CN107899535B - Gas jet flow distributed tower plate without amplification effect and design method thereof - Google Patents
Gas jet flow distributed tower plate without amplification effect and design method thereof Download PDFInfo
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Abstract
本发明提供一种无放大效应的气体射流分散式塔板及其设计方法。该塔板包括一基板，该基板为盲板；基板下方设置有弧形气体导流板；基板的两侧或中央设有升气管，在升气管的侧壁顶部连接有平行于基板的布气管线，布气管线由至少一根布气管组成；基板上没有升气管的另外两侧分别设有降液板和溢流堰，降液板在基板上方，与基板之间有间隙，溢流堰与基板相连并高于基板；布气管下部开设有射流孔。本发明在塔板上设置布气管线，平行于塔板均匀分布，由于气体出口的压力处处相等，可保证从射流孔喷射出的气体不受液体分布的影响，减小液体面落差引起的汽液分布不均。通过布气管线的合理布局，使气体均匀喷射到塔板上，通过剪切液相，促进气液相传质并消除放大效应。
The invention provides a gas jet dispersed tray without amplification effect and a design method thereof. The tower plate includes a base plate, which is a blind plate; an arc-shaped gas deflector is arranged under the base plate; gas risers are arranged on both sides or the center of the base plate, and a gas distribution pipe parallel to the base plate is connected to the top of the side wall of the riser tube. Pipeline, gas distribution pipeline is composed of at least one gas distribution pipe; the other two sides of the base plate without air riser are respectively provided with a downcomer plate and an overflow weir, the downcomer plate is above the base plate, and there is a gap between the base plate and the overflow weir It is connected with the substrate and is higher than the substrate; the lower part of the air distribution pipe is provided with jet holes. In the present invention, gas distribution pipelines are arranged on the tray, which are evenly distributed parallel to the tray. Since the pressure of the gas outlet is equal everywhere, it can ensure that the gas ejected from the jet hole is not affected by the liquid distribution, and the vapor caused by the drop of the liquid surface can be reduced. Liquid distribution is uneven. Through the reasonable layout of the gas distribution pipeline, the gas is evenly sprayed onto the tray, and the gas-liquid phase mass transfer is promoted and the amplification effect is eliminated by shearing the liquid phase.
Description
技术领域technical field
本发明涉及一种无放大效应的气体射流分散式塔板及其设计方法，属于化工及炼油技术领域。The invention relates to a gas jet dispersed tray without amplification effect and a design method thereof, belonging to the technical field of chemical industry and oil refining.
背景技术Background technique
一、传统板式塔的先天弊端和放大效应问题1. The inherent disadvantages and amplification effect of the traditional plate tower
蒸馏塔具有规模经济的特性，装置大型化是降低生产成本、提高规模效益的主要途径。塔设备规模扩大以后，塔内的非理想流动和不均匀的汽液分散加剧，将导致处理能力、塔板效率、操作弹性等技术指标的显著降低。Distillation towers have the characteristics of economies of scale, and large-scale equipment is the main way to reduce production costs and improve economies of scale. After the scale of the tower equipment is enlarged, the non-ideal flow and uneven vapor-liquid dispersion in the tower will intensify, which will lead to a significant reduction in technical indicators such as processing capacity, tray efficiency, and operating flexibility.
常规大型板式塔因为汽液流动传质方式存在先天弊端：塔中气相沿着竖直方向由下至上通过塔板，液相在塔板上由一端向另一端水平流动，然后由降液管导流到下一层塔板，气体必须穿过塔板和液层才能进入上层空间。但是液体在板上流动时，受塔板、塔壁和气相流动的阻力，沿液体流向会存在液面落差，形成液层的不均匀分布。因为气体密度远小于液体密度，惯性小，所以液体的不均匀分布必然会导致气体的不均匀分布。这样气液不良分布将更为加剧，使得入口液层较厚，气体量少，易发生泄漏，而出口液层较薄，气体量大，易发生雾沫夹带，气、液两相不能充分接触，严重的甚至威胁生产安全。这是传统错流式塔板普遍存在的问题。Conventional large-scale tray towers have inherent disadvantages due to the vapor-liquid flow and mass transfer method: the gas phase in the tower passes through the trays from bottom to top in the vertical direction, and the liquid phase flows horizontally from one end to the other end of the trays, and then is guided by the downcomer. Flowing to the next tray, the gas must pass through the tray and the liquid layer to enter the upper space. However, when the liquid flows on the plate, due to the resistance of the plate, the tower wall and the flow of the gas phase, there will be a drop in the liquid level along the liquid flow direction, forming an uneven distribution of the liquid layer. Because the gas density is much smaller than the liquid density, the inertia is small, so the uneven distribution of the liquid will inevitably lead to the uneven distribution of the gas. In this way, the poor distribution of gas and liquid will be more aggravated, so that the inlet liquid layer is thicker, the gas volume is small, and leakage is easy to occur, while the outlet liquid layer is thinner, the gas volume is large, and mist entrainment is easy to occur, and the gas and liquid phases cannot be fully contacted. , seriously even threaten production safety. This is a common problem with traditional cross-flow trays.
随着塔径扩大，高液相负荷下液流的惯性巨大，而气流开孔数也成倍增加，不仅加剧了液流阻力，流动随机性也显著增强，板上操作状况存在着极大的不确定性，不能像小塔一样准确预测。塔板空间的气液分散受传递动力学的调控，表现出严重的水力学不稳定(随机)性，塔板出现沟流、股流和返混等非理想操作，泄漏和雾沫夹带甚至可以同时出现且呈数量级猛增，造成板效率和处理能力降低、压降增加和稳定性变差，这就是放大效应问题，塔设备规模扩大会加剧板式塔的气液不均匀分布，恶化塔板操作性能。With the expansion of the tower diameter, the inertia of the liquid flow under high liquid phase load is huge, and the number of gas flow openings also doubles, which not only intensifies the resistance of the liquid flow, but also significantly enhances the randomness of the flow. There are great differences in the operating conditions on the board. Uncertainty, cannot be predicted as accurately as a small tower. The gas-liquid dispersion in the tray space is regulated by the transfer dynamics, showing serious hydraulic instability (randomity), non-ideal operations such as channel flow, stream flow, and back-mixing in the tray, leakage and mist entrainment can even Simultaneous occurrence and a sharp increase in order of magnitude, resulting in reduced plate efficiency and processing capacity, increased pressure drop, and poor stability. This is the problem of amplification effects. The expansion of the scale of tower equipment will aggravate the uneven distribution of gas and liquid in the plate tower and deteriorate the operation of the plate. performance.
二、多溢流板式塔的设计困难2. The design of multi-overflow plate tower is difficult
目前主要采用多溢流设计处理放大效应，即减少流道长度，降低液流强度，以降低塔板上液流的惯性和液层的波动程度。但多溢流设计也面临着液相在多根降液管内的均匀分配，以及气相在降液管间鼓泡区内的均匀分配问题。多溢流液体的分配与塔板结构的对称性直接相关，其中偏心式降液管的对称性就比中心降液管和侧降液管差得多，它的左右两侧出口堰长不等，降液管底隙出口面积大小和流出阻力也相同，容易造成气液偏流。对溢流通道数大于等于三溢流的塔板，由于塔板本身结构的不对称性，从降液管下来的液体就更难进行均匀分布。At present, the multi-overflow design is mainly used to deal with the amplification effect, that is, to reduce the length of the flow channel and the intensity of the liquid flow, so as to reduce the inertia of the liquid flow on the tray and the fluctuation of the liquid layer. However, the multi-overflow design also faces the problem of uniform distribution of liquid phase in multiple downcomers and uniform distribution of gas phase in the bubbling area between downcomers. The distribution of multi-overflow liquid is directly related to the symmetry of the tray structure, and the symmetry of the eccentric downcomer is much worse than that of the central downcomer and side downcomer, and the lengths of the outlet weirs on the left and right sides are not equal , the outlet area of the downcomer bottom gap and the outflow resistance are also the same, which is easy to cause gas-liquid drift. For trays with overflow channels greater than or equal to three overflows, due to the asymmetry of the tray itself, it is more difficult for the liquid coming down from the downcomer to be evenly distributed.
需要注意的是，多溢流设计中气体分布的均匀性仍然由液层分布决定，大塔径对两相的分散都是不利的，而且液相与气相的非理想分布作用彼此相互影响，会进一步加剧非均匀分配效果。多溢流虽然能够实现塔的放大设计，但并未解决塔板自身的非理想操作问题，只能靠增加塔板数，提高安全因子来弥补。It should be noted that the uniformity of gas distribution in the multi-overflow design is still determined by the distribution of the liquid layer. The large diameter of the tower is not conducive to the dispersion of the two phases, and the non-ideal distribution of the liquid phase and the gas phase affects each other, which will further Exacerbates the non-uniform distribution effect. Although multiple overflows can realize the enlarged design of the column, it does not solve the non-ideal operation problem of the tray itself, and can only be compensated by increasing the number of trays and improving the safety factor.
现有专利中，“汽液接触系统及方法”(专利号US3410540)、“一种增大处理能力的MD塔板”(专利号：US5,318,732)、“一种带有导流板的MD塔板”(专利号：US5,098,615)、“一种带有防冲击泄漏受液盘的MD塔板”(专利号：US5,209,875)等多项专利就是采用多溢流以及悬挂式降液管来对待板式塔的放大效应问题。因为液层在塔板上始终存在液面落差，而且悬挂式降液管的泄漏严重，会激化大塔的放大效应，塔板效率也不高，所以这些专利在改善各鼓泡区的气液分布作用仍然有限。Among the existing patents, "Vapor-liquid Contact System and Method" (Patent No. US3410540), "An MD Tray with Increased Processing Capacity" (Patent No.: US5,318,732), "A MD Tray with a Baffle Tray" (Patent No.: US5,098,615), "An MD Tray with an Anti-Shock Leakage Receiver" (Patent No.: US5,209,875) and many other patents use multiple overflows and suspended downcomers Tube to deal with the amplification effect of tray tower. Because the liquid layer always has a liquid level drop on the tray, and the serious leakage of the suspended downcomer will intensify the amplification effect of the large tower, and the efficiency of the tray is not high, so these patents are improving the gas-liquid distribution in each bubbling area The role is still limited.
发明内容Contents of the invention
为解决上述问题，本发明的目的在于提供一种无放大效应的气体射流分散式塔板，可以使气体均匀射流到一个没有液面落差的液层，从根本上消除放大效应的先天弊端，使气液两相分布更加均匀，提高塔板的传质效率和处理能力。In order to solve the above problems, the object of the present invention is to provide a gas jet dispersion tray without amplification effect, which can make the gas evenly jet to a liquid layer without liquid level drop, fundamentally eliminate the inherent disadvantages of amplification effect, and make The gas-liquid two-phase distribution is more uniform, which improves the mass transfer efficiency and processing capacity of the tray.
为达到上述目的，本发明提供了一种无放大效应的气体射流分散式塔板，其中：该塔板包括一基板，该基板为盲板；In order to achieve the above object, the present invention provides a gas jet dispersion type tray without amplification effect, wherein: the tray includes a base plate, and the base plate is a blind plate;
基板下部设置有弧形气体导流板；The lower part of the substrate is provided with an arc-shaped gas deflector;
基板的两侧或中央设有升气管，并且，在升气管的侧壁顶部连接有平行于基板的布气管线，布气管线由至少一根布气管组成；Air risers are provided on both sides or in the center of the base plate, and an air distribution pipeline parallel to the base plate is connected to the top of the side wall of the air riser, and the air distribution pipeline is composed of at least one air distribution pipe;
基板上没有升气管的另外两侧分别设有降液板和溢流堰，降液板和塔壁围成降液管，可以将上层基板流下来的液体导流到这层基板上，溢流堰在与降液板位置对称的另外一侧，与基板相连并高于基板，可以在基板上保持一定厚度的液层，使得气、液相能够充分接触传质，完成传质的液体流过溢流堰后降落到下层塔板上；There are downcomer plates and overflow weirs on the other two sides of the base plate where there is no riser. The weir is on the other side symmetrical to the downcomer plate. It is connected to the substrate and is higher than the substrate. It can maintain a liquid layer of a certain thickness on the substrate, so that the gas and liquid phases can fully contact the mass transfer, and the liquid that completes the mass transfer flows through. After overflowing the weir, it falls to the lower tray;
布气管下部开设有射流孔。The lower part of the gas distribution pipe is provided with a jet hole.
与传统塔板气体由下而上穿过塔板的设计格局不同，本发明在塔板上设置布气管线，平行于塔板均匀分布，由于气体出口的压力处处相等，可以保证从射流孔喷射出的气体不受液体分布的影响。通过布气管线的合理布局，使气体均匀喷射到塔板上，并通过剪切液相，减小液体惯性对分布的影响，可以使气体不受液面落差的影响均匀喷射进入液层，进而大大增加相界面积。同时彻底消除塔板泄漏，大大降低雾沫夹带，消除放大效应，极大的提高塔板的传质效率和处理能力。Different from the design pattern of the traditional tray gas passing through the tray from bottom to top, the present invention arranges gas distribution pipelines on the tray, which are evenly distributed parallel to the tray. Since the pressure of the gas outlet is equal everywhere, it can ensure that the gas is injected from the jet hole. The outgoing gas is not affected by the liquid distribution. Through the reasonable layout of the gas distribution pipeline, the gas is evenly sprayed onto the tray, and the influence of the liquid inertia on the distribution is reduced by shearing the liquid phase, so that the gas can be sprayed evenly into the liquid layer without being affected by the liquid level drop, and then Greatly increase the phase boundary area. At the same time, the leakage of the tray is completely eliminated, the entrainment of mist is greatly reduced, the amplification effect is eliminated, and the mass transfer efficiency and processing capacity of the tray are greatly improved.
在上述无放大效应的气体射流分散式塔板中，溢流堰与降液板位置对称，作用是保持一定厚度的液层，液体越过溢流堰流出，可以降落到下一层基板上。In the above-mentioned gas jet dispersion tray without amplification effect, the overflow weir is symmetrical to the downcomer plate, and its function is to maintain a liquid layer of a certain thickness. The liquid flows out over the overflow weir and can fall to the next layer of substrate.
在上述无放大效应的气体射流分散式塔板中，塔板设置在塔设备内部，其基板水平设置。基板上不开孔，为盲板；优选地，基板下部设置有弧形气体导流板，液体只能从降液管流入下层塔板，从而彻底解决了设备放大后泄漏量猛增的难题，并且塔板上的液流也不会受到鼓泡孔与泄漏孔的影响，可以更均匀地流过塔板。同时当气体携带部分液滴向上流动的过程中，由于气体惯性力的作用，塔板上的布气管线会起到一定的捕沫作用，加上塔板下方的导流板对雾沫夹带的捕集，塔设备的雾沫夹带也会大大的降低，从而极大地降低了放大效应。同时，气体由上而下进入塔板，可减小降液管中的气体夹带并降低塔板间距。图2a中箭头所指示的高出来的竖板是降液板，降液板与塔壁围成一个弓形管腔叫降液管，可以把上面一层下来的液体引到基板上。In the above-mentioned gas jet dispersion type tray without amplification effect, the tray is arranged inside the tower equipment, and its base plate is arranged horizontally. There are no holes on the base plate, which is a blind plate; preferably, the lower part of the base plate is provided with an arc-shaped gas deflector, and the liquid can only flow from the downcomer to the lower tray, thus completely solving the problem of a sharp increase in leakage after the equipment is enlarged. And the liquid flow on the tray will not be affected by the bubbling holes and leakage holes, and can flow through the tray more evenly. At the same time, when the gas carries part of the liquid droplets upward, due to the action of the gas inertia force, the gas distribution pipeline on the tray will play a certain role in catching foam, and the deflector below the tray will prevent the entrainment of mist. The entrainment of mist in the tower equipment will also be greatly reduced, thus greatly reducing the amplification effect. At the same time, the gas enters the tray from top to bottom, which can reduce the gas entrainment in the downcomer and reduce the spacing between the trays. The raised vertical plate indicated by the arrow in Figure 2a is the downcomer plate, and the downcomer plate and the tower wall form an arcuate cavity called the downcomer, which can lead the liquid from the upper layer to the base plate.
在上述塔板中，升气管可以为基板侧面的弓形空腔形成的，也可以为单独设置的管，优选为基板侧面的弓形空腔形成。升气管的数量苦役为一个或数个。In the above-mentioned trays, the gas riser can be formed by an arcuate cavity on the side of the substrate, or can be a separate tube, preferably formed by an arcuate cavity on the side of the substrate. The number of chimneys is one or several.
塔设备整体上一般为圆柱形，基板为方形，其侧面与塔设备的内壁之间会有空腔，从截面上看，该空腔为弓形。这部分空气可以直接用作升气管，即升气管为基板侧面的弓形空腔所形成，并且，可以在升气管的顶部设置顶板。顶板的形状可以根据需要设置。顶板为平面时，结构简单，但对气体没有导向作用，气流方向改变会造成边界层分离，并在顶部形成驻点，压降大，通常用于小气量(速)；顶板为弧形时，对气体有导向作用，压降小，但加工有难度，通常用于大气量(速)。The tower equipment is generally cylindrical as a whole, and the base plate is square. There will be a cavity between its side and the inner wall of the tower equipment. Seen from the cross section, the cavity is bow-shaped. This part of the air can be directly used as the air riser, that is, the air riser is formed by the arcuate cavity on the side of the substrate, and a top plate can be arranged on the top of the air riser. The shape of the top plate can be set as required. When the top plate is flat, the structure is simple, but it has no guiding effect on the gas. The change of the airflow direction will cause the boundary layer to separate, and a stagnation point will be formed on the top. The pressure drop is large, and it is usually used for small gas volume (velocity); when the top plate is curved, It has a guiding effect on the gas, the pressure drop is small, but it is difficult to process, and it is usually used for large volume (speed).
根据本发明的具体实施方案，升气管的空腔侧壁上可以设置开孔，升气管与布气管线通过开孔连通。According to a specific embodiment of the present invention, openings may be provided on the cavity side wall of the air riser, and the air riser communicates with the air distribution pipeline through the openings.
根据本发明的具体实施方案，升气管的空腔侧壁与基板的夹角α优选为90°-145°，如图1所示。α角度越大，对气流的导向作用越明显，能够避免流体边界层分离，减小压降。并且升气管的空腔侧壁与基板的结合处优选设有圆弧倒角。According to a specific embodiment of the present invention, the angle α between the cavity side wall of the air riser and the base plate is preferably 90°-145°, as shown in FIG. 1 . The larger the α angle, the more obvious the guiding effect on the airflow, which can avoid the separation of the fluid boundary layer and reduce the pressure drop. In addition, arc chamfering is preferably provided at the joint between the cavity side wall of the air riser and the base plate.
根据本发明的具体实施方案，对于直径≥2m的塔设备，升气管中可以设置一个或多个分布板，将气流均匀导入布气管线。分布板的作用类似跑道，能够使气相均匀分配进入各布气管，避免气流因为边壁效应主要进入中心布气管。According to a specific embodiment of the present invention, for tower equipment with a diameter ≥ 2m, one or more distribution plates may be arranged in the air riser to guide the air flow evenly into the air distribution pipeline. The function of the distribution plate is similar to that of a runway, which can evenly distribute the gas phase into each air distribution pipe, and prevent the air flow from mainly entering the central air distribution pipe due to the side wall effect.
根据本发明的具体实施方案，当升气管设置在基板两侧的弓形区时，两侧的升气管分别与布气管连接，一根布气管的两端分别与两侧的一根升气管连接，各布气管等长。According to a specific embodiment of the present invention, when the air risers are arranged in the arcuate regions on both sides of the substrate, the air risers on both sides are respectively connected to the air distribution pipes, and the two ends of an air distribution pipe are respectively connected to an air riser on both sides, Each cloth trachea is equal in length.
根据本发明的具体实施方案，升气管的顶部水平总截面积与布气管线的水平总截面积相等，即升气管的顶部水平总截面积与(所有)布气管的水平总截面积相等，以保证在同样的气体流量下具有相近的气速。其中，升气管的顶部水平总截面积是把两侧的升气管都计算在内。According to a specific embodiment of the present invention, the top horizontal total cross-sectional area of the air riser is equal to the horizontal total cross-sectional area of the air distribution pipeline, that is, the top horizontal total cross-sectional area of the air riser is equal to the horizontal total cross-sectional area of (all) air distribution pipes, so that Guaranteed to have similar gas velocity under the same gas flow. Wherein, the horizontal total cross-sectional area of the top of the chimney is to take the chimneys on both sides into account.
根据本发明的具体实施方案，当布气管线有多根布气管时，在基板上位于相邻两根布气管的中间位置处设置射流挡板，射流挡板下部优选开有液体连通孔。射流挡板类似水床中的阻波器，可以避免液体冲击形成振荡，设立连通孔可保证基板上处处液位相同，起到连通器的作用。这两者将大装置分隔成彼此连通的小区，可保持大型装置中水面的均匀性，避免放大效应。According to a specific embodiment of the present invention, when the gas distribution pipeline has multiple gas distribution pipes, a jet baffle is provided on the base plate at the middle position between two adjacent air distribution pipes, and the lower part of the jet baffle is preferably provided with a liquid communication hole. The jet baffle is similar to the wave trap in the water bed, which can avoid the vibration caused by the impact of the liquid, and the establishment of communication holes can ensure the same liquid level everywhere on the substrate, and play the role of a connector. These two divide the large device into interconnected cells, which can maintain the uniformity of the water surface in the large device and avoid the amplification effect.
根据本发明的具体实施方案，布气管线可以采用等径或者不等径的直管或者环管。布气管的排布可以与液流方向垂直或平行，或者，按照圆环状或放射状排布。布气管的截面形状可以为圆形、圆锥形、椭圆形或矩形，优选地，布气管壁厚为2-8mm。According to a specific embodiment of the present invention, the gas distribution pipeline may adopt straight pipes or circular pipes with equal or unequal diameters. The air distribution pipes can be arranged vertically or parallel to the liquid flow direction, or arranged in a circular or radial manner. The cross-sectional shape of the air distribution pipe can be circular, conical, oval or rectangular. Preferably, the wall thickness of the air distribution pipe is 2-8mm.
图2a-图2j为各种类型的塔板结构示意图。其中，图2a为两侧弓形空腔升气管连接平行布气管的结构图，布气管线与液流方向垂直，液流方向指向堰板；图2b为两侧弓形空腔升气管连接主布气管和平行支布气管的结构图，主布气管方向与液流方向垂直，支布气管平行液流方向；图2c为两侧圆管形升气管连接主布气管和平行支布气管的结构图，主布气管方向与液流方向垂直，支布气管平行液流方向；图2d为两侧圆管形升气管连接主布气管和环形支布气管的结构图，主布气管为直管，各级支布气管为同心圆环管；图2e为两侧圆管形升气管连接主布气管和环形支布气管的结构图，主布气管为十字形，各级支布气管为同心圆环管；图2f为两侧圆管形升气管连接主布气管和辐射状支布气管的结构图，各级支布气管为直径由小变大的直圆管，呈辐射状分布；图2g为两侧圆管形升气管连接主布气管和辐射状支布气管的结构图，各级支布气管为直径由小变大的直三角形管，呈辐射状分布；图2h为两侧多根升气管连接平行布气管的结构图，每根升气管都对应一根布气管；图2i为中心升气管连接主布气管和平行支布气管的结构图，升气管在基板中心竖直向上，主布气管与液流方向平行，支布气管垂直液流方向且管长由中间向两边依次递减；图2j为中心升气管连接平行支布气管的结构图，升气管竖直向上，主体为矩形，顶部为半圆管形，与液流方向平行，支布气管垂直液流方向且管长由中间向两边依次递减。2a-2j are schematic diagrams of various types of tray structures. Among them, Fig. 2a is a structural diagram of the arc-shaped cavity ascending pipes on both sides connected to parallel air distribution pipes, the gas distribution pipeline is perpendicular to the liquid flow direction, and the liquid flow direction points to the weir plate; Fig. 2b is the arch-shaped cavity ascending pipes on both sides connected to the main air distribution pipe And the structure diagram of the parallel air distribution pipe, the direction of the main air distribution pipe is perpendicular to the direction of the liquid flow, and the distribution air pipe is parallel to the direction of the liquid flow; The direction of the main air distribution pipe is perpendicular to the direction of the liquid flow, and the branch air pipe is parallel to the direction of the liquid flow; Figure 2d is a structural diagram of the connection of the main air distribution pipe and the annular branch air pipe by the circular tube-shaped ascending pipes on both sides. The main air distribution pipe is a straight pipe. The distribution air pipe is a concentric ring pipe; Figure 2e is a structural diagram of the connection of the circular pipe-shaped air pipes on both sides to the main air distribution pipe and the annular distribution air pipe. The main air distribution pipe is cross-shaped, and the distribution air pipes at all levels are concentric ring pipes; Figure 2f is a structural diagram of the circular tube-shaped air risers on both sides connecting the main air distribution pipe and the radial distribution air pipes. The structural diagram of the circular tube-shaped air riser connecting the main air distribution pipe and the radial air distribution pipes. The distribution air pipes at all levels are right triangle tubes with diameters that change from small to large, distributed in a radial shape; Figure 2h shows the connection of multiple air risers on both sides The structural diagram of parallel air distribution pipes, each air riser corresponds to one air distribution pipe; Figure 2i is the structural diagram of the central air riser connecting the main air distribution pipe and the parallel branch air distribution pipes, the air riser is vertically upward in the center of the substrate, the main air distribution pipe and The direction of the liquid flow is parallel, the distribution air pipe is perpendicular to the liquid flow direction, and the length of the pipe decreases from the middle to both sides; Figure 2j is a structural diagram of the central air riser connecting the parallel distribution air pipes, the air riser is vertical upward, the main body is rectangular, and the top is semicircle Tubular shape, parallel to the direction of liquid flow, the branching trachea is perpendicular to the direction of liquid flow, and the length of the tube decreases from the middle to both sides.
根据本发明的具体实施方案，射流孔的水平投影形状可以为圆形、正方形或矩形。射流孔可以为等径通孔或缩径通孔；图3e为圆柱形射流孔和圆锥形射流孔的示意图；优选地，所述射流孔为锥角β(如图3e所示)为0-45°的缩径通孔；更优选地，射流孔的直径为2-10mm。According to a specific embodiment of the present invention, the horizontal projection shape of the jet hole may be a circle, a square or a rectangle. The jet hole can be an equal diameter through hole or a reduced diameter through hole; Fig. 3 e is a schematic diagram of a cylindrical jet hole and a conical jet hole; preferably, the jet hole is a cone angle β (as shown in Fig. 3 e) is 0- 45° reduced-diameter through hole; more preferably, the diameter of the jet hole is 2-10mm.
图3a-图3d为布气管及射流孔的结构示意图。其中，图3a为圆形布气管，管上开有圆柱形通孔作为射流孔；图3b为矩形布气管，管上开有圆柱形通孔作为射流孔；图3c为圆形布气管，管上开有长条形通孔作为射流孔；图3d为圆形布气管，管上开有圆形通孔作为射流孔，并且下方设置有圆形喷嘴，喷嘴可以连接有弯头，弯头位于布气管内部。3a-3d are structural schematic diagrams of the air distribution pipe and jet holes. Among them, Figure 3a is a circular air distribution pipe with a cylindrical through hole as a jet hole; Figure 3b is a rectangular air distribution pipe with a cylindrical through hole as a jet hole; Figure 3c is a circular air distribution pipe with a pipe There is a strip-shaped through hole as a jet hole on the top; Figure 3d is a circular air distribution pipe with a circular through hole as a jet hole on the tube, and a circular nozzle is provided below. The nozzle can be connected with an elbow, and the elbow is located at Inside the air duct.
根据本发明的具体实施方案，布气管的射流孔可以采用三角形叉排方式，孔心距为孔径的1.5-10倍；优选地，在排列多根的布气管上，沿垂直布气管的方向向下开设1-5排射流孔。According to a specific embodiment of the present invention, the jet holes of the air distribution pipe can adopt a triangular fork arrangement, and the hole center distance is 1.5-10 times of the aperture; 1-5 rows of jet orifices are provided below.
根据本发明的具体实施方案，射流孔下可以安装有垂直于布气管的喷嘴；喷嘴上缘与射流孔平齐，或者伸入到布气管中心位置，连接一段水平管段。喷嘴可以为圆柱形或圆锥形。喷嘴在布气管外的长度可以控制为喷嘴直径的1-8倍，这样可以减小气体的发散，从而使更多的气体动能转化为界面能，提高传质效率。According to the specific embodiment of the present invention, a nozzle perpendicular to the air distribution pipe can be installed under the jet hole; the upper edge of the nozzle is flush with the jet hole, or extends into the center of the air distribution pipe to connect a horizontal pipe section. Nozzles can be cylindrical or conical. The length of the nozzle outside the gas distribution pipe can be controlled to be 1-8 times the diameter of the nozzle, which can reduce the divergence of the gas, so that more kinetic energy of the gas can be converted into interface energy, and the mass transfer efficiency can be improved.
本发明还提供了上述无放大效应的气体射流分散式塔板的设计方法，去包括由布气管线在液面上的高度和气体喷射进入液面的深度确定布气管线到基板距离的步骤；The present invention also provides the design method of the above-mentioned gas jet dispersed tray without amplification effect, including the step of determining the distance from the gas distribution pipeline to the substrate according to the height of the gas distribution pipeline above the liquid surface and the depth of the gas injection into the liquid surface;
布气管线距离塔板的高度受气体喷射入塔板深度和喷嘴在液面上高度两方面控制，其中，喷嘴在液面上高度不大于气相射流的起始段长度，气体喷射入液层深度利用量纲分析法计算得出：The height of the gas distribution pipeline from the tray is controlled by the depth of the gas injection into the tray and the height of the nozzle on the liquid surface. Calculated by dimensional analysis method:
假设气体从射流孔出来后属于紊流流动，并且出口断面上的速度分布一致，因此，根据动量守恒：可以得出布气管线在液面上的高度，即布气管线在液面上的高度按照以下公式确定：Assuming that the gas is a turbulent flow after coming out of the jet hole, and the velocity distribution on the outlet section is consistent, therefore, according to the conservation of momentum: The height of the gas distribution pipeline above the liquid surface can be obtained, that is, the height of the gas distribution pipeline above the liquid surface is determined according to the following formula:
式中：R为气体喷射到达液面时的半径，单位为m；r0为气体喷嘴出口半径，单位为m；h为射流孔到液平面的距离，单位为m；um为气体喷射到液面时的中心轴速，单位为m/s；u0为射流孔出口截面速度，单位为m/s；k为比例系数，范围0.3-1；φ为形状系数，为0.5-1.0，中心对称性越好，形状越趋于圆形，φ越趋近于1；a为湍流系数，与喷口断面的湍流强度和速度分布均匀性有关，范围是0.2-0.6；In the formula: R is the radius when the gas jet reaches the liquid surface, the unit is m; r0 is the radius of the gas nozzle outlet, the unit is m; h is the distance from the jet hole to the liquid level, the unit is m; u m is the gas jet to The central axis velocity at the liquid level, the unit is m/s; u 0 is the velocity of the exit section of the jet hole, the unit is m/s; k is the proportional coefficient, the range is 0.3-1; φ is the shape coefficient, it is 0.5-1.0, The better the symmetry, the more circular the shape, and the closer φ is to 1; a is the turbulence coefficient, which is related to the turbulence intensity and velocity distribution uniformity of the nozzle section, and the range is 0.2-0.6;
气体喷射进入液面的深度利用量纲分析法求出，气体喷射进入液面的深度按照以下公式确定：The depth of the gas injection into the liquid surface is obtained by dimensional analysis, and the depth of the gas injection into the liquid surface is determined according to the following formula:
f(L,d0,τ,h,θ,μ,ρg,w)＝0 (4)f(L,d 0 ,τ,h,θ,μ,ρ g ,w)=0 (4)
L'＝f(h',d',θ,R1) (8)L'=f(h',d',θ,R 1 ) (8)
当液体粘度<2mPa·s时，简化为以下关联式：When the liquid viscosity is less than 2mPa·s, it is simplified to the following correlation:
L'＝A/(h'2+B) (9)L ' ＝A/(h'2 +B) (9)
L'＝A/(h'2+B)+exp(-h')L' (10)L'=A/(h'2 +B)+exp(-h ' )L' (10)
式中：L为气体喷射进入液面的深度，为50-150mm；d0为射流孔直径，为3-20mm；τ为气体冲击力，N；θ为射流孔与液面夹角；μ为气体黏性力，单位为pa·s；ρg为气体密度，单位为kg/m3；ρL为液体密度，单位为kg/m3；w为液体比重；A、B均为模型系数。In the formula: L is the depth of gas injection into the liquid surface, which is 50-150mm; d 0 is the diameter of the jet hole, which is 3-20mm; τ is the impact force of the gas, N; θ is the angle between the jet hole and the liquid surface; Gas viscosity, unit is pa·s; ρ g is gas density, unit is kg/m 3 ; ρ L is liquid density, unit is kg/m 3 ; w is liquid specific gravity; A and B are model coefficients.
本发明的优点在于：The advantages of the present invention are:
1、塔板的基板是一个盲板，气体从上而下向板上的液层射流，并不像传统塔板由下而上通过塔板鼓泡或射流，气体的分布与液体分布无关，而且没有气体的阻挡，盲板上的液层液面落差很小，这种气液接触模式改变了传统塔板固有的气液错流模式，没有气液分布不均的问题，塔设备的放大效应将得以消除。1. The base plate of the tray is a blind plate, and the gas jets from top to bottom to the liquid layer on the plate, unlike traditional trays that bubble or jet through the tray from bottom to top, and the distribution of gas has nothing to do with the distribution of liquid. Moreover, there is no gas barrier, and the drop of the liquid layer on the blind plate is very small. This gas-liquid contact mode has changed the inherent gas-liquid cross-flow mode of the traditional tray, and there is no problem of uneven gas-liquid distribution. The expansion of the tower equipment effect will be eliminated.
2、在本发明的气液接触模式下，气体向均匀分布的液层进行高速射流，射流造成的剪切力将促进气泡或液滴的形成，从而获得相当大的传质相界面，有利于提高传质效率；并且气体在液层中向下射流后，因存在气液密度差，会再由下向上浮升，使得气体在液层中由传统的单向一过性变为下行和上行两个过程，停留时间显著增长，也可以提高传质效率。2. Under the gas-liquid contact mode of the present invention, the gas is jetted at a high speed to the evenly distributed liquid layer, and the shear force caused by the jet will promote the formation of bubbles or droplets, thereby obtaining a considerable mass transfer phase interface, which is beneficial to Improve the mass transfer efficiency; and after the gas jets down in the liquid layer, due to the gas-liquid density difference, it will rise from the bottom to the top again, so that the gas in the liquid layer changes from the traditional one-way transient to down and up For both processes, a significant increase in residence time can also improve mass transfer efficiency.
3、塔板压降主要是气相在升气管和布气管中克服形体阻力和摩擦阻力的机械能损失，不再像传统塔板那样包括液层的压降，所以板上所需液层高可以根据气相射流深度进行计算，更容易实现设计和操作控制。3. The pressure drop of the tray is mainly the mechanical energy loss of the gas phase overcoming the physical resistance and frictional resistance in the gas riser and gas distribution pipe. It no longer includes the pressure drop of the liquid layer like the traditional tray, so the height of the liquid layer on the plate can be determined according to the gas phase. The calculation of the jet depth makes it easier to realize the design and operation control.
4、因为塔板的基板上没有开孔，所以不可能出现传统塔板上常见的泄漏问题。泄漏会造成塔板上的液体停留时间过短，在塔板上没有经过充分的气液相接触传质，直接漏到下层塔板上，引起高浓度液相向低浓度液相的返混，造成传质效率的降低。本发明特别适用于生产中要求无泄漏的工况。4. Because there is no opening on the base plate of the tray, it is impossible to have the common leakage problem on the traditional tray. Leakage will cause the residence time of the liquid on the tray to be too short, without sufficient gas-liquid phase contact and mass transfer on the tray, it will directly leak to the lower tray, causing back-mixing of the high-concentration liquid phase to the low-concentration liquid phase, resulting in a decrease in mass transfer efficiency. The invention is especially suitable for working conditions requiring no leakage in production.
5、本发明在塔板的上方设置有布气管线，气体向上流动的过程中会由于惯性力的作用撞击管线，其中夹带的液滴会在管壁上聚集，到一定程度后，在重力的作用下返回塔板，因此，布气管线起到一定的捕沫作用；同时在塔板下安装的导流装置也会起到降低雾沫夹带的作用，在一定程度上减少塔板间距。5. In the present invention, a gas distribution pipeline is arranged above the tray. When the gas flows upward, it will hit the pipeline due to the action of inertial force, and the entrained liquid droplets will gather on the pipe wall. After a certain degree, under the influence of gravity Therefore, the gas distribution pipeline plays a certain role in trapping foam; at the same time, the deflector installed under the tray will also reduce the entrainment of mist and reduce the distance between the trays to a certain extent.
6、塔板的升气管结构可以采用弓形空腔，根据侧壁与布气管的倾角，可以调整流动方向，减小流动压降；也可以采用管形结构，便于分布进入布气管。升气管内设置分布板，可以像跑道一样将气流强制引导均匀分布进入各个布气管。布气管可以根据塔设备的规模和体系物性特点，加工成直管或圆管，管径也根据气速可以设计成不同形状，当气速较小时可采用圆管以增加机械强度，当气速较大时可采取矩形管，使得管内各点的线速度一致；布气管上的射流孔可以为通孔或设计成短管，当压降不是很大时，通孔结构简单，而短管加工难度增加，但可以降低流动阻力。6. The air riser structure of the tray can adopt a bow-shaped cavity, and according to the inclination angle between the side wall and the air distribution pipe, the flow direction can be adjusted to reduce the flow pressure drop; it can also adopt a tubular structure to facilitate distribution into the air distribution pipe. A distribution plate is set in the air riser, which can force the airflow to be evenly distributed into each air distribution pipe like a runway. The gas distribution pipe can be processed into straight or round pipes according to the scale of the tower equipment and the physical properties of the system. The diameter of the pipe can also be designed into different shapes according to the gas velocity. When it is larger, a rectangular tube can be used to make the linear velocity of each point in the tube consistent; the jet hole on the air distribution tube can be designed as a through hole or a short tube. When the pressure drop is not very large, the through hole structure is simple, and the short tube processing Difficulty increases, but flow resistance can be reduced.
附图说明Description of drawings
图1a和图1b为实施例1提供的气体射流分散式塔板的结构示意图，其中，图1a为主视图，图1b为俯视图。Figure 1a and Figure 1b are schematic structural views of the gas jet dispersion tray provided in Example 1, wherein Figure 1a is a front view, and Figure 1b is a top view.
图2a-图2j为各种类型的塔板结构示意图。2a-2j are schematic diagrams of various types of tray structures.
图3a-图3d为布气管及射流孔的结构示意图。3a-3d are structural schematic diagrams of the air distribution pipe and jet holes.
图3e为圆柱形射流孔或圆锥形射流孔的示意图。Fig. 3e is a schematic diagram of a cylindrical jet hole or a conical jet hole.
具体实施方式Detailed ways
为了对本发明的技术特征、目的和有益效果有更加清楚的理解，现对本发明的技术方案进行以下详细说明，但不能理解为对本发明的可实施范围的限定。In order to have a clearer understanding of the technical features, purposes and beneficial effects of the present invention, the technical solution of the present invention is described in detail below, but it should not be construed as limiting the scope of implementation of the present invention.
实施例1Example 1
本实施例提供了一种无放大效应的气体射流分散式塔板，其结构如图1a和图1b所示，图1a为主视图，图1b为俯视图。This embodiment provides a gas jet dispersion tray without amplification effect, the structure of which is shown in Figure 1a and Figure 1b, Figure 1a is a front view, and Figure 1b is a top view.
该塔板包括基板1，该基板1为盲板；The tray includes a base plate 1, which is a blind plate;
基板1下方设置有弧形气体导流板7；An arc-shaped gas deflector 7 is arranged under the substrate 1;
基板1的两侧设有升气管2，基板1与塔的内部之间具有一弓形空腔，升气管2就是该弓形空腔形成的，一共有2个升气管，升气管2的空腔侧壁与基板1的夹角α为90°，并且，二者的结合处设有圆弧倒角；There are air risers 2 on both sides of the base plate 1. There is an arcuate cavity between the base plate 1 and the inside of the tower. The air riser 2 is formed by the arcuate cavity. There are two air risers in total. The angle α between the wall and the base plate 1 is 90°, and the junction of the two is provided with a circular chamfer;
升气管2的顶板8为圆弧状；The top plate 8 of the gas riser 2 is arc-shaped;
降液板与塔壁围成一个弓形管腔，即降液管5，可以把上面一层下来的液体引到基板1上；The downcomer plate and the tower wall form an arcuate cavity, that is, the downcomer 5, which can lead the liquid from the upper layer to the base plate 1;
该塔板用于直径为1.2m的塔设备，故升气管2中设置2个分布板，将气流均匀导入布气管线3；The tray is used for tower equipment with a diameter of 1.2m, so two distribution plates are set in the gas riser 2 to guide the air flow evenly into the gas distribution pipeline 3;
在升气管2的侧壁顶部连接有平行于基板1的布气管线3，布气管线3由8根布气管组成，布气管为等长等径、截面为圆形的直管，布气管的壁厚为2mm，布气管的排布与液流方向垂直；The air distribution pipeline 3 parallel to the base plate 1 is connected to the top of the side wall of the air riser 2. The air distribution pipeline 3 is composed of 8 air distribution pipes. The air distribution pipe is a straight pipe with equal length and diameter and a circular cross section. The wall thickness is 2mm, and the air distribution pipes are arranged perpendicular to the liquid flow direction;
一根布气管的两端分别与一根升气管2连通；升气管2的顶部水平总截面积与布气管的水平总截面积相等；升气管2的空腔侧壁上设置有开孔9，升气管2与布气管线3通过开孔9连通；The two ends of an air distribution pipe are respectively communicated with an air riser 2; the horizontal total cross-sectional area of the top of the air riser 2 is equal to the horizontal total cross-sectional area of the air distribution pipe; the cavity side wall of the air riser 2 is provided with openings 9, The gas riser 2 communicates with the gas distribution pipeline 3 through the opening 9;
在基板1上位于相邻两根布气管的中间的位置处设置射流挡板10，射流挡板10下部开设有液体连通孔11；A jet baffle 10 is provided on the base plate 1 at a position between two adjacent air distribution pipes, and a liquid communication hole 11 is opened at the lower part of the jet baffle 10;
基板1的另外两侧或周边设有溢流堰6，该溢流堰6与基板1相连并高于基板1；An overflow weir 6 is provided on the other two sides or the periphery of the substrate 1, and the overflow weir 6 is connected to the substrate 1 and is higher than the substrate 1;
沿垂直布气管的方向向下开设1排射流孔4，射流孔4为圆形通孔，水平投影形状为圆形，射流孔的直径为2mm；射流孔采用三角形叉排方式，孔心距为孔径的4倍；A row of jet holes 4 is opened downward along the direction of the vertical air distribution pipe. The jet holes 4 are circular through holes, and the horizontal projection shape is circular. The diameter of the jet holes is 2mm; 4 times the aperture;
射流孔4下安装有垂直于布气管的圆柱形喷嘴；喷嘴的上缘与射流孔平齐，或者伸入到布气管中心位置，连接一段水平管段；喷嘴在布气管外的长度为喷嘴的直径的2倍。A cylindrical nozzle perpendicular to the air distribution pipe is installed under the jet hole 4; the upper edge of the nozzle is flush with the jet hole, or extends into the center of the air distribution pipe to connect a horizontal pipe section; the length of the nozzle outside the air distribution pipe is the diameter of the nozzle 2 times.
采用本实施例的气体射流分散式塔板时，布气管线在液面上的高度可以按照以下公式确定：When using the gas jet dispersion tray of this embodiment, the height of the gas distribution pipeline above the liquid surface can be determined according to the following formula:
式中：R为气体喷射到达液面时的半径，单位为100mm；r0为气体喷嘴出口半径，单位为5mm；h为射流孔到液平面的距离，单位为15mm；um为气体喷射到液面时的中心轴速，单位为m/s；u0为射流孔出口截面速度，单位为m/s；k为0.5；φ为1；a为湍流系数，其数值为0.6；In the formula: R is the radius when the gas jet reaches the liquid surface, the unit is 100mm; r0 is the gas nozzle outlet radius, the unit is 5mm; h is the distance from the jet hole to the liquid level, the unit is 15mm; u m is the gas jet to The central axis velocity at the liquid level, the unit is m/s; u 0 is the exit section velocity of the jet hole, the unit is m/s; k is 0.5; φ is 1; a is the turbulence coefficient, and its value is 0.6;
气体喷射进入液面的深度按照以下公式确定：The depth of gas injection into the liquid surface is determined according to the following formula:
f(L,d0,τ,h,θ,μ,ρg,w)＝0 (4)f(L,d 0 ,τ,h,θ,μ,ρ g ,w)=0 (4)
L'＝f(h',d',θ,R1) (8)L'=f(h',d',θ,R 1 ) (8)
当液体粘度<2mPa·s时，简化为以下关联式：When the liquid viscosity is less than 2mPa·s, it is simplified to the following correlation:
L'＝A/(h'2+B) (9)L ' ＝A/(h'2 +B) (9)
L'＝A/(h'2+B)+exp(-h')L' (10)L'=A/(h'2 +B)+exp(-h ' )L' (10)
式中：L为气体喷射进入液面的深度，其值为50mm；d0为射流孔直径，其值为5mm；τ为气体冲击力，N；θ为射流孔与液面夹角，其值为90℃；μ为气体黏性力，其值为1.005mPa·s；ρg为气体密度，其值为1.25kg/m3；ρL为液体密度，其值为998kg/m3；w为0.998；A为16250、B为100。In the formula: L is the depth of gas injection into the liquid surface, and its value is 50mm; d 0 is the diameter of the jet hole, and its value is 5mm; τ is the gas impact force, N; θ is the angle between the jet hole and the liquid surface, and its value is 90℃; μ is the gas viscous force, its value is 1.005mPa·s; ρ g is the gas density, its value is 1.25kg/m 3 ; ρ L is the liquid density, its value is 998kg/m 3 ; w is 0.998; A is 16250, B is 100.
实施例2Example 2
本实施例提供了一种无放大效应的气体射流分散式塔板，其结构如图1a和图1b所示，图1a为主视图，图1b为俯视图。This embodiment provides a gas jet dispersion tray without amplification effect, the structure of which is shown in Figure 1a and Figure 1b, Figure 1a is a front view, and Figure 1b is a top view.
该塔板包括基板1，该基板1为盲板；The tray includes a base plate 1, which is a blind plate;
基板1下方设置有弧形气体导流板7；An arc-shaped gas deflector 7 is arranged under the substrate 1;
基板1的两侧设有升气管2，基板1与塔的内部之间具有一弓形空腔，升气管2就是该弓形空腔形成的，一共有2个升气管，升气管2的空腔侧壁与基板1的夹角α为90°，并且，二者的结合处设有圆弧倒角；There are air risers 2 on both sides of the base plate 1. There is an arcuate cavity between the base plate 1 and the inside of the tower. The air riser 2 is formed by the arcuate cavity. There are two air risers in total. The angle α between the wall and the base plate 1 is 90°, and the junction of the two is provided with a circular chamfer;
升气管2的顶板8为圆弧状；The top plate 8 of the gas riser 2 is arc-shaped;
该塔板用于直径为2.4m的塔设备，故升气管2中设置4个分布板，将气流均匀导入布气管线3；The tray is used for tower equipment with a diameter of 2.4m, so 4 distribution plates are set in the air riser 2 to guide the air flow evenly into the gas distribution pipeline 3;
在升气管2的侧壁顶部连接有平行于基板1的布气管线3，布气管线3由16根布气管组成，布气管为等长等径、截面为圆形的直管，布气管的壁厚为2mm，布气管的排布与液流方向垂直；The air distribution pipeline 3 parallel to the base plate 1 is connected to the top of the side wall of the air riser 2. The air distribution pipeline 3 is composed of 16 air distribution pipes. The air distribution pipe is a straight pipe with equal length and diameter and a circular cross section. The wall thickness is 2mm, and the air distribution pipes are arranged perpendicular to the liquid flow direction;
一根布气管的两端分别与一根升气管2连通；升气管2的顶部水平总截面积与布气管的水平总截面积相等；升气管2的空腔侧壁上设置有开孔9，升气管2与布气管线3通过开孔9连通；The two ends of an air distribution pipe are respectively communicated with an air riser 2; the horizontal total cross-sectional area of the top of the air riser 2 is equal to the horizontal total cross-sectional area of the air distribution pipe; the cavity side wall of the air riser 2 is provided with openings 9, The gas riser 2 communicates with the gas distribution pipeline 3 through the opening 9;
在基板1上位于相邻两根布气管的中间的位置处设置射流挡板10，射流挡板10下部开设有液体连通孔11；A jet baffle 10 is provided on the base plate 1 at a position between two adjacent air distribution pipes, and a liquid communication hole 11 is opened at the lower part of the jet baffle 10;
基板1的另外两侧或周边设有溢流堰6，该溢流堰6与基板1相连并高于基板1；An overflow weir 6 is provided on the other two sides or the periphery of the substrate 1, and the overflow weir 6 is connected to the substrate 1 and is higher than the substrate 1;
沿垂直布气管的方向向下开设3排射流孔4，射流孔4为圆形通孔，水平投影形状为圆形，射流孔的直径为2mm；射流孔采用三角形叉排方式，孔心距为孔径的4倍；Three rows of jet holes 4 are set downward along the direction of the vertical air distribution pipe. The jet holes 4 are circular through holes, the shape of the horizontal projection is circular, and the diameter of the jet holes is 2mm; 4 times the aperture;
射流孔4下安装有垂直于布气管的圆锥形喷嘴；喷嘴的上缘与射流孔平齐，或者伸入到布气管中心位置，连接一段水平管段；喷嘴在布气管外的长度为喷嘴的直径的2倍；A conical nozzle perpendicular to the air distribution pipe is installed under the jet hole 4; the upper edge of the nozzle is flush with the jet hole, or extends into the center of the air distribution pipe to connect a horizontal pipe section; the length of the nozzle outside the air distribution pipe is the diameter of the nozzle 2 times of
采用本实施例的气体射流分散式塔板时，布气管线在液面上的高度可以按照以下公式确定：When using the gas jet dispersion tray of this embodiment, the height of the gas distribution pipeline above the liquid surface can be determined according to the following formula:
式中：R为气体喷射到达液面时的半径，其值为100mm；r0为气体喷嘴出口半径，其值为5mm；h为射流孔到液平面的距离，其值为15mm；um为气体喷射到液面时的中心轴速，单位为m/s；u0为射流孔出口截面速度，单位为m/s；k为0.5；φ为1；a为湍流系数，其值为0.6；In the formula: R is the radius when the gas jet reaches the liquid surface, its value is 100mm; r0 is the radius of the gas nozzle outlet, its value is 5mm; h is the distance from the jet hole to the liquid level, its value is 15mm; u m is The central axis velocity when the gas is sprayed to the liquid surface, the unit is m/s; u 0 is the exit section velocity of the jet hole, the unit is m/s; k is 0.5; φ is 1; a is the turbulence coefficient, its value is 0.6;
气体喷射进入液面的深度按照以下公式确定：The depth of gas injection into the liquid surface is determined according to the following formula:
f(L,d0,τ,h,θ,μ,ρg,w)＝0 (4)f(L,d 0 ,τ,h,θ,μ,ρ g ,w)=0 (4)
L'＝f(h',d',θ,R1) (8)L'=f(h',d',θ,R 1 ) (8)
当液体粘度<2mPa·s时，简化为以下关联式：When the liquid viscosity is less than 2mPa·s, it is simplified to the following correlation:
L'＝A/(h'2+B) (9)L ' ＝A/(h'2 +B) (9)
L'＝A/(h'2+B)+exp(-h')L' (10)L'=A/(h'2 +B)+exp(-h ' )L' (10)
式中：L为气体喷射进入液面的深度，其值为50mm；d0为射流孔直径，其值为5mm；τ为气体冲击力，N；θ为射流孔与液面夹角，其值为90℃；μ为气体黏性力，其值为1.005mPa·s；ρg为气体密度，其值为1.25kg/m3；ρL为液体密度，其值为998kg/m3；w为0.998；A为11250，B为75。In the formula: L is the depth of gas injection into the liquid surface, and its value is 50mm; d 0 is the diameter of the jet hole, and its value is 5mm; τ is the gas impact force, N; θ is the angle between the jet hole and the liquid surface, and its value is 90℃; μ is the gas viscous force, its value is 1.005mPa·s; ρ g is the gas density, its value is 1.25kg/m 3 ; ρ L is the liquid density, its value is 998kg/m 3 ; w is 0.998; A is 11250 and B is 75.
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