CN1098728C - Eddy-current ultragravitational field reactor and its application - Google Patents
Eddy-current ultragravitational field reactor and its application Download PDFInfo
- Publication number
- CN1098728C CN1098728C CN99105437A CN99105437A CN1098728C CN 1098728 C CN1098728 C CN 1098728C CN 99105437 A CN99105437 A CN 99105437A CN 99105437 A CN99105437 A CN 99105437A CN 1098728 C CN1098728 C CN 1098728C
- Authority
- CN
- China
- Prior art keywords
- eddy
- ultragravitational
- current
- reative cell
- continuous phase
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Fee Related
Links
Images
Landscapes
- Physical Or Chemical Processes And Apparatus (AREA)
Abstract
The present invention relates to a pneumatic eddy super gravity field reactor which is characterized in that the reactor is provided with at least one reaction chamber, and a continuous phase inlet is arranged on the reaction chamber; a fixed supporter is arranged in the reaction chamber, carriers that reactants can be attached to are arranged on the supporter, and the continuous phase inlet and the supporter are tangentially arranged; a liquid distributor is arranged at a corresponding position to the reaction chamber, a separation chamber is connected with the rear part of the last-level reaction chamber, and the continuous phase outlet is arranged in the separation chamber; the chambers are separated from each other by partitions and are communicated with each other through clearances of the partitions; a liquid collector and a discharge opening are arranged at the lower part of the device. The reactor is used in the transference and reaction processes of two-phase or multiphase materials such as the physical and chemical reaction between phases of various materials, such as steam to liquid, liquid to liquid and steam to liquid to solid.
Description
Technical field
The present invention relates to a kind of eddy-current ultragravitational field reactor that is used for Chemical Manufacture or waste product purification process reinforcement transmission, especially for the transfer reaction process that comprises two-phase or multiphase system.As the physical-chemical reaction between the phase border of vapour one liquid, liquid-liquid, each system of vapour-liquid-solid.
Background technology
In the conventional mass transfer apparatus, the alternate transmission of material and reaction effect are except outside the Pass having with factors such as the physico-chemical property of participating in the vapour-liquid solid phase self of reacting, humidity, pressure, and be also relevant with size, flow condition and the relative velocity of alternate contact area.In traditional equipment (as packed tower, plate column, nethike embrane tower etc.), liquid phase is from top to bottom to flow naturally by gravity, therefore liquid film is thick, flow velocity is low, the time of staying is long, this mass transport process and selectivity absorption to liquid phase control is very disadvantageous, to gas phase owing to be subjected to the restriction of the buoyancy factor, the gas speed ratio of flooding point is lower, and this is for the mass transport process of strengthening gas phase control, and it also is disadvantageous reducing equipment volume.
At the problems referred to above, people develop the extra gravity field device (being called for short overweight machine) that a class is called RPB in recent years.Be a kind of equipment that transmits with mixed process of strengthening with centrifugal force, the typical structure of this kind equipment is characterized as by sealed enclosure and the belt packed bed that can rotate at a high speed to be formed, in the middle of the ring packing layer of rotor, be provided with liquid distribution trough, liquid ring and enter filler in the filler, the side of casing has air admission hole, under the effect of barometric gradient, gas enters packed layer, vapour-liquid phase counter current contacting in filler by annular packed bed filler outer shroud.This kind equipment the time can produce in operation to be stablized adjustable centrifugal force field and makes the buoyancy factor improve 1～3 order of magnitude, liquid in super gravity field owing to be subjected to the effect of great shear forces, be drawn as film as thin as a wafer, very thin silk and small dripping, the surface is upgraded rapidly, produce huge alternate contact area, therefore greatly improved mass transfer rate, also improved spotting out gas speed.Everything is all highly beneficial to strengthening mass transport process, and can reduce equipment volume significantly, reduces investment.Owing to have good feature, solved many under normal gravitational field insoluble problem, therefore in separation processes such as absorption, parsing, distillation, use and obtained outstanding achievement.But, because overweight machine is with moving Dai Jing, with machine for tower, so just must solve the movable sealing of machine, the stability of machine operation, reliability, problem such as chronicity and maintenance, when especially handling a large amount of material, it is too big that RPB is not easy to do, substitute with a plurality of minicomputers, then investment, power consumption, operational management all can increase suddenly, in addition because of dynamically balanced reason, the rotating speed of RPB can not be too high, these problems have all directly restricted applying of overweight machine, and this kind equipment only utilized the effect of centrifugal force field, and the characteristic in rotary fluid center (vortex core district) is failed to consider.
Summary of the invention
The purpose of this invention is to provide a kind of eddy-current ultragravitational field reactor, make it moving, thoroughly solve because of the existing problem of mechanical movement with quiet generation; Make full use of the characteristic of rotating fluid, further improve reaction efficiency; And can be applicable to multiple phase material flow in super gravity field, participate in the reaction device.
The object of the present invention is achieved like this, and a kind of eddy-current ultragravitational field reactor is characterized in that being provided with at least a reative cell, is provided with the continuous phase import in reative cell; Establish fixed support body in the reative cell, but be provided with the carrier of attachment reaction thing in this supporter, this continuous phase import and this carrier tangentially are provided with; Corresponding position with carrier in the reative cell is provided with liquid distributor; Connect a separation chamber in the rear portion of afterbody reative cell, the separation chamber is located in this continuous phase outlet; Between every chamber by baffle region every, and by the gap mutual conduction of dividing plate; Establish catch box and discharging opening in this device bottom.
The carrier that above-mentioned supporter is provided with can be a nethike embrane, and this nethike embrane can be vortex shape, sheet is tabular or multi-layer combined, also can be annular, star, spirality, wing.Described carrier can be honeycomb filler or packed bed.The phase import of advancing continuously of being somebody's turn to do presents the convergence shape, is provided with lash adjusting device in the continuous phase import of its convergence shape.Reative cell can be contacted more than two, separated by dividing plate therebetween, and by the gap conducting of dividing plate periphery, catch box can be located at the lower end of reative cell, is provided with the discharge opeing slit in this catch box and reacting chamber space.This catch box also can be located at the lower end of separation chamber, is provided with the discharge opeing slit between this catch box and separation chamber.Described reative cell can be gone up, following series connection is provided with two reacting chamber spaces and is provided with demarcation strip, and logical by mutual conductance on the through hole on the dividing plate, the separation chamber can be located at the upper end of upper strata reative cell, the upper end of separation chamber is located in the continuous phase outlet, and liquid distributor is located at the upper end of the carrier of attachment reaction thing on the supporter.
This device can be applicable to absorption, absorption, parsing, distillation, drying, catalyzed conversion, liquid-liquid extraction, tail gas clean-up and the dust collecting process in the industries such as oil, chemical industry, metallurgy, pharmacy, food, environmental protection, and among the preparation technology of viscosity number less than the material of 10 pools.
Operation principle of the present invention is that base main body structure of the present invention is a device that comprises continuous phase import, liquid distributor, reative cell, separation chamber, reaches the continuous phase outlet, establishes catch box and discharging opening in this device bottom; Fixed support body is housed in the reative cell, but is provided with the carrier of attachment reaction thing in this supporter, as the vortex-like rack of hollow or packed bed etc., this continuous phase import and this carrier tangentially are provided with; Reative cell and separation chamber are separated by a dividing plate.During the equipment operation, (is example as continuous phase with gas), air-flow is by placing the tangential continuous phase import that is provided with of reative cell one side to import, and at stable super gravity field of reaction indoor high-speed rotation formation, its rotating speed can be by fan pressure and the lash adjusting device control that is positioned at import, continuous phase can be reacting gas itself, also can be only as power.Reactant liquor evenly sprays to rack by liquid distributor and forms liquid film, because the high-speed cutting campaign of air-flow, the surface of reactant carrier is under pressure, and the continuous attenuation of liquid film is until tearing up, atomize and forming microgranular dispersion rapidly.For the interphase mass transfer of reactant provides greatly and the contact surface of bringing in constant renewal in, mass tranfer coefficient enlarges markedly, the also corresponding quickening of reaction rate.Add strong stirring action uniformly of this device and high-velocity fluid to the suspension effect of dispersion, all provide sufficient necessary condition for the absorption between system, absorption, catalyzed conversion, power conversion and mass transfer between phases.
What is particularly worth mentioning is that rotating fluid can be divided into two characteristic areas, quasi-potential stream district and like Gu Qu (or claiming vortex core).Fluid is a laminar flow characteristics in quasi-potential stream district, is made as the master with centrifugal separator, and big particle diameter material separates at this; Intersection (transition region) the tangential velocity maximum in quasi-potential stream district and vortex core district; The fluid rotating speed reduces rapidly along radius in the vortex core, be tending towards 0 during to the center, pressure is tending towards-∞ at this, particulate is by a large amount of " suction ",, effectively separated during once more by transition region after the coalescence quality increases through collision at this micronic dust, droplet, but existing cyclonic unit mostly all the center of being designed to go out stream, particulate goes out thereupon, so the ubiquity weakness low to the micro particle catching rate.The present invention then changes device into periphery and goes out the stream mode, keeps and effectively utilized the above-mentioned feature of rotary body, causes the arresting efficiency to particulate to be greatly improved, and has guaranteed absorption, has been separated in this equipment and once finishes.Reacted liquid gets rid of to wall because of centrifugal action and flows into liquid holding box downwards.Gas then enters the separation chamber through further discharging or reclaim (also can be recycled) after the dehumidifying by the slit of plate washer periphery.Liquid and solid are then emitted by discharging opening in good time.
Be not difficult to find out that owing to adopt such scheme, this device is compared with prior art possesses following characteristics:
1. this device is power with continuous phase, and the continuous phase that is adopted can be gas, also can be liquid.Continuous phase can be participated in reaction, also can be only as power; Can be single, also can be two or more mixtures.
2. the super gravity field that is formed by the control of blower fan (or pump) and import aperture, scooter commentaries on classics up to ten thousand (have overweight machine rotating speed now and be generally 1-2 thousand right side of turning left) are changeed in stable and reliable operation.Speed governing is arbitrarily easy, and startup-shutdown is rapid, and gets final product operation under positive pressure, but also negative pressure operation.
3. the vortex-like rack of hollow is moving with quiet generation, does not have the machine operation problem, and rotation gas is repeatedly cutting with it, and relative velocity is very high, can make online liquid-sheet atomization, and the surface is brought in constant renewal in, and alternate contact area is very big, and mass tranfer coefficient is very high.
4. vortex-like rack can be designed to hollow, can avoid stopping up, and can also effectively utilize the centrifugation of the characteristic and the transition region in vortex core district simultaneously, improves the arresting efficiency to particulate.
5. because of this device has the impact atomizing, thus less demanding to liquid distributor self, the power consumption and the problems such as corresponding wearing and tearing and obstruction of having removed various atomizers (as rotary atomizer, jet atomization device) from.Liquid distributor can be a plurality of, is used for various materials and participates in reaction.
6. the whirlpool net can be made into various forms.As vortex-like packed bed, vortex-like plate etc., also can be made into other shapes, as annular, star, spirality, sheet, rack or packed bed such as wing.Net, plate and filling surface can be got involved catalyst, and rack is an integral body, and easy accessibility is easy to safeguard and change, applicable to multiple differential responses occasion.
7. reative cell can be designed to plural serial stage tandem type, and differential responses (absorbing as selectivity) are finished continuously.Also can in parallelly use, handle the reaction of a large amount of materials.
8. can be widely used in the various technical processes such as preparation, absorption, absorption, parsing, distillation, drying, catalyzed conversion, liquid-liquid extraction, tail gas clean-up and dedusting in the industries such as oil, chemical industry, metallurgy, pharmacy, food, environmental protection.
9. simple in structure, working service is convenient.
10. power consumption is little, and operating cost is cheap.
Description of drawings
Fig. 1 is the structure outside drawing of first kind of embodiment of the present invention.
Figure 1A is the right view of Fig. 1.
Figure 1B is the vertical view of Fig. 1.
Fig. 2 is the B-B cutaway view of Figure 1A.
Fig. 3 is the B-B cutaway view of Fig. 1.
The structural representation of Fig. 4 second kind of embodiment of the present invention.
The structural representation of Fig. 5 the third embodiment of the present invention.
The structural representation of Fig. 6 the 4th kind of embodiment of the present invention.
The structural representation of Fig. 7 the 5th kind of embodiment of the present invention.
The structural representation of Fig. 8 hollow of the present invention whirlpool net.
MULTILAYER COMPOSITE nethike embrane structural representation among Fig. 9 the present invention.
The structural representation of spiral whirlpool net among Figure 10 the present invention.
The structural representation of Figure 11 ring-type of the present invention whirlpool net.
The structural representation of starlike whirlpool net among Figure 12 the present invention.
The structural representation of wing whirlpool net among Figure 13 the present invention.
The specific embodiment
Below in conjunction with accompanying drawing, by description detailed description the present invention of embodiment.
With reference to Fig. 1～Fig. 3, eddy-current ultragravitational field reactor of the present invention, at least one comprises continuous phase import 1, liquid distributor 8, reative cell 2, separation chamber 3, and device such as continuous phase outlet 4, establishes catch box 6 and discharging opening 7 in this device bottom; The reactant carrier is housed in the reative cell 2, and this carrier is the vortex-like net 11 of hollow in the present embodiment; Reative cell 2 is separated by a plate washer 9 with separation chamber 3.Hollow whirlpool net 11 and main body are made split type, and easy accessibility is beneficial to maintenance, and different nethike embrane forms can be housed on hollow whirlpool net 11 as required.
As shown in Figures 2 and 3, in the present embodiment, this continuous phase import 1 is convergence shape inlet, and it is provided with a wedge block 13 in this is the continuous phase inlet 1 of restraining shape, this wedge block 13 can move up and down along this continuous phase inlet 1, adjusts the size of the opened gap of this continuous phase inlet 1 with this.The lift adjustment mechanism that the adjustment structure that moves up and down of this wedge block 13 is general conventional constitutes, and (for example adopting structure that slideway matches with protruding pin or jackscrew ejection structure or the like) do not repeat them here.
In the present embodiment, hollow whirlpool net 11 as shown in Figure 8.It includes inside and outside two layers of mesh support 12, and is connected with the nethike embrane 14 of several arcuations in inside and outside between the two layers of mesh support 12, is hollow whirlpool net 11 with formation.This hollow whirlpool net 11 is located in this reative cell 2 regularly.The above-mentioned nethike embrane 14 that advances on phase direction and this hollow whirlpool net 11 that is the continuous phase import 1 that restrains shape is tangent.
As shown in Figure 2, in present embodiment, the below of reative cell 2 is provided with a catch box 6, and is provided with a discharge opeing slit 10 between reative cell 2 and catch box 6.The below of catch box 6 is provided with discharging opening 7.
Be connected with a separation chamber 3 in the rear portion of reative cell 2, reative cell 2 is separated by a dividing plate 9 with separation chamber 3, and the bottom of separation chamber 3 is provided with cannelure and leakage fluid dram 5 and has solved air-teturning mixed phenomenon during vapour-liquid is separated admittedly well.Separation chamber 3 is located in 4 of the outlets of continuous phase.
Below just the present invention one use embodiment to further specify operation principle of the present invention.
In this use embodiment, continuous phase is gas, and promptly from the boiler smoke behind the multi-tube dust cleaner, needing in the flue gas to purify the component of removing is micronic dust and SO
2, absorption liquid is a lime slurry.
The present invention is when work, plume is by continuous phase import 1 tangential importing and form a high speed vortex shape super gravity field in reative cell 2, the hollow whirlpool net of air-flow and hollow intersects for more than 11 time, producing very high relative velocity smashes the moisture film that liquid distributor 8 is sprayed on the nethike embrane 14, it is long-pending so just to obtain contact surface great, that bring in constant renewal in, and because of the heat transmission of plume self makes water droplet further evaporate atomizing, the vapour-liquid contact-making surface further increases, and has improved Ca very effectively
2+With water to SO
2The absorption conversion strength and to the arresting efficiency of micronic dust; After entering the micronic dust in vortex core district and water smoke and collide coalescence mutually with air-flow, tackled by moisture film when entering the whirlpool net once more, participate in SO after the contained basic anhydride stripping in the micronic dust
2Absorption, can reduce the consumption of absorption liquid alkaline matter, reduce the internal circulating load of liquid.After reaction was finished, liquid was got rid of to wall by centrifugal action together with its grit of carrying secretly, flowed into catch box 6 from slit 10, and was discharged by discharging opening 7 controls; The purified gas then slit by plate washer 9 peripheries enters separation chamber's 3 dehumidifying back liquid and is pressed in the cannelure of bottom and by leakage fluid dram 5 by air-flow and flows out; Then return in gas and to enter this outlet 4 dischargings continuously along continuous phase outlet 4 pipe outer walls.This version has reduced air-teturning mixed phenomenon effectively, has further guaranteed clean-up effect.If dustiness is too big or to SO
2Purifying rate require highly, also can adopt the structure of embodiment shown in Figure 4, two sections purification styles of tandem; Big as the smoke treatment amount, then can many in parallel uses.
Structure shown in the present embodiment also can be applicable among the lower preparation technology of product viscosity.
For example: with CO
2Gas is as continuous phase, with FeSO
2, ZnSO
4, MnSO
2Mixed liquor and ammoniacal liquor produce the ultra-fine powder of manganese-zinc ferrite.
During operation, CO
2Gas is imported by the continuous phase import 1 that places reative cell 2 one side tangential position, and rotates stable super gravity field of formation at a high speed in reative cell 2.Its rotating speed can be by blast and the wedge block that is positioned at import 13 controls, and reactant liquor evenly sprays to rack by liquid distributor 8 and forms liquid film.Because the dissection of air-flow asks that at nethike embrane vapour-liquid forms microgranular dispersion, for the transfer reaction of vapour one liquid-liquid three alternate materials has been created sufficient condition.After reaction was finished, liquid and particulate got rid of to wall because of centrifugal force, collected unreacted CO by catch box 6
2Gas enters 3 further dehumidifying backs, separation chamber by continuous phase outlet 4 discharges by the slit of plate washer 9 peripheries, recycles.Emulsion is discharged by discharging opening 7 in good time, obtains the ultra-fine powder of manganese-zinc ferrite through the postorder processing.
Fig. 4 illustrates the structure of second kind of embodiment of the present invention.In the present embodiment, the reative cell 2 of two same structures contacting side by side in front and back, the structure of these two reative cells 2 and first kind of embodiment are identical.In 2 of two reative cells separately, utilize the gap of the periphery of this dividing plate 92 conductings of two reative cells to be formed the mode of two-step serial by a dividing plate 9.The structure of present embodiment can be applicable to multistage and absorbs processing.Its operation principle is as follows:
The SO of the first order in the high concentration ammonium sulfite solution absorption sulfur process tail gas
2, guarantee to pay the concentration requirement of product ammonium sulfite with this.Remaining SO
2The solution lower with concentration in the second level further absorbs to guarantee SO in the tail gas
2Content reaches discharge standard.The absorption liquid concentration of back one utmost point is used further to the first order when bringing up to certain degree.Two towers that desirable like this generation is industrial.And the problem of non-secondary pollution.
Fig. 5 illustrates the third embodiment of the present invention, in the present embodiment, includes a reative cell 2, is fixed with hollow whirlpool net 11 in it, is provided with liquid distributor 8 in the center of hollow whirlpool net 11.These reative cell 2 upper ends slightly relatively axial centre place of hollow whirlpool net 11 are provided with continuous phase import 1.The rear portion of this reative cell 2 is provided with one is axially separated by dividing plate 9 between the Room 3, two, separation chamber of lengthening, and by the gap mutual conduction of dividing plate 9 peripheries.Separation chamber 3 is located in continuous phase outlet 4, is provided with a discharge opeing slit 10 in the bottom of this separation chamber 3 and is communicated in a catch box 6.Be provided with discharging opening 7 in the lower end of catch box 6; It is split type that rack 11 and main body are made, and nethike embrane 14 be in close outer form of dredging, can effectively control the generation of droplet.
The structure of present embodiment is mainly used in the liquid-liquid extraction.
Existing extraction tower has the effective depth of 60%-90% approximately in order to remedy the adverse effect that is caused owing to vertical immixture, can not strengthen arbitrarily by the material liquid of extraction tower and the flow of extractant in the unit interval simultaneously, otherwise will produce liquid flooding.So just make that the volume of extraction tower is very big, and output efficiency is not high.Adopt baud formula and Lu Wei formula centrifugal extractor reduction equipment volume greatly, increase productivity.But similar with overweight machine, this kind equipment needs bigger power consumption and faces more numerous and diverse maintenance of machine problem.
Utilize the eddy current type extra gravity field device shown in the present embodiment can solve above-mentioned contradiction preferably.Lengthening separation chamber and catch box placed separation chamber's end on the base main body architecture basics in the present embodiment.Be continuous phase with the light liquid during operation, heavy-fluid is then added by liquid distributor, the reverse contact of two-phase (because of heavy-fluid viscosity bigger, the delay effect of whirlpool net can hinder it and form droplet, thereby has stopped the phenomenon of emulsification), the heavy-fluid of dispersion is dripped because of centrifugal action and is shifted to the reactor outer rim gradually, reaction back two-phase enters the separation chamber simultaneously, after the layering, light liquid is discharged by the continuous phase outlet, and heavy-fluid then enters catch box by discharging opening control discharging.
Fig. 6 illustrates the 4th kind of embodiment of the present invention.Include two reative cells 2 of serial connection up and down at present embodiment, in each reative cell 2, be provided with rack 11, be provided with 2 of continuous phase import 1, two reative cells in these rack 11 tangent horizontal directions and separate, be distributed with through hole 91 on this dividing plate 9 by dividing plate 9; The lower end of lower floor's reative cell 2 is separated by dividing plate 9 and is provided with a catch box 6, and dividing plate 9 herein can be the taper setting, by the hole conducting of the periphery of this dividing plate 9 and center in lower floor's reative cell 2.The top of upper strata reative cell 2 connects between Room 3, two, a separation chamber and is also separated by dividing plate 9, and by the peripheral conducting of dividing plate 9, continuous phase outlet 4 is by the upper end of being located at this separation chamber 3.8 tops of being located at the upper strata reative cell of liquid distributor.
Present embodiment is to be applied to evaporating and concentrating process, for example in existing black liquid alkali recovery process, sprays into combustion furnace again after often needing with multi-effect evaporator rare black liquor to be concentrated and burns organic matter.This technological process is long, and heat energy loss is big.
Equipment is when moving row, and the flue gas sectional tangentially enters, and black liquor sprays to hollow whirlpool net 11 by top annular liquid distributor 8, nethike embrane 14 adopts multi-layer combined as shown in Figure 9, in order to improve the carrier fluid amount, to compare with existing empty body single flow spray drying tower, efficient greatly improves.
Because the present invention has extremely strong dispersiveness and certain liquid ability of holding to liquid, and can make thermal plume in device, keep the long time of staying, heat energy utilization rate height.Therefore available paper plant provides the flue gas of boiler for oneself or directly with the flue gas of combustion furnace black liquor is concentrated and even evaporate, and meanwhile also can efficiently remove coal dust and SO in the flue gas
2, receive good economic benefit and environmental benefit.
Fig. 7 illustrates the 5th kind of embodiment of the present invention.Structure shown in the present embodiment can be applicable to catalytic combustion.In the burning cleaning system of organic exhaust gas, adopt the catalytic combustion mode can make initiation temperature reduce to 523-623K, the time of staying shortens to 0.005-0.01s.Present embodiment can constitute the combustion chamber in a kind of burning cleaning system of organic exhaust gas, see also shown in Figure 7, include a reative cell 2, continuous phase adopts organic exhaust gas, and enter by continuous phase import 1 at a high speed, being provided with hollow whirlpool net 11 in the reative cell 2, this hollow whirlpool net 11 can adopt structure as shown in Figure 8 in the present embodiment, and the wire netting of intervention catalyst, also can adopt with the metal beehive carrier of getting involved catalyst and make compound rack, the structure that goes out as shown in figure 10, every interlayer stays the 10-20mm space, insulate with pottery magnetic support in two ends, online joining power is connected power supply before the ignition, get final product direct heatable catalyst, after reaching ignition temperature, powered-down.Organic exhaust gas tangentially enters the combustion chamber, and rotation is advanced, and has improved the moving and time of staying of air-flow greatly, and efficiency of combustion can obviously increase.
Figure 10 to Figure 13 illustrates the different structure of whirlpool of the present invention net, and the user can select for use according to different user demands.A kind of spiral helicine whirlpool net 15 shown in Figure 10, net 15 no hollow cores in this kind whirlpool are located in the structure of upper end of reative cell 2 structure that goes out as shown in Figure 6 so it often is used in liquid distributor 8; A kind of ring-type whirlpool net 16 shown in Figure 11, this ring-type whirlpool net 16 can increase the time of break-through of two phase reaction thing, increases its reaction time in reative cell 2 with this; Shown in Figure 12 is a kind of star whirlpool net 17, and net 17 each plate body in star whirlpool are two-layer about in the of 171 is made of nethike embrane 172 for this, can be folded with honeycomb filler 173 in the middle of two-layer nethike embrane 172; Shown in Figure 13 is a kind of wing whirlpool net 18, has bending-like wing 182 on the nethike embrane 181 of this kind wing whirlpool net 18, and this kind structure can increase the surface area of nethike embrane 181, and increasing its reactant with this has adhesive ability.
Claims (14)
1, a kind of eddy-current ultragravitational field reactor is characterized in that being provided with at least a reative cell, is provided with the continuous phase import in reative cell; Establish fixed support body in the reative cell, but be provided with the carrier of attachment reaction thing in this supporter, this continuous phase import and this carrier tangentially are provided with, and gas tangentially enters in the reative cell at a high speed by this continuous phase import and forms the eddy current that rotates at a high speed in this reative cell; Corresponding position with this carrier in the reative cell is provided with liquid distributor; Connect a separation chamber in the rear portion of afterbody reative cell, the separation chamber is located in this continuous phase outlet; Between per two reative cells and the reative cell and between reative cell and separation chamber respectively by baffle region every, and by the gap mutual conduction of dividing plate; Establish catch box and discharging opening in this device bottom.
2, a kind of eddy-current ultragravitational field reactor according to claim 1 is characterized in that the carrier that described supporter is provided with is a nethike embrane, and this nethike embrane is a vortex shape, sheet is tabular or multi-layer combined.
3, a kind of eddy-current ultragravitational field reactor according to claim 1 and 2 is characterized in that the nethike embrane that described supporter is provided with is annular, star, spirality, wing.
4, a kind of eddy-current ultragravitational field reactor according to claim 1 is characterised in that described carrier is the honeycomb filler.
5, a kind of eddy-current ultragravitational field reactor according to claim 1 is characterised in that described carrier is a packed bed.
6, a kind of eddy-current ultragravitational field reactor according to claim 1 is characterized in that described continuous phase import presents the convergence shape, is provided with lash adjusting device in the continuous phase import of its convergence shape.
7, a kind of eddy-current ultragravitational field reactor according to claim 1 is characterised in that described reative cell can be polyphone more than two, separates by dividing plate therebetween, and by the gap conducting of dividing plate periphery.
8, a kind of eddy-current ultragravitational field reactor according to claim 1 is characterized in that described catch box can be located at the lower end of reative cell, is provided with the discharge opeing slit in this catch box and reacting chamber space.
9, a kind of eddy-current ultragravitational field reactor according to claim 1 is characterized in that described catch box can be located at the lower end of separation chamber, is provided with the discharge opeing slit between this catch box and separation chamber.
10, a kind of eddy-current ultragravitational field reactor according to claim 1 is characterized in that described reative cell can go up, and following series connection is provided with, and two reacting chamber spaces are provided with demarcation strip, by the through hole mutual conduction on the dividing plate.
11, according to claim 1 or 10 described a kind of eddy-current ultragravitational field reactors, it is characterized in that described separation chamber can be located at the upper end of upper strata reative cell, the upper end of separation chamber is located in the continuous phase outlet.
12,, it is characterized in that described liquid distributor is located at the upper end of the carrier of the attachment reaction thing on the supporter according to claim 1 or 10 described a kind of eddy-current ultragravitational field reactors.
13, a kind of eddy-current ultragravitational field reactor according to claim 1 is characterized in that described liquid distributor can be not several of reactant liquor of the same race of input.
14, a kind of application of eddy-current ultragravitational field reactor, it is characterized in that this device can be applicable to absorption, absorption, parsing, distillation, drying, catalyzed conversion, liquid-liquid extraction, tail gas clean-up and the dust collecting process in oil, chemical industry, metallurgy, pharmacy, food, the environmental protection industry (epi), and viscosity number is less than the preparation technology of the material of 10 pools.
Priority Applications (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN99105437A CN1098728C (en) | 1999-04-06 | 1999-04-06 | Eddy-current ultragravitational field reactor and its application |
| AU52771/99A AU5277199A (en) | 1999-03-31 | 1999-08-12 | Supergravitational field vortex reactor and the use thereof |
| PCT/CN1999/000114 WO2000059599A1 (en) | 1999-03-31 | 1999-08-12 | Supergravitational field vortex reactor and the use thereof |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN99105437A CN1098728C (en) | 1999-04-06 | 1999-04-06 | Eddy-current ultragravitational field reactor and its application |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1269256A CN1269256A (en) | 2000-10-11 |
| CN1098728C true CN1098728C (en) | 2003-01-15 |
Family
ID=5271983
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN99105437A Expired - Fee Related CN1098728C (en) | 1999-03-31 | 1999-04-06 | Eddy-current ultragravitational field reactor and its application |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1098728C (en) |
Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100417436C (en) * | 2005-07-14 | 2008-09-10 | 中国石油化工股份有限公司 | Catalytic selective hydrogenation |
| CN106865674B (en) * | 2017-03-01 | 2020-06-05 | 煤炭科学技术研究院有限公司 | Method for extracting and dephenolizing phenol-containing wastewater by multistage mixing and enhanced separation |
| CN113083179B (en) * | 2021-03-02 | 2022-12-30 | 北京化工大学 | Preparation system and application of methoxyamine hydrochloride by coupling supergravity with ultrasound and microwaves |
| CN114713014A (en) * | 2022-03-23 | 2022-07-08 | 成都兴鑫悦环保技术开发有限公司 | Rotary packed bed of honeycomb type hypergravity machine |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4382900A (en) * | 1980-09-01 | 1983-05-10 | Imperial Chemical Industries Plc | Centrifugal gas-liquid contact apparatus |
| CN1062098A (en) * | 1992-01-16 | 1992-06-24 | 北京化工学院 | The rotating bed super gravity field device that has aspirator |
| US5362464A (en) * | 1987-03-02 | 1994-11-08 | Turbotak Inc. | Method for removing sulfur oxides |
| CN1116125A (en) * | 1995-07-06 | 1996-02-07 | 北京化工大学 | Extra gravity field device of cross current rotary bed |
| CN2221437Y (en) * | 1995-07-04 | 1996-03-06 | 北京化工大学 | Over-gravity field device of rotary bed for reinforcing transfer reaction |
-
1999
- 1999-04-06 CN CN99105437A patent/CN1098728C/en not_active Expired - Fee Related
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4382900A (en) * | 1980-09-01 | 1983-05-10 | Imperial Chemical Industries Plc | Centrifugal gas-liquid contact apparatus |
| US5362464A (en) * | 1987-03-02 | 1994-11-08 | Turbotak Inc. | Method for removing sulfur oxides |
| CN1062098A (en) * | 1992-01-16 | 1992-06-24 | 北京化工学院 | The rotating bed super gravity field device that has aspirator |
| CN2221437Y (en) * | 1995-07-04 | 1996-03-06 | 北京化工大学 | Over-gravity field device of rotary bed for reinforcing transfer reaction |
| CN1116125A (en) * | 1995-07-06 | 1996-02-07 | 北京化工大学 | Extra gravity field device of cross current rotary bed |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1269256A (en) | 2000-10-11 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN1122554C (en) | Separating device | |
| US20080066622A1 (en) | Reflecting packed column | |
| CN205517261U (en) | Minimum discharge of many pollutants of industry coal fired boiler flue gas is desorption system in coordination | |
| CN2808276Y (en) | Large-volume high-concentration fume purifying equipment | |
| CN2382463Y (en) | Pneumatic eddy super gravity field reactor | |
| CN1281297C (en) | Dry process stack gas desulfur reaction tower with variation structure | |
| CN1098728C (en) | Eddy-current ultragravitational field reactor and its application | |
| CN2936409Y (en) | Super-filter water purifier | |
| CN113996170A (en) | Efficient dedusting, demisting and whiting device after desulfurization and treatment method | |
| WO2011102749A1 (en) | Packet-type vortical packing for heat and mass exchange column-type apparatuses | |
| CN2396883Y (en) | Conical cyclone gas distributing machine | |
| WO2000059599A1 (en) | Supergravitational field vortex reactor and the use thereof | |
| CN201752626U (en) | Super-gravity multi-cyclone dust elimination and desulfurization multifunctional device | |
| CN110339675A (en) | A kind of method and apparatus removing isopropanol gas | |
| CN1221644A (en) | Cyclone dispersion absorbing/separating process and absorbing tower | |
| CN2537467Y (en) | Forced vortex-absorption adsorptive gas-liquid separator | |
| CN214597998U (en) | SO in flue gas after wet desulphurization3Device of high-efficient desorption | |
| CN111632435B (en) | Method for purifying waste gas containing liquid hazardous chemicals | |
| CN2330404Y (en) | Melamine-urea washing and gas-liquid separation combined equipment | |
| CN208727154U (en) | Dedusting, desulphurization and denitration integrated fume purification device | |
| CN218357962U (en) | High-efficiency gas-liquid separator for treating atmospheric pollution | |
| CN207102191U (en) | Denitrating flue gas preprocessor | |
| CN216825634U (en) | High-efficient dust removal defogging takes off white device after desulfurization | |
| CN109126453B (en) | Low-temperature denitration process | |
| RU2579084C2 (en) | Contact interaction between gas and fluid and device to this end |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C19 | Lapse of patent right due to non-payment of the annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |