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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- CN107899535B CN107899535B CN201711351265.6A CN201711351265A CN107899535B CN 107899535 B CN107899535 B CN 107899535B CN 201711351265 A CN201711351265 A CN 201711351265A CN 107899535 B CN107899535 B CN 107899535B
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- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/32—Packing elements in the form of grids or built-up elements for forming a unit or module inside the apparatus for mass or heat transfer
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- B—PERFORMING OPERATIONS; TRANSPORTING
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Abstract
The invention provides a gas jet flow dispersive tower plate without amplification effect and a design method thereof. The tower plate comprises a base plate which is a blind plate; an arc-shaped gas guide plate is arranged below the substrate; the two sides or the center of the substrate are provided with gas risers, the top of the side wall of each gas riser is connected with a gas distribution pipeline parallel to the substrate, and each gas distribution pipeline consists of at least one gas distribution pipe; the other two sides of the substrate without the gas rising pipe are respectively provided with a down-flow plate and an overflow weir, the down-flow plate is arranged above the substrate and has a gap with the substrate, and the overflow weir is connected with the substrate and is higher than the substrate; the lower part of the gas distribution pipe is provided with a jet hole. The gas distribution pipelines are arranged on the tower plates and are uniformly distributed in parallel to the tower plates, and the pressure of the gas outlets is equal everywhere, so that the gas jetted from the jet holes is not influenced by the liquid distribution, and the uneven gas-liquid distribution caused by the liquid surface fall is reduced. Through the reasonable layout of the gas distribution pipeline, gas is uniformly sprayed onto the tower plate, and the gas-liquid phase mass transfer is promoted and the amplification effect is eliminated by shearing the liquid phase.
Description
Technical Field
The invention relates to a gas jet distributed tower plate without amplification effect and a design method thereof, belonging to the technical field of chemical industry and oil refining.
Background
First, the problems of inherent defects and amplification effects of conventional plate towers
The distillation tower has the characteristic of scale economy, and the large-scale device is a main way for reducing the production cost and improving the scale benefit. After the scale of the tower equipment is enlarged, the non-ideal flow and the uneven vapor-liquid dispersion in the tower are intensified, and the technical indexes such as the processing capacity, the tower plate efficiency, the operation flexibility and the like are obviously reduced.
The conventional large plate tower has inherent defects due to a vapor-liquid flow mass transfer mode: the gas phase in the tower passes through the tower plate from bottom to top along the vertical direction, the liquid phase flows horizontally from one end to the other end on the tower plate and then is guided to the next layer of tower plate by the downcomer, and the gas can enter the upper space only after passing through the tower plate and the liquid layer. However, when the liquid flows on the plate, due to the resistance of the tower plate, the tower wall and the gas phase flow, liquid level difference exists along the liquid flow direction, and the liquid layer is unevenly distributed. Since the gas density is much less than the liquid density and the inertia is small, an uneven distribution of the liquid will necessarily result in an uneven distribution of the gas. Gas-liquid maldistribution will be more aggravated like this for the entry liquid layer is thicker, and the gas volume is few, easily takes place to leak, and the export liquid layer is thinner, and the gas volume is big, easily takes place the mist and smugglies secretly, and gas, liquid double-phase can not fully contact, serious threat production safety even. This is a common problem with conventional cross-flow trays.
Along with the enlargement of the diameter of the tower, the inertia of liquid flow under high liquid phase load is huge, the opening number of the gas flow is multiplied, the liquid flow resistance is aggravated, the flow randomness is obviously enhanced, the operation condition on the plate has great uncertainty, and the prediction can not be accurately carried out like a small tower. The gas-liquid dispersion in the tower plate space is regulated and controlled by transfer dynamics, the serious hydraulics instability (randomness) is shown, the tower plate has non-ideal operations such as channeling, stream flow, back mixing and the like, leakage and entrainment can even occur simultaneously and are increased greatly in magnitude order, the plate efficiency and the treatment capacity are reduced, the pressure drop is increased, the stability is poor, the problem of amplification effect is solved, the gas-liquid uneven distribution of the plate tower is aggravated by the scale expansion of tower equipment, and the operation performance of the tower plate is worsened.
Design difficulty of two or more overflow plate type tower
At present, the amplification effect is mainly processed by adopting a multi-overflow design, namely the length of a flow channel is reduced, and the strength of liquid flow is reduced so as to reduce the inertia of the liquid flow on a tower plate and the fluctuation degree of a liquid layer. However, the multiple overflow design also faces the problem of uniform distribution of the liquid phase within the plurality of downcomers and uniform distribution of the gas phase within the bubble zone between the downcomers. The distribution of the multi-overflow liquid is directly related to the symmetry of the tower plate structure, wherein the symmetry of the eccentric downcomer is much different from that of the central downcomer and the side downcomers, the outlet weirs on the left side and the right side of the eccentric downcomer are different in length, the outlet area of the bottom gap of the downcomer is the same as the outflow resistance, and gas-liquid bias flow is easily caused. For the tray with overflow channels more than or equal to three overflows, the liquid from the downcomer is more difficult to distribute evenly due to the asymmetry of the structure of the tray.
It should be noted that the uniformity of gas distribution in a multiple overflow design is still determined by the liquid layer distribution, large column diameters are detrimental to the dispersion of the two phases, and the non-ideal distribution of the liquid and gas phases interact with each other, further exacerbating the non-uniform distribution effect. Although the multi-overflow can realize the enlarged design of the tower, the problem of non-ideal operation of the tower plates is not solved, and the multi-overflow can be compensated only by increasing the number of the tower plates and improving the safety factor.
In the prior patents, a plurality of patents such as 'vapor-liquid contact system and method' (patent No. US3410540), 'an MD tray with an increased processing capacity' (patent No. US5,318,732), 'an MD tray with a guide plate' (patent No. US5,098,615), 'an MD tray with a liquid receiving disc for preventing impact leakage' (patent No. US5,209,875) and the like are to adopt a multi-overflow and a suspended downcomer to treat the amplification effect of the tray column. Because the liquid layer always has liquid level drop on the tower plate, the leakage of the suspension type downcomer is serious, the amplification effect of a large tower can be activated, and the efficiency of the tower plate is not high, the functions of the patents on improving the gas-liquid distribution of each bubbling area are still limited.
Disclosure of Invention
In order to solve the problems, the invention aims to provide a gas jet flow distributed tower plate without amplification effect, which can enable gas to be uniformly jetted to a liquid layer without liquid level drop, fundamentally eliminate the inherent defect of the amplification effect, enable gas-liquid two-phase distribution to be more uniform, and improve the mass transfer efficiency and the processing capacity of the tower plate.
In order to achieve the above object, the present invention provides a gas jet dispersive tray without amplification effect, wherein: the tower plate comprises a base plate which is a blind plate;
an arc-shaped gas guide plate is arranged at the lower part of the substrate;
the gas-distributing pipeline is connected to the top of the side wall of the gas-distributing pipeline and is parallel to the substrate, and the gas-distributing pipeline consists of at least one gas-distributing pipe;
the other two sides of the base plate without the gas rising pipe are respectively provided with a down-flow plate and an overflow weir, the down-flow plate and the tower wall enclose a down-flow pipe, liquid flowing from the upper base plate can be guided onto the base plate, the overflow weir is arranged on the other side symmetrical to the down-flow plate, is connected with the base plate and is higher than the base plate, a liquid layer with a certain thickness can be kept on the base plate, so that gas and liquid can be in full contact with mass transfer, and the liquid after mass transfer falls onto the lower tower plate after flowing through the overflow weir;
the lower part of the gas distribution pipe is provided with a jet hole.
Different from the design pattern that the gas of the traditional tower plate passes through the tower plate from bottom to top, the invention arranges the gas distribution pipeline on the tower plate and is uniformly distributed parallel to the tower plate, and the pressure of the gas outlet is equal everywhere, thus ensuring that the gas ejected from the jet hole is not influenced by the liquid distribution. Through the reasonable layout of the gas distribution pipeline, gas is uniformly sprayed onto the tower plates, the influence of liquid inertia on distribution is reduced by shearing liquid phase, the gas can be uniformly sprayed into the liquid layer without the influence of liquid level drop, and further the phase interface area is greatly increased. And meanwhile, the leakage of the tower plate is thoroughly eliminated, the entrainment is greatly reduced, the amplification effect is eliminated, and the mass transfer efficiency and the processing capacity of the tower plate are greatly improved.
In the gas jet flow dispersive column plate without amplification effect, the overflow weir and the down-flow plate are symmetrical in position and are used for keeping a liquid layer with a certain thickness, and liquid flows out over the overflow weir and can fall onto the next layer of base plate.
In the abovementioned gas jet dispersion trays without amplification effect, the trays are arranged inside the column apparatus with their base plates arranged horizontally. The substrate is not provided with holes and is a blind plate; preferably, the lower part of the base plate is provided with an arc-shaped gas guide plate, and liquid can only flow into the lower-layer tower plate from the downcomer, so that the problem of large leakage rate after equipment amplification is thoroughly solved, and liquid flow on the tower plate can not be influenced by the bubble holes and the leakage holes and can flow through the tower plate more uniformly. Meanwhile, in the process that gas carries part of liquid drops to flow upwards, due to the action of gas inertia force, the gas distribution pipeline on the tower plate can play a certain foam catching role, and the guide plate below the tower plate catches foam, so that the foam clamping of the tower equipment is greatly reduced, and the amplification effect is greatly reduced. Meanwhile, gas enters the tower plates from top to bottom, so that gas entrainment in the downcomer can be reduced, and the distance between the tower plates can be reduced. The raised risers, as indicated by the arrows in fig. 2a, are downcomers that enclose an arcuate lumen with the column wall, called a downcomer, to direct liquid from above onto the base plate.
In the above-mentioned tray, the gas-raising tube may be formed of an arcuate cavity in the side of the base plate, or may be a separately provided tube, preferably formed of an arcuate cavity in the side of the base plate. The number of draft tubes is one or several.
The tower device is generally cylindrical in shape as a whole, the base plate is square, and there is a cavity between its side and the inner wall of the tower device, which cavity is arcuate in shape when viewed in cross-section. This air can be used directly as a draft tube, i.e. the draft tube is formed by an arcuate cavity in the side of the base plate, and a roof can be provided at the top of the draft tube. The shape of the top plate can be set as desired. When the top plate is a plane, the structure is simple, but no guiding effect is generated on gas, boundary layer separation is caused by the change of the direction of the airflow, a stagnation point is formed at the top, the pressure drop is large, and the device is usually used for small gas flow (speed); when the roof is the arc, have the guide effect to gaseous, the pressure drop is little, but the processing has the degree of difficulty, is used for big tolerance (speed) usually.
According to the specific embodiment of the invention, the side wall of the cavity of the gas lift pipe can be provided with an opening, and the gas lift pipe is communicated with the gas distribution pipe line through the opening.
According to a particular embodiment of the invention, the angle α of the side walls of the cavity of the draft tube to the base plate is preferably from 90 ° to 145 °, as shown in fig. 1. The larger the angle alpha is, the more obvious the guiding effect on the air flow is, the separation of a fluid boundary layer can be avoided, and the pressure drop is reduced. And the joint of the cavity side wall of the riser and the base plate is preferably provided with an arc chamfer.
According to a particular embodiment of the invention, for column units having a diameter of 2m or more, one or more distribution plates may be provided in the riser to evenly direct the gas flow into the gas distribution line. The distribution plate acts like a runway, so that gas phase can be uniformly distributed to enter each gas distribution pipe, and gas flow is prevented from mainly entering the central gas distribution pipe due to the side wall effect.
According to the specific embodiment of the invention, when the air-lift pipes are arranged in the arc-shaped areas at the two sides of the base plate, the air-lift pipes at the two sides are respectively connected with the air-distribution pipes, the two ends of one air-distribution pipe are respectively connected with one air-lift pipe at the two sides, and the air-distribution pipes are equal in length.
According to a particular embodiment of the invention, the top horizontal total cross-sectional area of the draft tube is equal to the horizontal total cross-sectional area of the gas distribution line, i.e. the top horizontal total cross-sectional area of the draft tube is equal to the horizontal total cross-sectional area of (all) gas distribution tubes, to ensure similar gas velocities at the same gas flow rate. Wherein, the total horizontal cross-sectional area of the top of the draft tube is calculated by the draft tubes on both sides.
According to the specific embodiment of the invention, when the gas distribution pipeline has a plurality of gas distribution pipes, the jet flow baffle plate is arranged on the base plate at the middle position of two adjacent gas distribution pipes, and the lower part of the jet flow baffle plate is preferably provided with a liquid communication hole. The jet baffle is similar to a wave trap in a water bed, can avoid liquid from impacting to form oscillation, and can ensure that the liquid level at each position on the substrate is the same by arranging the communicating holes, thereby playing the role of the communicating device. The two devices divide the large device into mutually communicated cells, so that the uniformity of the water surface in the large device can be kept, and the amplification effect is avoided.
According to the specific embodiment of the invention, the gas distribution pipeline can adopt straight pipes or circular pipes with equal diameters or different diameters. The gas distribution pipes can be arranged in a way of being vertical or parallel to the liquid flow direction, or in a way of being circular or radial. The cross-sectional shape of the gas distribution pipe can be circular, conical, elliptical or rectangular, and preferably, the wall thickness of the gas distribution pipe is 2-8 mm.
FIGS. 2 a-2 j are schematic diagrams of various types of tray structures. Wherein, fig. 2a is a structural diagram of two sides of the arc-shaped cavity riser connected with the parallel gas distribution pipes, the gas distribution pipes are perpendicular to the liquid flow direction, and the liquid flow direction points to the weir plate; FIG. 2b is a structural diagram of a main gas distribution pipe and a parallel branch gas distribution pipe connected by two side arc-shaped cavity gas risers, wherein the direction of the main gas distribution pipe is vertical to the liquid flow direction, and the branch gas distribution pipe is parallel to the liquid flow direction; FIG. 2c is a structural diagram of a circular tube-shaped gas riser on two sides connecting a main gas distribution pipe and a parallel branch gas distribution pipe, wherein the main gas distribution pipe is vertical to the liquid flow direction, and the branch gas distribution pipe is parallel to the liquid flow direction; FIG. 2d is a structural diagram of two circular tube-shaped gas risers connected with a main gas distribution tube and annular branch gas distribution tubes, wherein the main gas distribution tube is a straight tube, and the branch gas distribution tubes at all levels are concentric circular tubes; FIG. 2e is a structural diagram of a circular tube-shaped gas rising pipe at two sides connecting a main gas distribution pipe and annular branch gas distribution pipes, wherein the main gas distribution pipe is in a cross shape, and the branch gas distribution pipes at all levels are concentric circular tubes; FIG. 2f is a structural diagram of the two side circular tube-shaped gas risers connecting the main gas distribution tube and the radial gas distribution tubes, each stage of the gas distribution tubes are straight circular tubes with the diameters increasing from small to large and are distributed radially; FIG. 2g is a structural diagram of a circular tube-shaped riser at two sides connecting a main gas distribution pipe and radial branch gas distribution pipes, wherein each branch gas distribution pipe is a straight triangular tube with a diameter increasing from small to large and is distributed radially; FIG. 2h is a structural diagram of a plurality of gas risers on two sides connected with parallel gas distribution pipes, each gas riser corresponding to one gas distribution pipe; FIG. 2i is a structural diagram of a central ascending tube connecting a main gas distribution tube and parallel branch gas distribution tubes, wherein the ascending tube is vertically upward at the center of a substrate, the main gas distribution tube is parallel to the liquid flow direction, the branch gas distribution tubes are perpendicular to the liquid flow direction, and the tube lengths are sequentially decreased from the middle to the two sides; FIG. 2j is a structural diagram of a central ascending tube connected with parallel branch distribution tubes, the ascending tube is vertically upward, the main body is rectangular, the top is semicircular and parallel to the liquid flow direction, the branch distribution tubes are perpendicular to the liquid flow direction, and the tube lengths are gradually decreased from the middle to the two sides.
According to a particular embodiment of the invention, the horizontal projection shape of the jet hole may be circular, square or rectangular. The jet hole can be an equal-diameter through hole or a reducing through hole; FIG. 3e is a schematic diagram of a cylindrical jet hole and a conical jet hole; preferably, the jet hole is a reducing through hole with a taper angle beta (shown in fig. 3 e) of 0-45 degrees; more preferably, the jet holes have a diameter of 2-10 mm.
Fig. 3 a-3 d are schematic structural views of the air distribution pipe and the jet hole. Wherein, fig. 3a is a circular air distribution pipe, which is provided with a cylindrical through hole as a jet hole; FIG. 3b is a rectangular air distribution pipe, which is provided with a cylindrical through hole as a jet hole; FIG. 3c is a circular air distribution pipe, which is provided with a long strip-shaped through hole as a jet hole; fig. 3d is a circular gas distribution pipe, on which a circular through hole is opened as a jet hole, and a circular nozzle is arranged below, the nozzle can be connected with an elbow, and the elbow is positioned inside the gas distribution pipe.
According to the specific embodiment of the invention, the jet holes of the air distribution pipe can adopt a triangular staggered mode, and the hole center distance is 1.5-10 times of the hole diameter; preferably, 1-5 rows of jet holes are formed in the air distribution pipes which are arranged in a plurality of rows and downwards along the direction vertical to the air distribution pipes.
According to the specific embodiment of the invention, a nozzle vertical to the air distribution pipe can be arranged below the jet hole; the upper edge of the nozzle is flush with the jet hole or extends into the central position of the gas distribution pipe to be connected with a section of horizontal pipe section. The nozzle may be cylindrical or conical. The length of the nozzle outside the gas distribution pipe can be controlled to be 1-8 times of the diameter of the nozzle, so that the gas divergence can be reduced, more gas kinetic energy is converted into interface energy, and the mass transfer efficiency is improved.
The invention also provides a design method of the gas jet dispersive column plate without the amplification effect, which comprises the step of determining the distance between the gas distribution pipeline and the substrate according to the height of the gas distribution pipeline on the liquid surface and the depth of the gas injection into the liquid surface;
the height of the gas distribution pipeline from the tower plate is controlled by the depth of gas injection into the tower plate and the height of the nozzle above the liquid level, wherein the height of the nozzle above the liquid level is not more than the length of the initial segment of the gas-phase jet flow, and the depth of the gas injection into the liquid layer is calculated by using a dimensional analysis method to obtain:
assuming that the gas flows in a turbulent manner after exiting from the jet holes and the velocity distribution is uniform over the exit section, therefore, according to the conservation of momentum:the height of the gas distribution line above the liquid level can be determined, i.e. the height of the gas distribution line above the liquid level is determined according to the following formula:
in the formula: r is the radius of the gas jet when it reaches the liquid surface, in unitsIs m; r is0Is the gas nozzle exit radius in m; h is the distance from the jet hole to the liquid plane, and the unit is m; u. ofmThe central axis speed when the gas is sprayed to the liquid surface is in m/s; u. of0The velocity of the outlet section of the jet hole is expressed in m/s; k is a proportionality coefficient, and the range is 0.3-1; phi is a shape coefficient which is 0.5-1.0, the central symmetry is better, the shape tends to be circular, and phi approaches to 1; a is a turbulence coefficient which is related to the turbulence intensity of the section of the nozzle and the speed distribution uniformity, and the range is 0.2-0.6;
the depth of the gas jet into the liquid surface is determined by a dimensional analysis method, and the depth of the gas jet into the liquid surface is determined according to the following formula:
f(L,d0,τ,h,θ,μ,ρg,w)＝0 (4)
L'＝f(h',d',θ,R1) (8)
when the liquid viscosity is <2mPa · s, it is reduced to the following correlation:
L'＝A/(h'2+B) (9)
L'＝A/(h'2+B)+exp(-h')L' (10)
in the formula: l is the depth of gas injection into the liquid surface and is 50-150 mm; d0The diameter of the jet hole is 3-20 mm; τ is gas impact force, N; theta is an included angle between the jet hole and the liquid level; μ is gas viscosity in pa · s; rhogIs the gas density in kg/m3；ρLIs the liquid density in kg/m3(ii) a w is the specific gravity of the liquid; A. and B are model coefficients.
The invention has the advantages that:
1. the base plate of the column plate is a blind plate, gas flows from top to bottom to the liquid layer jet flow on the plate, and the gas distribution is irrelevant to the liquid distribution unlike the traditional column plate which bubbles or jet flow from bottom to top, and no gas blocks, the liquid level drop of the liquid layer on the blind plate is very small, the gas-liquid contact mode changes the inherent gas-liquid cross flow mode of the traditional column plate, the problem of uneven gas-liquid distribution is avoided, and the amplification effect of the column equipment can be eliminated.
2. In the gas-liquid contact mode, gas is subjected to high-speed jet flow towards the uniformly distributed liquid layer, and the formation of bubbles or liquid drops is promoted by the shearing force caused by the jet flow, so that a quite large mass transfer phase interface is obtained, and the mass transfer efficiency is improved; and after the gas is jetted downwards in the liquid layer, the gas can rise from bottom to top due to the gas-liquid density difference, so that the gas is changed into two processes of descending and ascending from the traditional one-way transition in the liquid layer, the retention time is obviously prolonged, and the mass transfer efficiency can be improved.
3. The pressure drop of the tower plate is mainly the mechanical energy loss of gas phase in the gas lift pipe and the gas distribution pipe to overcome the body resistance and the frictional resistance, and the pressure drop of a liquid layer is not included like the pressure drop of a traditional tower plate, so the liquid layer height required on the plate can be calculated according to the gas phase jet flow depth, and the design and the operation control are easier to realize.
4. Because there are no openings in the base of the tray, the leakage problems common to conventional trays are unlikely to occur. The leakage can cause the liquid retention time on the tower plate to be too short, the sufficient gas-liquid phase contact mass transfer is not carried out on the tower plate, and the liquid is directly leaked to the lower tower plate, so that the back mixing of the high-concentration liquid phase to the low-concentration liquid phase is caused, and the reduction of the mass transfer efficiency is caused. The invention is especially suitable for the working condition requiring no leakage in production.
5. According to the invention, the gas distribution pipeline is arranged above the tower plate, gas can impact the pipeline due to the action of inertia force in the upward flowing process, entrained liquid drops can be gathered on the pipe wall, and return to the tower plate under the action of gravity after reaching a certain degree, so that the gas distribution pipeline plays a certain foam catching role; meanwhile, the flow guide device arranged below the tower plate can also play a role in reducing entrainment, so that the distance between the tower plates is reduced to a certain extent.
6. The gas-raising pipe structure of the column plate can adopt an arch-shaped cavity, and the flowing direction can be adjusted according to the inclination angle between the side wall and the gas-distributing pipe, so that the flowing pressure drop is reduced; also can adopt a tubular structure, which is convenient for being distributed and entering the gas distribution pipe. The distribution plate is arranged in the gas lift pipe, and can forcibly guide the gas flow to be uniformly distributed into each gas distribution pipe like a runway. The gas distribution pipe can be processed into a straight pipe or a circular pipe according to the scale of tower equipment and the physical property characteristics of a system, the pipe diameter can be designed into different shapes according to the gas velocity, the circular pipe can be adopted to increase the mechanical strength when the gas velocity is low, and the rectangular pipe can be adopted when the gas velocity is high, so that the linear velocities of all points in the pipe are consistent; the jet hole on the gas distribution pipe can be a through hole or designed into a short pipe, when the pressure drop is not very large, the through hole has a simple structure, the processing difficulty of the short pipe is increased, and the flow resistance can be reduced.
Drawings
FIGS. 1a and 1b are schematic structural views of a gas jet dispersion tray as provided in example 1, wherein FIG. 1a is a front view and FIG. 1b is a top view.
FIGS. 2 a-2 j are schematic diagrams of various types of tray structures.
Fig. 3 a-3 d are schematic structural views of the air distribution pipe and the jet hole.
Fig. 3e is a schematic view of a cylindrical jet hole or a conical jet hole.
Detailed Description
The technical solutions of the present invention will be described in detail below in order to clearly understand the technical features, objects, and advantages of the present invention, but the present invention is not limited to the practical scope of the present invention.
Example 1
This example provides a gas jet dispersion tray without amplification effect, the structure of which is shown in FIG. 1a and FIG. 1b, FIG. 1a is a front view and FIG. 1b is a top view.
The tower plate comprises a base plate 1, wherein the base plate 1 is a blind plate;
an arc-shaped gas guide plate 7 is arranged below the substrate 1;
the two sides of the base plate 1 are provided with gas risers 2, an arched cavity is arranged between the base plate 1 and the interior of the tower, the gas risers 2 are formed by the arched cavity, 2 gas risers are arranged in total, the included angle alpha between the side wall of the cavity of the gas riser 2 and the base plate 1 is 90 degrees, and the joint of the two gas risers is provided with an arc chamfer;
the top plate 8 of the gas lift pipe 2 is arc-shaped;
the downcomer and the tower wall enclose an arched pipe cavity, namely a downcomer 5, which can guide the liquid on the upper layer to the base plate 1;
the column plate is used for column equipment with the diameter of 1.2m, so 2 distribution plates are arranged in the gas rising pipe 2 to uniformly guide gas flow into the gas distribution pipeline 3;
the top of the side wall of the gas lift pipe 2 is connected with a gas distribution pipe line 3 parallel to the base plate 1, the gas distribution pipe line 3 consists of 8 gas distribution pipes, the gas distribution pipes are straight pipes with equal length and equal diameter and circular sections, the wall thickness of the gas distribution pipes is 2mm, and the gas distribution pipes are arranged perpendicular to the liquid flow direction;
two ends of one gas distribution pipe are respectively communicated with one gas lift pipe 2; the horizontal total sectional area of the top of the gas rising pipe 2 is equal to the horizontal total sectional area of the gas distribution pipe; an opening 9 is formed in the side wall of the cavity of the gas lift pipe 2, and the gas lift pipe 2 is communicated with the gas distribution pipeline 3 through the opening 9;
a jet baffle 10 is arranged at the position of the middle of two adjacent gas distribution pipes on the substrate 1, and a liquid communication hole 11 is formed in the lower part of the jet baffle 10;
the other two sides or the periphery of the substrate 1 are provided with overflow weirs 6, and the overflow weirs 6 are connected with the substrate 1 and are higher than the substrate 1;
the jet flow device is characterized in that 1 row of jet flow holes 4 are formed downwards along the direction vertical to the air distribution pipe, the jet flow holes 4 are circular through holes, the horizontal projection shape is circular, and the diameter of each jet flow hole is 2 mm; the jet holes adopt a triangular fork arrangement mode, and the hole center distance is 4 times of the hole diameter;
a cylindrical nozzle vertical to the gas distribution pipe is arranged below the jet hole 4; the upper edge of the nozzle is flush with the jet hole or extends into the central position of the gas distribution pipe to be connected with a section of horizontal pipe section; the length of the nozzle outside the gas distribution pipe is 2 times of the diameter of the nozzle.
When the gas jet dispersive tray is adopted, the height of the gas distribution pipeline on the liquid level can be determined according to the following formula:
in the formula: r is the radius of the gas jet when reaching the liquid surface, and the unit is 100 mm; r is0Is the radius of the outlet of the gas nozzle, and the unit is 5 mm; h is the distance from the jet hole to the liquid plane, and the unit is 15 mm; u. ofmThe central axis speed when the gas is sprayed to the liquid surface is in m/s; u. of0The velocity of the outlet section of the jet hole is expressed in m/s; k is 0.5; phi is 1; a is the turbulence factor, which has a value of 0.6;
the depth of the gas jet into the liquid surface is determined according to the following formula:
f(L,d0,τ,h,θ,μ,ρg,w)＝0 (4)
L'＝f(h',d',θ,R1) (8)
when the liquid viscosity is <2mPa · s, it is reduced to the following correlation:
L'＝A/(h'2+B) (9)
L'＝A/(h'2+B)+exp(-h')L' (10)
in the formula: l is the gas injected into the liquid surfaceA depth of 50 mm; d0The diameter of the jet hole is 5 mm; τ is gas impact force, N; theta is an included angle between the jet hole and the liquid level, and the value of theta is 90 ℃; μ is a gas viscosity of 1.005 mPas; rhogA gas density of 1.25kg/m3；ρLIs liquid density and has a value of 998kg/m3(ii) a w is 0.998; a is 16250 and B is 100.
Example 2
This example provides a gas jet dispersion tray without amplification effect, the structure of which is shown in FIG. 1a and FIG. 1b, FIG. 1a is a front view and FIG. 1b is a top view.
The tower plate comprises a base plate 1, wherein the base plate 1 is a blind plate;
an arc-shaped gas guide plate 7 is arranged below the substrate 1;
the two sides of the base plate 1 are provided with gas risers 2, an arched cavity is arranged between the base plate 1 and the interior of the tower, the gas risers 2 are formed by the arched cavity, 2 gas risers are arranged in total, the included angle alpha between the side wall of the cavity of the gas riser 2 and the base plate 1 is 90 degrees, and the joint of the two gas risers is provided with an arc chamfer;
the top plate 8 of the gas lift pipe 2 is arc-shaped;
the column plate is used for tower equipment with the diameter of 2.4m, so 4 distribution plates are arranged in the gas rising pipe 2 to uniformly guide gas flow into the gas distribution pipeline 3;
the top of the side wall of the gas lift pipe 2 is connected with a gas distribution pipe line 3 parallel to the substrate 1, the gas distribution pipe line 3 consists of 16 gas distribution pipes, the gas distribution pipes are straight pipes with equal length and equal diameter and circular sections, the wall thickness of the gas distribution pipes is 2mm, and the gas distribution pipes are arranged perpendicular to the liquid flow direction;
two ends of one gas distribution pipe are respectively communicated with one gas lift pipe 2; the horizontal total sectional area of the top of the gas rising pipe 2 is equal to the horizontal total sectional area of the gas distribution pipe; an opening 9 is formed in the side wall of the cavity of the gas lift pipe 2, and the gas lift pipe 2 is communicated with the gas distribution pipeline 3 through the opening 9;
a jet baffle 10 is arranged at the position of the middle of two adjacent gas distribution pipes on the substrate 1, and a liquid communication hole 11 is formed in the lower part of the jet baffle 10;
the other two sides or the periphery of the substrate 1 are provided with overflow weirs 6, and the overflow weirs 6 are connected with the substrate 1 and are higher than the substrate 1;
the jet flow device is characterized in that 3 rows of jet flow holes 4 are formed downwards along the direction vertical to the air distribution pipe, the jet flow holes 4 are circular through holes, the horizontal projection shape is circular, and the diameter of each jet flow hole is 2 mm; the jet holes adopt a triangular fork arrangement mode, and the hole center distance is 4 times of the hole diameter;
a conical nozzle vertical to the gas distribution pipe is arranged below the jet hole 4; the upper edge of the nozzle is flush with the jet hole or extends into the central position of the gas distribution pipe to be connected with a section of horizontal pipe section; the length of the nozzle outside the gas distribution pipe is 2 times of the diameter of the nozzle;
when the gas jet dispersive tray is adopted, the height of the gas distribution pipeline on the liquid level can be determined according to the following formula:
in the formula: r is the radius of the gas jet when reaching the liquid surface, and the value is 100 mm; r is0Is the radius of the outlet of the gas nozzle, and the value is 5 mm; h is the distance from the jet hole to the liquid plane, and the value of h is 15 mm; u. ofmThe central axis speed when the gas is sprayed to the liquid surface is in m/s; u. of0The velocity of the outlet section of the jet hole is expressed in m/s; k is 0.5; phi is 1; a is the turbulence factor, which has a value of 0.6;
the depth of the gas jet into the liquid surface is determined according to the following formula:
f(L,d0,τ,h,θ,μ,ρg,w)＝0 (4)
L'＝f(h',d',θ,R1) (8)
when the liquid viscosity is <2mPa · s, it is reduced to the following correlation:
L'＝A/(h'2+B) (9)
L'＝A/(h'2+B)+exp(-h')L' (10)
in the formula: l is the depth of the gas injection into the liquid surface, and the value is 50 mm; d0The diameter of the jet hole is 5 mm; τ is gas impact force, N; theta is an included angle between the jet hole and the liquid level, and the value of theta is 90 ℃; μ is a gas viscosity of 1.005 mPas; rhogA gas density of 1.25kg/m3；ρLIs liquid density and has a value of 998kg/m3(ii) a w is 0.998; a is 11250 and B is 75.
Claims (65)
1. A gas jet dispersive column plate without amplification effect is characterized in that: the tower plate comprises a base plate which is a blind plate;
an arc-shaped gas guide plate is arranged below the substrate;
gas risers are arranged at two sides or the center of the base plate, and gas distribution pipeline parallel to the base plate is connected to the top of the side wall of the gas riser and consists of at least one gas distribution pipeline;
the other two sides of the base plate without the gas rising pipe are respectively provided with a down-flow plate and an overflow weir, the down-flow plate is arranged above the base plate, a gap is reserved between the down-flow plate and the base plate, and the down-flow plate and the tower wall enclose a down-flow pipe to guide liquid onto the base plate; the overflow weir is arranged on the other side symmetrical to the position of the liquid falling plate, is connected with the substrate and is higher than the substrate, and can keep a liquid layer with a certain thickness on the substrate;
the lower part of the gas distribution pipe is provided with a jet hole, and the jet hole is arranged downwards along the direction vertical to the gas distribution pipe so as to jet gas to a liquid layer on the tower plate from top to bottom;
the distance between the gas distribution pipeline and the substrate is determined by the height of the gas distribution pipeline on the liquid level and the depth of gas injection into the liquid level;
wherein the height of the gas distribution pipeline on the liquid level is determined according to the following formula:
in the formula: r is the radius of the gas jet when it reaches the liquid surface, and the unit is m; r is0Is the gas nozzle exit radius in m; h is the distance from the jet hole to the liquid plane, and the unit is m; u. ofmThe central axis speed when the gas is sprayed to the liquid surface is in m/s; u. of0The velocity of the outlet section of the jet hole is expressed in m/s; k is a proportionality coefficient and is determined by experiments; phi is the exit shape coefficient; a is a turbulence coefficient, and is related to the turbulence intensity and the speed distribution uniformity of the nozzle section;
the depth of the gas jet into the liquid surface is determined according to the following formula:
f(L,d0,τ,h,θ,μ,ρg,w)＝0 (4)
L'＝f(h',d',θ,R1) (8)
when the liquid viscosity is <2mPa · s, it is reduced to the following correlation:
L'＝A/(h'2+B) (9)
L'＝A/(h'2+B)+exp(-h')L' (10)
in the formula: l is the depth of the gas injection into the liquid surface, and the unit is m; d0The diameter of the jet hole is m; τ is gas impact force, N; theta is an included angle between the jet hole and the liquid level; mu is gas viscosity and has a unit of Pa.s; rhogIs the gas density in kg/m3；ρLIs the liquid density in kg/m3(ii) a w is the specific gravity of the liquid; f is a function expression; A. and B are model coefficients.
2. Dispersive tray of gas jets without amplification effect according to claim 1, characterized in that: the gas risers may be formed as arcuate cavities in the sides of the substrate or as separately disposed tubes.
3. The dispersive tray of gas jets without amplification effect according to claim 2, wherein the number of chimneys is one or several.
4. The gas jet dispersion tray without amplification effect according to claim 2, wherein when the gas lift tube is formed by an arcuate cavity at the side of the base plate, the top plate of the gas lift tube is planar or circular arc-shaped;
an opening is formed in the side wall of the cavity of the gas lifting pipe, and the gas lifting pipe is communicated with the gas distribution pipe line through the opening;
the included angle alpha between the side wall of the cavity of the gas lift pipe and the base plate is 90-145 degrees.
5. The gas jet dispersion tray without amplification effect according to claim 3, wherein when the gas lift tube is formed by an arcuate cavity at the side of the base plate, the top plate of the gas lift tube is planar or circular arc-shaped;
an opening is formed in the side wall of the cavity of the gas lifting pipe, and the gas lifting pipe is communicated with the gas distribution pipe line through the opening;
the included angle alpha between the side wall of the cavity of the gas lift pipe and the base plate is 90-145 degrees.
6. The dispersive gas jet tray without amplification effect according to claim 4, wherein the junction between the side wall of the cavity of the gas lift tube and the base plate is provided with a rounded chamfer.
7. The dispersive gas jet tray without amplification effect according to claim 5, wherein the junction between the side wall of the cavity of the gas lift tube and the base plate is provided with a rounded chamfer.
8. Dispersive tray of gas jets without amplification effect according to claim 1, characterized in that: for tower equipment with the diameter of more than or equal to 2m, one or more distribution plates are arranged in the gas lift pipe to uniformly guide gas flow into the gas distribution pipeline.
9. Dispersive tray of gas jets without amplification effect according to claim 2, characterized in that: for tower equipment with the diameter of more than or equal to 2m, one or more distribution plates are arranged in the gas lift pipe to uniformly guide gas flow into the gas distribution pipeline.
10. Dispersive tray of gas jets without amplification effect according to claim 3, characterized in that: for tower equipment with the diameter of more than or equal to 2m, one or more distribution plates are arranged in the gas lift pipe to uniformly guide gas flow into the gas distribution pipeline.
11. Dispersive tray of gas jets without amplification effect according to claim 4, characterized in that: for tower equipment with the diameter of more than or equal to 2m, one or more distribution plates are arranged in the gas lift pipe to uniformly guide gas flow into the gas distribution pipeline.
12. Dispersive tray of gas jets without amplification effect according to claim 5, characterized in that: for tower equipment with the diameter of more than or equal to 2m, one or more distribution plates are arranged in the gas lift pipe to uniformly guide gas flow into the gas distribution pipeline.
13. Dispersive tray of gas jets without amplification effect according to claim 6, characterized in that: for tower equipment with the diameter of more than or equal to 2m, one or more distribution plates are arranged in the gas lift pipe to uniformly guide gas flow into the gas distribution pipeline.
14. Dispersive tray of gas jets without amplification effect according to claim 7, characterized in that: for tower equipment with the diameter of more than or equal to 2m, one or more distribution plates are arranged in the gas lift pipe to uniformly guide gas flow into the gas distribution pipeline.
15. Dispersive tray of gas jets without amplification effect according to any of the claims 1 to 14, characterized in that: the gas lift pipes are arranged in the arch areas on two sides of the substrate; the air rising pipes on the two sides are respectively connected with the air distribution pipes, and the air distribution pipes are equal in length;
the horizontal total sectional area of the top of the gas raising pipe is equal to the horizontal total sectional area of the gas distribution pipe.
16. Dispersive tray of gas jets without amplification effect according to any of the claims 1 to 14, characterized in that: when a plurality of air distribution pipes are arranged, a jet flow baffle is arranged at the position, located between two adjacent air distribution pipes, on the base plate.
17. Dispersive tray of gas jets without amplification effect according to claim 15, characterized in that: when a plurality of air distribution pipes are arranged, a jet flow baffle is arranged at the position, located between two adjacent air distribution pipes, on the base plate.
18. Dispersive tray of gas jets without amplification effect according to claim 16, characterized in that: and the lower part of the jet flow baffle is provided with a liquid communicating hole.
19. Dispersive tray of gas jets without amplification effect according to claim 17, characterized in that: and the lower part of the jet flow baffle is provided with a liquid communicating hole.
20. Dispersive tray of gas jets without amplification effect according to any of the claims 1 to 14, 17 to 19, characterized in that: the gas distribution pipeline adopts straight pipes or circular pipes with equal diameter or unequal diameters.
21. Dispersive tray of gas jets without amplification effect according to claim 15, characterized in that: the gas distribution pipeline adopts straight pipes or circular pipes with equal diameter or unequal diameters.
22. Dispersive tray of gas jets without amplification effect according to claim 16, characterized in that: the gas distribution pipeline adopts straight pipes or circular pipes with equal diameter or unequal diameters.
23. Dispersive tray of gas jets without amplification effect according to claim 20, characterized in that: the gas distribution pipes are arranged in a way of being vertical or parallel to the direction of liquid flow, or in a circular or radial way.
24. Dispersive tray of gas jets without amplification effect according to claim 21, characterized in that: the gas distribution pipes are arranged in a way of being vertical or parallel to the direction of liquid flow, or in a circular or radial way.
25. Dispersive tray of gas jets without amplification effect according to claim 22, characterized in that: the gas distribution pipes are arranged in a way of being vertical or parallel to the direction of liquid flow, or in a circular or radial way.
26. Dispersive tray of gas jets without amplification effect according to claim 20, characterized in that: the cross section of the gas distribution pipe is circular, conical, elliptical or rectangular.
27. Dispersive tray of gas jets without amplification effect according to claim 21, characterized in that: the cross section of the gas distribution pipe is circular, conical, elliptical or rectangular.
28. Dispersive tray of gas jets without amplification effect according to claim 22, characterized in that: the cross section of the gas distribution pipe is circular, conical, elliptical or rectangular.
29. Dispersive tray of gas jets without amplification effect according to claim 20, characterized in that: the wall thickness of the gas distribution pipe is 2-8 mm.
30. Dispersive tray of gas jets without amplification effect according to claim 21, characterized in that: the wall thickness of the gas distribution pipe is 2-8 mm.
31. Dispersive tray of gas jets without amplification effect according to claim 22, characterized in that: the wall thickness of the gas distribution pipe is 2-8 mm.
32. Dispersive tray of gas jets without amplification effect according to any of the claims 1 to 14, 17 to 19, 21 to 31, characterized in that: the horizontal projection shape of the jet hole is circular or rectangular.
33. Dispersive tray of gas jets without amplification effect according to claim 32, characterized in that: the rectangle is a square.
34. Dispersive tray of gas jets without amplification effect according to claim 15, characterized in that: the horizontal projection shape of the jet hole is circular or rectangular.
35. Dispersive tray of gas jets without amplification effect according to claim 34, characterized in that: the rectangle is a square.
36. Dispersive tray of gas jets without amplification effect according to claim 16, characterized in that: the horizontal projection shape of the jet hole is circular or rectangular.
37. The dispersive tray of gas jets without amplification effect according to claim 36, characterized in that: the rectangle is a square.
38. Dispersive tray of gas jets without amplification effect according to claim 20, characterized in that: the horizontal projection shape of the jet hole is circular or rectangular.
39. Dispersive tray of gas jets without amplification effect according to claim 38, characterized in that: the rectangle is a square.
40. Dispersive tray of gas jets without amplification effect according to claim 32, characterized in that: the jet hole is an equal-diameter through hole or a reducing through hole.
41. Dispersive tray of gas jets without amplification effect according to any of the claims 33 to 39, characterized in that: the jet hole is an equal-diameter through hole or a reducing through hole.
42. A dispersive tray of gas jets without amplification effect according to claim 40, wherein: the jet hole is a reducing through hole with a cone angle beta of less than 45 degrees.
43. A dispersive tray of gas jets without amplification effect according to claim 41, wherein: the jet hole is a reducing through hole with a cone angle beta of less than 45 degrees.
44. Dispersive tray of gas jets without amplification effect according to claim 32, characterized in that: the diameter of the jet hole is 2-10 mm.
45. Dispersive tray of gas jets without amplification effect according to any of the claims 33 to 39, characterized in that: the diameter of the jet hole is 2-10 mm.
46. Dispersive tray of gas jets without amplification effect according to claim 32, characterized in that: the jet holes of the air distribution pipe adopt a triangular fork arrangement mode, and the hole center distance is 1.5-10 times of the hole diameter.
47. Dispersive tray of gas jets without amplification effect according to any of the claims 33 to 39, characterized in that: the jet holes of the air distribution pipe adopt a triangular fork arrangement mode, and the hole center distance is 1.5-10 times of the hole diameter.
48. Dispersive tray of gas jets without amplification effect according to claim 32, characterized in that: on the multiple arranged air distribution pipes, 1-5 rows of jet holes are arranged downwards along the direction vertical to the air distribution pipes.
49. Dispersive tray of gas jets without amplification effect according to any of the claims 33 to 39, characterized in that: on the multiple arranged air distribution pipes, 1-5 rows of jet holes are arranged downwards along the direction vertical to the air distribution pipes.
50. Dispersive tray of gas jets without amplification effect according to any of the claims 1 to 14, 17 to 19, 21 to 31, 33 to 40, 42 to 44, 46, 48, characterized in that: and a nozzle perpendicular to the air distribution pipe is arranged below the jet hole.
51. Dispersive tray of gas jets without amplification effect according to claim 15, characterized in that: and a nozzle perpendicular to the air distribution pipe is arranged below the jet hole.
52. Dispersive tray of gas jets without amplification effect according to claim 16, characterized in that: and a nozzle perpendicular to the air distribution pipe is arranged below the jet hole.
53. Dispersive tray of gas jets without amplification effect according to claim 20, characterized in that: and a nozzle perpendicular to the air distribution pipe is arranged below the jet hole.
54. Dispersive tray of gas jets without amplification effect according to claim 32, characterized in that: and a nozzle perpendicular to the air distribution pipe is arranged below the jet hole.
55. A dispersive tray of gas jets without amplification effect according to claim 41, wherein: and a nozzle perpendicular to the air distribution pipe is arranged below the jet hole.
56. Dispersive tray of gas jets without amplification effect according to claim 45, characterized in that: and a nozzle perpendicular to the air distribution pipe is arranged below the jet hole.
57. A gas jet dispersion tray without amplification effect according to claim 47, wherein: and a nozzle perpendicular to the air distribution pipe is arranged below the jet hole.
58. Dispersive tray of gas jets without amplification effect according to claim 49, characterized in that: and a nozzle perpendicular to the air distribution pipe is arranged below the jet hole.
59. Dispersive tray of gas jets without amplification effect according to claim 20, characterized in that: the upper edge of the nozzle is flush with the jet hole or extends into the central position of the gas distribution pipe to be connected with a section of horizontal pipe section.
60. A dispersive tray of gas jets without amplification effect according to any of claims 51 to 58, wherein: the upper edge of the nozzle is flush with the jet hole or extends into the central position of the gas distribution pipe to be connected with a section of horizontal pipe section.
61. A dispersive tray of gas jets without amplification effect according to claim 50, characterised in that: the nozzle is cylindrical or conical.
62. A dispersive tray of gas jets without amplification effect according to any of claims 51 to 58, wherein: the nozzle is cylindrical or conical.
63. A dispersive tray of gas jets without amplification effect according to claim 50, characterised in that: the length of the nozzle outside the gas distribution pipe is 1-8 times of the diameter of the nozzle.
64. A dispersive tray of gas jets without amplification effect according to any of claims 51 to 58, wherein: the length of the nozzle outside the gas distribution pipe is 1-8 times of the diameter of the nozzle.
65. A method of designing a dispersive tray of gas jets without amplification effect as claimed in any of claims 1 to 64, in which: the method comprises the steps of determining the distance from a gas distribution pipeline to a substrate according to the height of the gas distribution pipeline on a liquid surface and the depth of gas injection into the liquid surface;
wherein the height of the gas distribution pipeline on the liquid level is determined according to the following formula:
in the formula: r is the radius of the gas jet when it reaches the liquid surface, and the unit is m; r is0Is the gas nozzle exit radius in m; h is the distance from the jet hole to the liquid plane, and the unit is m; u. ofmThe central axis speed when the gas is sprayed to the liquid surface is in m/s; u. of0The velocity of the outlet section of the jet hole is expressed in m/s; k is a proportionality coefficient and is determined by experiments; phi is the exit shape coefficient; a is a turbulence coefficient, and is related to the turbulence intensity and the speed distribution uniformity of the nozzle section;
the depth of the gas jet into the liquid surface is determined according to the following formula:
f(L,d0,τ,h,θ,μ,ρg,w)＝0 (4)
L'＝f(h',d',θ,R1) (8)
when the liquid viscosity is <2mPa · s, it is reduced to the following correlation:
L'＝A/(h'2+B) (9)
L'＝A/(h'2+B)+exp(-h')L' (10)
in the formula: l is the depth of gas injection into the liquid surfaceIn the unit of m; d0The diameter of the jet hole is m; τ is gas impact force, N; theta is an included angle between the jet hole and the liquid level; mu is gas viscosity and has a unit of Pa.s; rhogIs the gas density in kg/m3；ρLIs the liquid density in kg/m3(ii) a w is the specific gravity of the liquid; f is a function expression; A. and B are model coefficients.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201711351265.6A CN107899535B (en) | 2017-12-15 | 2017-12-15 | Gas jet flow distributed tower plate without amplification effect and design method thereof |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201711351265.6A CN107899535B (en) | 2017-12-15 | 2017-12-15 | Gas jet flow distributed tower plate without amplification effect and design method thereof |
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| CN107899535A CN107899535A (en) | 2018-04-13 |
| CN107899535B true CN107899535B (en) | 2019-12-27 |
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| CN1264595C (en) * | 2004-11-16 | 2006-07-19 | 天津市创举科技有限公司 | Compound absorption tray |
| CN202376859U (en) * | 2011-12-23 | 2012-08-15 | 青岛京润石化设计研究院有限公司 | Gas-liquid separator |
| FR2989595B1 (en) * | 2012-04-18 | 2014-04-11 | IFP Energies Nouvelles | PARTITION DISPENSER PLATE FOR OFFSHORE GAS / LIQUID CONTACT COLUMN |
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