 图中液位平衡槽 8与受液槽 5连通。
图 8是本发明分隔流无返混喷射塔盘另一种实施例的一组双层塔盘的左 视结构示意图， 图中液位平衡槽 8在塔盘中间放置。
图 9是本发明分隔流无返混喷射塔盘一种实施例的导液槽的俯视结构示 意图。
图 10是图 9中间 B-B剖视结构示意图。
具体实施方式
以下结合实施例及其附图进一步叙述本发明。 具体实施例仅用于进一步 详细说明本发明技术方案， 不限制本申请权利要求的保护范围。
本发明设计的分隔流无返混喷射塔盘 （简称塔盘， 参见图 1 10 )， 该塔 盘由上层塔盘 1和下层塔盘 2组合而成，每层塔盘均包括降液槽 3、降液管 4、 受液槽 5、立体喷射传质单元 6和导液槽 9 ; 其特征在于在塔盘中心的水平位 置开有长条形的受液槽 5， 受液槽 5包括中心受液槽 51和其他受液槽 52， 中 心受液槽 51开在塔盘的中心线上， 其他受液槽 52对称平行开在中心受液槽 51的左右两侧， 长条形受液槽的长度取决于其所处位置的直径或弦长， 中心 受液槽 51的长度与塔盘直径相同， 其他长条形受液槽 52的长度取决于该受 液槽 52所处位置的弦长； 在相邻两个受液槽 5之间开有长条形的降液槽 3， 根据降液槽 3所处的位置分为中心降液槽 31和其他降液槽 32， 其他降液槽 32相互平行对称安排在中心降液槽 31 的左右两侧； 在降液槽 3的底部设计 有一定数量的降液口 7， 每个降液口 7对应一根降液管 4， 降液管 4通过降液 口 7伸入并固定在降液槽 3内； 在降液槽 3和受液槽 5之间安排有一个或 组立体喷射传质单元 6， 在立体喷射传质单元 6的帽罩周围设置导液槽 9 ; 所
述导液槽 9为隔流板式导液槽， 该导液槽 9三面有壁， 一端开口， 中间有凸 管 11， 凸管 11的尺寸及数量与立体喷射传质单元 6上帽罩相一致， 与开口 端相对应的另一端导液槽的板壁 12高度与帽罩等高，安装时导液槽 9的开口 一端朝向降液槽 3， 一组立体喷射传质单元 6对应一个导液槽 9， 导液槽 9的 宽度与立体喷射传质单元 6在水平塔板上所占的宽度相同， 根据导液槽 9所 处的位置分为中心导液槽 91和中心导液槽 91左右两侧相互平行对称的其他 导液槽 92 ; 本发明所述上层塔盘 1和下层塔盘 2形状结构基本一致， 上层塔 盘 1的降液槽 3下边的一组降液管 4与下层塔盘 2的受液槽 5相对应， 错位 安装组合为双层的分隔流无返混喷射塔盘， 相邻任意两层塔盘均可组合成本 发明所述的双层塔盘， 换言之本发明塔盘的上层塔盘与下层塔盘的位置可以 互换。
本发明塔盘的进一步的特征是： 在塔盘中心与受液槽 5相垂直的位置设 置长条形的液位平衡槽 8， 液位平衡槽 S设计在塔盘中间， 液位平衡槽 8左 右两侧的塔盘结构对称一致； 根据塔径及液量的大小， 液位平衡槽 8设计为 1〜5个， 各液位平衡槽 8相互平行且与受液槽 5垂直排列； 液位平衡槽 8和 降液槽 3连通； 或者液位平衡槽 8和受液槽 5连通。
所述立体喷射传质单元 6可以是现有技术中的新型垂直筛板、 径向侧导 喷射塔板、 膜喷射无返混塔板、 浮阀塔板或泡罩塔板。
所述降液槽 3的深度为 10- 300誦， 宽度为 50〜400議； 降液槽 3上端超 出水平塔盘， 超出水平塔盘的部分构成塔盘的溢流堰 10， 溢流堰 10 的高度 取值与现有技术相同。
所述降液管 4的数量为 2〜20个， 上层塔盘 1、 下层塔盘 2的降液管数 量相同； 降液管 4伸入降液槽 3内的深度为 0〜280画； 降液管 4的直径为降 液槽 3宽度的 20% 50%; 受液槽 5的宽度为 50〜400mm。
所述降液管 4上开有导液孔 41， 开孔位置在降液管 4伸入到降液槽 3内 部的部分； 导液孔 41 的形状可以为圆形、 矩形或长条形 （参见图 1 ) , 根据 液量的大小在每个降液管上幵 1-8排导液孔， 开孔面积为降液管 4伸入到降 液槽 3内管道总面积的 20-80%。
每层降液槽 3与受液槽 5的数量相差为 1， 即降液槽 3为奇数时， 受液 槽 5为偶数； 同理亦然； 每层降液槽 3的数量为 1〜20个。
所述降液口 7及降液管 4的横截面是圆形、 矩形或菱形； 降液槽 3的纵 向截面是矩形或梯形； 受液槽 5的纵向截面是矩形或梯形。
当液位平衡槽 8与降液槽 3连通时， 液位平衡槽 8的深度大于降液槽 3 的深度 20〜300mm; 当液位平衡槽 8与受液槽 5连通时， 液位平衡槽 8的深 度大于受液槽 5的深度 20〜300誦； 液位平衡槽的宽度为 200〜400匪。
本发明塔盘综合采用了多降液管结构、 导液槽结构和立体喷射传质单元 结构， 采用多降液管结构， 可以实现液体分流， 提高液体停留时间， 避免雾 沫夹带， 抗堵性强， 尤其适合大塔径、 易发泡物系的工况； 采用导液槽结构， 可将己传质液体及未传质液体进行隔流， 实现液体无返混； 采用立体喷射传 质单元结构可以充分利用气液喷射传质的高效率特性， 重视气液接触时间和 空间的提升， 降低雾沫夹带， 使之在整个塔板传质区的气液接触成为均布的、 无错流的、 喷射传质为主的过程， 同时消除偏流、 滞流和液面梯度的影响， 使塔板效率得到全面提升。
本发明塔盘的突出优点是， 它实现了气液相在塔板的浓度均一， 对气液 相偏流具有很好的改善作用； 降液区所占塔截面积很小， 提高了塔截面的利 用率； 由于液体在塔板上的流动路程变短液位会相应的降低， 降低了液面梯 度， 避免了液相在塔板上的返混现象， 同时还能降低发泡； 这种塔板同样具 有传质分离设备所要求的压降小的特点。
下面给出本发明的具体实施例。
实施例 1
设计一种分隔流无返混喷射塔盘 （参见图 1-4)， 该塔盘由上层塔盘 1和 下层塔盘 2组合而成， 上层塔盘 1包括 2个降液槽 32、 16根降液管 4、 1个 中心受液槽 51和 2个其他受液槽 52、 4组立体喷射传质单元 6、 2组中心导 液槽 91和 2组其他导液槽 92 ;下层塔盘 2包括 3个降液槽 3、 16根降液管 4、 2个受液槽 5、 4组立体喷射传质单元 6、 2组中心导液槽 91和 2组其他导液 槽 92 ; 降液槽 3、 受液槽 5采用矩形槽结构； 降液管 4采用圆筒管式结构；
立体喷射传质单元 6为新型垂直筛板。
其工作原理和过程是： 从上组塔盘传质后的液体通过降液管 4落入本组 塔盘内的受液槽 5内， 受液槽 5中的液体往上溢流进入到该层塔盘， 通过立 体喷射传质单元 6下部的底隙进入帽罩 61， 在帽罩 61 内与下层塔盘 2吹上 来的气体进行充分接触传质、 传热， 而后传质后的液体通过帽罩 61 的罩孔 61 1喷射至导液槽 9， 并从导液槽 9的开口端流入该层的降液槽 3， 通过导液 槽 3对应的降液管 4流入下层塔盘 2的受液槽 5上， 该层塔盘的受液槽 5中 的液体往上溢流至本层塔盘的立体喷射传质单元 6内，在帽罩 61内与下组塔 盘吹上来的气体进行接触传质、 传热， 而后再通过导液槽 9流入降液管 4进 入下一组塔盘内的受液槽 5， 完成一个传质过程。
实施例 2
设计一种分隔流无返混喷射塔盘（参见图 5-6 )， 区别是该塔盘在实施例 1 的主要结构基础上， 在塔盘的中间位置与受液盘相垂直的方向设置有 1 个 长条形液位平衡槽 8， 且液位平衡槽 8与降液槽 3相连通； 其与实施例 1的 工作原理基本相同， 因设置了液位平衡槽 8， 且该液位平衡槽 8与降液槽 3 相连通， 因而可以使各端降液槽 3中的液体在液位平衡槽 8汇集后， 平均分 配到各降液槽 3中， 使得液体分布均匀， 降低液面梯度。 该结构更适合于塔 径大于 DN3000的情形。
实施例 3 :
设计一种分隔流无返混喷射塔盘（参见图 7 )， 塔盘结构与实施例 2基本 相同， 区别是： 液位平衡槽 8与受液槽 5相连通； 工作原理是： 液位平衡槽 8与受液槽 5相连通， 可以使各端受液槽 5中的液体在液位平衡槽 8汇集后， 平均分配到各受液槽 5中， 使得液体分布均匀， 有利于降低液面梯度。
本发明未述及之处适用于现有技术。
Claims
1. 一种分隔流无返混喷射塔盘， 该塔盘由上层塔盘和下层塔盘组合而 成， 每层塔盘均包括降液槽、 降液管、 受液槽、 立体喷射传质单元和导液槽； 其特征在于在塔盘中心的水平位置开有长条形的受液槽， 受液槽包括中心受 液槽和其他受液槽， 中心受液槽开在塔盘的中心线上， 其他受液槽对称平行 幵在中心受液槽的左右两侧，受液槽的长度取决于其所处位置的直径或弦长， 中心受液槽的长度与塔盘直径相同， 其他受液槽的长度取决于该受液槽所处 位置的弦长； 在相邻两个受液槽之间开有长条形的降液槽， 在降液槽的底部 设计有降液口， 每个降液口对应一根降液管， 每个降液管通过降液口伸入并 固定在降液槽内； 在降液槽和受液槽之间安排有立体喷射传质单元； 在立体 喷射传质单元帽罩的周围设置导液槽， 所述导液槽为隔流板式导液槽， 该导 液槽设置在立体喷射传质单元帽罩的周围， 其结构为三面有壁， 一端幵口， 中间有凸管， 凸管的尺寸及数量与立体喷射传质单元上帽罩相一致， 与开口 一端相对应的另一端导液槽的板壁高度与帽罩等高， 导液槽的开口一端朝向 降液槽， 导液槽的宽度与立体喷射传质单元在水平塔板上所占的宽度相同， 一个导液槽对应一组立体喷射传质单元； 所述上层塔盘和下层塔盘形状结构 基本一致， 上层塔盘降液槽下边的一组降液管与下层塔盘的一个受液槽相对 应， 错位安装， 组合为双层的分隔流无返混喷射塔盘。
2、 根据权利要求 1所述的分隔流无返混喷射塔盘， 其特征在于在每层塔 盘中， 在塔盘中心与受液槽相垂直的方向设置有 1-5个液位平衡槽， 液位平 衡槽左右两侧的塔盘结构对称一致； 所述液位平衡槽与降液槽连通、 或者液 位平衡槽与受液槽连通， 且液位平衡槽的深度大于降液槽的深度。
3、根据权利要求 1所述的分隔流无返混喷射塔盘， 其特征在于降液管伸 入到降液槽内的部分开有设计数量的导液孔。
4. 根据权利要求 1所述的分隔流无返混喷射塔盘，其特征在于所述降液 槽的深度为 10-300mm， 降液槽的宽度为 50〜400誦；所述降液管的数量为 2〜 20 个， 降液管的直径为降液槽宽度的 20 50% ; 所述受液槽的宽度为 50〜
400mm, 受液槽的深度为 50〜400mm。
5.根据权利要求 2所述的分隔流无返混喷射塔盘， 其特征在于所述液位 平衡槽的深度大于降液槽的深度 20〜300顏； 液位平衡槽的宽度为 200〜 400mm。
6.根据权利要求 1或 4所述的分隔流无返混喷射塔盘， 其特征在于所述 降液口及降液管的横截面是圆形、 矩形或菱形； 降液槽的纵向截面是矩形或 梯形； 受液槽的纵向截面是矩形或梯形。
7.根据权利要求 1所述的分隔流无返混喷射塔盘， 其特征在于所述立体 喷射传质单元为新型垂直筛板、 径向侧导喷射塔板、 膜喷射无返混塔板、 浮 阀塔板或泡罩塔板。
8.根据权利要求 3所述的分隔流无返混喷射塔盘， 其特征在于每个降液 管上开有 1 -8排导液孔， 且导液孔开孔面积为降液管伸入到降液槽内管道总 面积的 20-80%。
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| CN102961888B (zh) * | 2012-12-04 | 2014-09-17 | 天津市创举科技有限公司 | 一种分隔流无返混喷射塔盘 |
| CN103463828B (zh) * | 2013-09-05 | 2015-09-02 | 中国海洋石油总公司 | 垂直吹膜塔板 |
| CN108479684B (zh) * | 2018-04-24 | 2020-04-14 | 天津市天屹化工技术开发有限公司 | 一种圆形分流浮阀塔盘 |
| CN110871021B (zh) * | 2018-08-30 | 2022-03-08 | 中国石油化工股份有限公司 | 气液传质装置 |
| CN111375354B (zh) * | 2018-12-31 | 2022-06-07 | 中国石油化工股份有限公司 | 一种气液传质设备 |
| CN115212601B (zh) * | 2022-07-18 | 2024-07-26 | 厦门市凯讯科技有限公司 | 小塔板间距的筛板塔 |
| CN115253354B (zh) * | 2022-07-25 | 2023-08-18 | 山东凯斯达机械制造有限公司 | 一种筛板塔板单元组件、汽提塔式装置及粮油深加工方法 |
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