CN205095757U - Reaction commodity circulation distributor and solid particle bed reactor - Google Patents
Reaction commodity circulation distributor and solid particle bed reactor Download PDFInfo
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- CN205095757U CN205095757U CN201520382278.XU CN201520382278U CN205095757U CN 205095757 U CN205095757 U CN 205095757U CN 201520382278 U CN201520382278 U CN 201520382278U CN 205095757 U CN205095757 U CN 205095757U
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Abstract
The utility model relates to a chemical industry equipment field discloses a reaction commodity circulation distributor and solid particle bed reactor, should react the commodity circulation distributor and include distributor main part (10), is equipped with reactant circulation passageway in this distributor main part, and be provided with in this distributor main part with the fluid entry and the fluid issuing of reactant circulation passageway intercommunication, being located of reactant circulation passageway fluid entry with at least partly between the fluid issuing forms to inhaling a class section (12), and fluid sunction inlet (11) on distributor main part (10), this fluid sunction inlet is in on the extending direction of reactant circulation passageway fluid entry with between the fluid issuing to can make to produce a negative pressure and produce pumping action to the liquid phase commodity circulation with inhaling class section intercommunication fluid sunction inlet department, thereby make the reaction commodity circulation distributor can be in fairly wide gas -liquid looks load range, improve the distributivity ability of solid particle bed reactor reliably.
Description
Technical field
The utility model relates to chemical industry equipment, particularly, relates to a kind of reactant fluidic distributor and solid particle bed reactor.
Background technology
At present, the catalytic reaction in chemical field adopts the reactor with solid particle bed to carry out mostly.Usually, this reactor (tower) is for the chemical reaction between gas phase materials and liquid phase materials.Particularly, gas-liquid two-phase material is assigned on catalyst solid particle layers through reactor distribution tray or the reactant fluidic distributor be arranged on reactor tower tray and chemical reaction occurs.
The uniformity that the mixing of gas and liquid two-phase and material distribute on catalyst solid particle layers becomes the key factor that impact reaction generates product quality.More evenly, temperature and the reaction speed of catalyst reactor solid particle bed then more easily control for gas phase and liquid phase reacting material mixed allocation ground.Therefore, in order to make gas and liquid two-phase mix better and be assigned to equably on catalyst solid particle layers, following prior art is had.
US3218249 discloses a kind of traditional distribution tray.Uniform some distributors be made up of downspout and bubble cap in this distribution tray.Circulation road in an annular is formed between bubble cap and downspout.Bubble cap is provided with strip fluting.When normally working, the liquid level on tower tray because gas phase action is lower than the liquid level in circulation road in annular, thus can form pressure drop difference in circulation road on the outside and annular of bubble cap.Gas phase is carried liquid phase and is folded to via central tube upper end downflow weir and flows into bottom, finally by by outlet flow bed downwards.The major defect of this distributor is by the fluid flow of each allocation units very responsive to the liquid level change on tower tray, and this is particularly evident under high gas phase loading condiction.In space in addition above distribution tray due to vapor liquid equilibrium effect mineralization pressure gradient, these are larger to the liquid phase flow effect of single distributor.
US4126540 discloses a kind of distributor.This distributor is formed primarily of overhead guard and downspout.Downspout lateral opening hole.Gas phase is flowed into by downspout upper end open, and liquid phase flows into downspout by lateral opening hole.The position of perforate to ensure that in material that granule foreign is deposited on tower tray can not block perforate.The shortcoming of this distribution plate is that perforate is highly single, and suitable liquid phase load range is less, and limit load is lower.
US5158714 discloses a kind of modified bubble cap distributor, mainly comprises bubble cap, downspout and connecting rod.The liquid phase local distributing uniformity of this distributor by adopting the interior inlay fluid diffuser of different reinforcement liquid dispersions to improve each export distributor, but due to the existence of interior inlay fluid diffuser, in downspout, the friction pressure loss of gas-liquid two-phase fluid increases, cause liquid phase flow increasing tower tray liquid level sensitiveness in single distributor, thus reduce integral dispensing uniformity to a certain extent.
US5942162 discloses a kind of gas stripping type distributor.The operation principle of this air lift distributor is identical with bubble cap distributor, and difference is that downspout size diminishes, by increasing dropping liquid point quantity on tower tray with the various combination form of bubble cap.This distributor exists equally and changes very sensitive issue to tower tray liquid level.
Visible, in the prior art, the fluid flow of various reactant fluidic distributor (such as bubble cap distributor etc.) is very responsive, particularly particularly evident under high gas phase loading condiction to the liquid level change on reactor tower tray.And operability is lower, the oil quality requirement of hydrogenation plant maximization and increasingly stringent can not be applicable to preferably.
Utility model content
Technical problem to be solved in the utility model is for providing a kind of reactant fluidic distributor, this reactant fluidic distributor reliably can carry out the mixing of gas and liquid two-phase after in reactor being installed to, and be not easy the impact of the liquid level be subject on reactor tower tray.
In order to solve the problems of the technologies described above, the utility model provides a kind of reactant fluidic distributor, this reactant fluidic distributor comprises main distributor, reactant circulation passage is provided with in this main distributor, and this main distributor is provided with the fluid intake and fluid issuing that are communicated with described reactant circulation passage, being formed as at least partially between described fluid intake and described fluid issuing of described reactant circulation passage inhales stream section, the passage section area change of this suction stream section and large in two, middle little of to form venturi conduit structure, and described main distributor is also provided with inhales with described the fluid intake flowing section and be communicated with, this fluid intake is between described fluid intake and described fluid issuing on the bearing of trend of described reactant circulation passage.
Preferably, described suction stream section is formed as the tubular passage that diameter gradually changes, and this suction stream section is reduced to minimum diameter D2 gradually by the first diameter D1, then expands Second bobbin diameter D3 gradually to by described minimum diameter D2; Preferably, described first diameter D1 is 1.2-2.4 times of described minimum diameter D2, and described first diameter D1 is equal with described Second bobbin diameter D3; More preferably, described first diameter D1 is 1.4-1.8 times of described minimum diameter D2.
Preferably, described suction stream section has the cylindrical channel section that internal diameter is described minimum diameter D2, and described fluid intake is arranged in described cylindrical channel section.
Preferably, described stream section of inhaling comprises the reducing diameter part that diameter is reduced to minimum diameter D2 by the first diameter D1 and the wide diameter portion expanded to described Second bobbin diameter D3 from described minimum diameter D2, described reducing diameter part and described wide diameter portion are all formed as truncated cone-shaped, and described fluid intake is arranged on described wide diameter portion; Preferably, described first diameter D1 is 30-260mm, and described fluid intake is the circular hole of diameter 4-30mm, and described reducing diameter part is provided with auxiliary fluid inlet; More preferably, described first diameter D1 is 120-200mm, described fluid intake is the circular hole of diameter 10-20mm, described auxiliary fluid inlet is rectangular aperture, the length of this rectangular aperture is 20-80mm, width is 3-12mm, and the length direction of this rectangular aperture is perpendicular to the central axis of described reactant circulation passage.
Preferably, described suction stream section is formed as the revolution shape that bus is circular arc line, and described fluid intake is arranged on described minimum diameter D2 place; Preferably, described fluid intake is 1-10 circular hole, and this Circularhole diameter is 4-40mm; More preferably, described circular hole is 2-8, and this Circularhole diameter is 12-26mm.
Preferably, described reactant circulation passage also comprises and is formed as columned fluid output, and the position corresponding to this fluid output of described main distributor is provided with the auxiliary fluid inlet be communicated with this fluid output; Preferably, described auxiliary fluid inlet is 1-8 rectangular aperture, and the length of this rectangular aperture is 10-100mm and length direction is bearing of trend along described fluid output; More preferably, described auxiliary fluid inlet is 2-6 rectangular aperture, and the length of this rectangular aperture is 20-60mm.
Preferably, described fluid issuing is arranged on the lower surface of described main distributor, this reactant fluidic distributor also comprises and to be arranged on below described main distributor and to aim at the base plate of described fluid issuing, and this base plate is configured in the position of 5-50mm below the lower surface apart from described main distributor; Be preferably 10-20mm.
Preferably, described base plate is the flat board or the corrugated sheet that are provided with through hole; Preferably, described base plate is circular slab, and the area of this circular slab is greater than the area of described fluid issuing, and described through hole is the circular port of diameter 4-16mm; More preferably, the diameter of described circular slab is 60-200mm.
Preferably, described fluid intake is arranged at the upper surface of described main distributor, this reactant fluidic distributor also comprises the top cap portion be arranged on described main distributor, this top cap portion comprises lamina tecti and occlusion part, described lamina tecti be arranged on described main distributor upper surface top and and be separated with preset distance between the upper surface of described main distributor with fluid intake described in cover cap, described occlusion part extends downwards from described lamina tecti and exceedes the upper surface of described main distributor downwards, and between the lateral surface of described occlusion part and described main distributor, there is interval, preferentially, described lamina tecti is circular slab, and the area of this circular slab is 1.96-9 times of the area of described fluid intake, and described occlusion part is tubular annular slab, and described preset distance is 10-80mm, more preferably, described preset distance is 15-40mm, and the area of this circular slab is 2.56-4.84 times of the area of described fluid intake.
Preferably, described fluid intake is arranged at the upper surface of described main distributor, this reactant fluidic distributor also comprises the top conducting element be arranged on described main distributor, this top conducting element is cover the top cap portion of described main distributor side at least partially or be installed to the top deflector of described main distributor upper surface by arranging bar, wherein, described top cap portion comprises lamina tecti, occlusion part and fixed part, described lamina tecti be arranged on described main distributor upper surface top and and be separated with preset distance between the upper surface of described main distributor with fluid intake described in cover cap, described fixed part abuts with the upper surface of described main distributor and fixes, described occlusion part extends downwards from described lamina tecti and exceedes the upper surface of described main distributor downwards, between the lateral surface of described occlusion part and described main distributor, there is interval, thus guiding channel is formed between described main distributor and described occlusion part, preferably, described lamina tecti is rectangular slab, the area of this rectangular slab is 1.44-4 times of the area of described fluid intake, and described occlusion part and described fixed part are be connected to the rectangular slab in the both side ends of described lamina tecti length direction, and described preset distance is 10-80mm, more preferably, described preset distance is 15-40mm, and the area of this rectangular slab is 1.69-2.25 times of the area of described fluid intake.
The utility model also provides a kind of solid particle bed reactor, this solid particle bed reactor comprises reactor wall, be connected to supporting disk on described reactor wall and tower tray, described tower tray is provided with the reactant fluidic distributor according to technique scheme; Preferably, the described main distributor of described reactant fluidic distributor is described main distributor from the 1.2-10 of the below length that the lower surface of described tower tray stretches out downwards doubly from the upper length that the upper surface of described tower tray protrudes upward; More preferably, when described tower tray being provided with reactant fluidic distributor according to above-mentioned portion of techniques scheme, described upper length is 2-4 times of described below length; When described tower tray being provided with reactant fluidic distributor according to above-mentioned portion of techniques scheme, described upper length is 3-8 times of described below length.
In addition, the utility model also provides a kind of solid particle bed reactor, this solid particle bed reactor comprises reactor wall, be connected to supporting disk on described reactor wall and tower tray, described tower tray is provided with the reactant fluidic distributor described in above-mentioned portion of techniques scheme, and reactant fluidic distributor described in each is arranged so that on described tower tray respective described guiding channel is positioned at the side back to described tower tray center of described reactant fluidic distributor; Preferably, the described main distributor of described reactant fluidic distributor is described main distributor from the 1.2-10 of the below length that the lower surface of described tower tray stretches out downwards doubly from the upper length that the upper surface of described tower tray protrudes upward; More preferably, when described tower tray being provided with the reactant fluidic distributor according to above-mentioned portion of techniques scheme, described upper length is 2-4 times of described below length, described first diameter D1 is 40-150mm, described minimum diameter D2 is 10-100mm, when described tower tray being provided with the reactant fluidic distributor according to above-mentioned portion of techniques scheme, described upper length is 3-8 times of described below length.
Preferably, described solid particle bed reactor is set to make when normal work the liquid level on described tower tray to be at least 10 times of described fluid intake diameter, and higher than fluid intake described at least one.
Pass through technique scheme, can make to produce negative pressure with this suction stream section communication of fluid suction inlet place and swabbing action is produced to liquid phase stream, thus make reactant fluidic distributor in quite wide liquid phase load range, can reliably improve the allocation performance of solid particle bed reactor.
Other features and advantages of the utility model are described in detail in detailed description of the invention part subsequently.
Accompanying drawing explanation
Accompanying drawing is used to provide further understanding of the present utility model, and forms a part for description, is used from explanation the utility model, but does not form restriction of the present utility model with detailed description of the invention one below.In the accompanying drawings:
Fig. 1 represents a kind of detailed description of the invention of reactant fluidic distributor described in the utility model.
Fig. 2 represents the another kind of detailed description of the invention of reactant fluidic distributor described in the utility model.
Fig. 3 represents a kind of detailed description of the invention of the solid particle bed reactor being provided with reactant fluidic distributor described in the utility model.
Fig. 4 is the A-A cross-sectional schematic of Fig. 3.
Fig. 5 is a kind of detailed description of the invention of reactant fluidic distributor described in the utility model.
Fig. 6 is a kind of detailed description of the invention of reactant fluidic distributor described in the utility model.
Fig. 7 is reactant fluidic distributor P described in the utility model and contrasts reactant fluidic distributor Q under different liquid phase load condition X, and reaction mass distributor is to the comparison schematic diagram of the sensitiveness Y that tower tray liquid level changes.
Fig. 8 is the experimental result schematic diagram utilizing reactant fluidic distributor structure in prior art.
Fig. 9 is the experimental result schematic diagram utilizing reactant fluidic distributor structure in the utility model technology.
Description of reference numerals
1 reactor wall 2 supporting disk
3 solid particle bed 4 tower trays
5 reactant fluidic distributor 10 main distributors
11 fluid intakes 12 inhale stream section
13 reducing diameter part 14 wide diameter portions
15 auxiliary fluid inlet 16 fluid output
17 cylindrical channel sections
20 top cap portion 21 lamina tectis
22 occlusion part 23 nuts
24 connecting rod 25 fixed parts
30 base plate 31 bottom plate holes
40 top deflectors 41 arrange bar
Detailed description of the invention
Below in conjunction with accompanying drawing, detailed description of the invention of the present utility model is described in detail.Should be understood that, detailed description of the invention described herein, only for instruction and explanation of the utility model, is not limited to the utility model.
In the utility model, when not doing contrary explanation, the noun of locality such as " upper and lower, left and right " of use typically refers to reference to upper and lower, left and right shown in the drawings; " inside and outside " refers to profile inside and outside relative to each parts itself.
As shown in Figure 1-2, the utility model provides a kind of reactant fluidic distributor, this reactant fluidic distributor comprises main distributor 10, reactant circulation passage is provided with in this main distributor 10, and this main distributor 10 is provided with the fluid intake and fluid issuing that are communicated with reactant circulation passage, being formed as at least partially between fluid intake and fluid issuing of reactant circulation passage inhales stream section 12, the passage section area change of this suction stream section 12 and large in two, middle little of to form venturi conduit structure, and main distributor 10 is also provided with and inhales the fluid intake 11 flowing section 12 and be communicated with, this fluid intake 11 is between fluid intake and fluid issuing on the bearing of trend of reactant circulation passage.
Because this suction stream section 12 is formed as venturi conduit structure, therefore, it is possible to make to produce negative pressure with this suction stream section 12 communication of fluid suction inlet 11 place to produce swabbing action to liquid phase stream.Inhale stream section 12 and can be formed as various shape, as long as it can the change of flow section can make to produce low pressure near swiftly flowing fluid, and form suction-operated.
Preferred suction flows the tubular passage that section 12 is formed as diameter change, and as shown in Figure 1, this suction stream section 12 is reduced to minimum diameter D2 gradually by the first diameter D1, then expands Second bobbin diameter D3 gradually to by described minimum diameter D2; Preferably, described first diameter D1 is 1.2-2.4 times of described minimum diameter D2, and described first diameter D1 is equal with described Second bobbin diameter D3; More preferably, described first diameter D1 is 1.4-1.8 times of described minimum diameter D2.As one preferred embodiment, as shown in Figure 5, inhale stream section 12 and there is the cylindrical channel section 17 that internal diameter is minimum diameter D2, and fluid intake 11 can be made to be arranged on this place, thus the total amount making fluid intake 11 and the suction stream section 12 with minimum diameter D2 be communicated with to make to produce liquid phase stream swabbing action maximizes.
Inhale stream section 12 can also be formed as shown in Figure 2, namely the reducing diameter part 13 that diameter is reduced to minimum diameter D2 by the first diameter D1 and the wide diameter portion 14 expanded from minimum diameter D2 to Second bobbin diameter D3 is comprised, reducing diameter part 13 and wide diameter portion 14 are all formed as truncated cone-shaped, and fluid intake 11 is arranged on wide diameter portion 14; Preferably, the first diameter D1 is 30-260mm, and fluid intake 11 is the circular hole of diameter 4-30mm, reducing diameter part 13 is provided with auxiliary fluid inlet 15; More preferably, first diameter D1 is 120-200mm, fluid intake 11 is the circular hole of diameter 10-20mm, auxiliary fluid inlet 15 is rectangular aperture, the length of this rectangular aperture is 20-80mm, width is 3-12mm, and the length direction of this rectangular aperture is perpendicular to the central axis of reactant circulation passage.
Particularly, this reducing diameter part 13 and wide diameter portion 14 can be formed as the cylindrical shell that sectional area constantly changes, such as taper, arc etc.
In addition, as one preferred embodiment, as shown in Figure 6, inhale stream section 12 and there is the cylindrical channel section 17 that internal diameter is minimum diameter D2, and fluid intake 11 can be made to be distributed on this place, thus the total amount making fluid intake 11 and the suction stream section 12 with minimum diameter D2 be communicated with to make to produce liquid phase stream swabbing action maximizes.Simultaneously, the wide diameter portion 14 that sectional area increases gradually is formed in Fig. 6, thus the liquid phase stream entering into main distributor 10 from tower tray 4 by swabbing action two can be mixed into gas-liquid logistics, and make this gas-liquid logistics with certain angular spread on the beds of below.
On the basis of technique scheme, inhale stream section 12 and be formed as the revolution shape that bus is circular arc line, fluid intake 11 is arranged on minimum diameter D2 place; Preferably, fluid intake 11 is 1-10 circular hole, and this Circularhole diameter is 4-40mm; More preferably, circular hole is 2-8, and this Circularhole diameter is 12-26mm.
In addition, as a kind of preferred embodiment of the present utility model, reactant circulation passage also comprises and is formed as columned fluid output 16, and the position corresponding to this fluid output 16 of main distributor 10 is provided with the auxiliary fluid inlet 15 be communicated with this fluid output 16; Preferably, auxiliary fluid inlet 15 is 1-8 rectangular aperture, and the length of this rectangular aperture is 10-100mm and length direction is bearing of trend along fluid output 16; More preferably, auxiliary fluid inlet 15 is 2-6 rectangular aperture, and the length of this rectangular aperture is 20-60mm.
These auxiliary fluid inlet 15 can for the gas phase that circulates under reactant fluidic distributor is in low liquid phase flow condition, and for circulating Partial Liquid Phase under reactant fluidic distributor is in high liquid phase flow condition, thus improve the operational load of reactant fluidic distributor.In addition, the size of above-mentioned auxiliary fluid inlet 15 can either be identical, also can be different.And the length direction of auxiliary fluid inlet 15 also can be set to other directions.
On the basis of technique scheme, described fluid issuing is arranged on the lower surface of described main distributor, this reactant fluidic distributor also comprises and to be arranged on below main distributor 10 and to aim at the base plate 30 of fluid issuing, and below the lower surface that this base plate 30 is configured in distance main distributor 10 position of 5-50mm; Be preferably 10-20mm.
Particularly, this base plate can be arranged on reactant fluidic distributor by connecting rod 24.Conflux adhewsive action and the part plume formed because of connecting rod 24 can either be avoided by this base plate 30, the allocation performance of gas-liquid two-phase logistics on beds can also be strengthened.
In addition, this base plate 30 is for being provided with flat board or the corrugated sheet of through hole; More preferably, base plate 30 is circular slab, and the area of this circular slab is greater than the area of fluid issuing, and through hole is the circular port of diameter 4-16mm; More preferably, the diameter of circular slab is 60-200mm.Particularly, the number of openings on this base plate 30 and size can set according to process conditions.
On the basis of technique scheme, fluid intake is arranged at the upper surface of main distributor 10, as shown in Figure 1, this reactant fluidic distributor also comprises the top cap portion 20 be arranged on main distributor 10, this top cap portion 20 comprises lamina tecti 21 and occlusion part 22, lamina tecti 21 be arranged on main distributor 10 upper surface top and and be separated with preset distance between the upper surface of main distributor 10 with cover cap fluid intake, occlusion part 22 extends downwards from lamina tecti 21 and exceedes the upper surface of main distributor 10 downwards, and between the lateral surface of occlusion part 22 and main distributor 10, there is interval, preferentially, lamina tecti 21 is circular slab, and the area of this circular slab is 1.96-9 times of the area of fluid intake, and occlusion part 22 is tubular annular slab, and preset distance is 10-80mm, more preferably, preset distance is 15-40mm, and the area of this circular slab is 2.56-4.84 times of the area of fluid intake.
On the basis of technique scheme, fluid intake is arranged at the upper surface of main distributor 10, as shown in Figure 2, this reactant fluidic distributor also comprises the top conducting element be arranged on main distributor 10, and this top conducting element is cover the top cap portion 20 of described main distributor 10 side at least partially or be installed to the top deflector 40 of described main distributor 10 upper surface by arranging bar 41.
As shown in Figure 6, this arrange bar 41 by welding or bolt be connected between top deflector 40 and main distributor 10.
Top cap portion 20 comprises lamina tecti 21, occlusion part 22 and fixed part 25, lamina tecti 21 be arranged on main distributor 10 upper surface top and and be separated with preset distance between the upper surface of main distributor 10 with cover cap fluid intake, fixed part 25 abuts with the upper surface of main distributor 10 and fixes, occlusion part 22 extends downwards from lamina tecti 21 and exceedes the upper surface of main distributor 10 downwards, between the lateral surface of occlusion part 22 and main distributor 10, there is interval, thus be formed with guiding channel between main distributor 10 and occlusion part 22; Preferably, lamina tecti 21 is rectangular slab, and the area of this rectangular slab is 1.44-4 times of the area of described fluid intake, and occlusion part 22 and fixed part 25 are for being connected to the rectangular slab in the both side ends of lamina tecti length direction, and preset distance is 10-80mm; More preferably, preset distance is 15-40mm, and the area of this rectangular slab is 1.69-2.25 times of the area of fluid intake.
The utility model also provides a kind of solid particle bed reactor, and this solid particle bed reactor comprises reactor wall 1, be connected to supporting disk 2 on reactor wall 1 and tower tray 4, tower tray 4 is provided with reactant fluidic distributor 5 according to technique scheme; Preferably, the main distributor 10 of reactant fluidic distributor 5 is main distributor 10 from the 1.2-10 of the below length that the lower surface of tower tray 4 stretches out downwards doubly from the upper length that the upper surface of tower tray 4 protrudes upward; More preferably, when tower tray 4 being provided with reactant fluidic distributor 5 described shown in Fig. 1, described upper length is 2-4 times of described below length; When tower tray 4 being provided with reactant fluidic distributor 5 according to Fig. 2, upper length is 3-8 times of below length.
In addition, the utility model is a kind of solid particle bed reactor also, this solid particle bed reactor comprises reactor wall 1, be connected to supporting disk 2 on reactor wall 1 and tower tray 4, tower tray 4 is provided with reactant fluidic distributor 5 described in technique scheme, and each reactant fluidic distributor 5 is arranged so that on tower tray 4 respective guiding channel is positioned at the side back to tower tray 4 center of reactant fluidic distributor 5.
In addition, as another preferred embodiment, the main distributor 10 of reactant fluidic distributor 5 is main distributor 10 from the 1.2-10 of the below length that the lower surface of tower tray 4 stretches out downwards doubly from the upper length that the upper surface of tower tray 4 protrudes upward.
More preferably, when tower tray 4 being provided with according to technique scheme reactant fluidic distributor 5, upper length is 2-4 times of below length, first diameter D1 is 40-150mm, minimum diameter D2 is 10-100mm, in addition, also can make when tower tray 4 being provided with reactant fluidic distributor 5, upper length is 3-8 times of below length.
Understand the utility model better for the ease of the public, be described below in conjunction with the situation of reactant fluidic distributor described in the utility model when using state.
Because main distributor 10 inhales stream section 12, therefore, it is possible to utilize this suction stream section 12 main distributor 10 to be divided into the straight tube on top or the increaser of reducing pipe and bottom with passage section area change.
Restricted flow can be made when the flow section by reducing by this suction stream section 12, there is the phenomenon that flow velocity or flow increase in fluid, its flow and flow section are inversely proportional to.And known the reduction of increase with fluid pressure of flow velocity by bernoulli law, namely common venturi phenomenon.Generally, this effect refers to and can produce low pressure near swiftly flowing fluid, thus produces suction-operated.And in the utility model, inventor have passed through repetition test, obtain aforesaid preferred setting data.
In addition, by arranging auxiliary fluid inlet 15 on main distributor 10 top can be used in the fluid circulation when liquid phase flow is excessive.Particularly, this assist openings 15 can be rectangle, triangle, circle, the various shape such as trapezoidal.
Further, flow into when running up to fluid intake in main distributor 10 so that the liquid phase on tower tray 4 can be made by arranging fluid intake 11 in main distributor 10 bottom.Fluid intake 11 is arranged on differing heights for multiple.And the total open area of above-mentioned fluid intake 11, open amount and size etc. can according to decisions such as liquid phase flow and its physical propertys.In the utility model, inventor have passed through repetition test, obtains aforesaid preferred setting data.
When this reactant fluidic distributor normally works, gas phase is by the auxiliary fluid inlet 15 on main distributor 10 top and the fluid intake inflow pipe at top, when on tower tray 4, liquid level starts to run up to certain altitude, liquid phase begins through fluid intake 11 and flow in main distributor 10.Gas phase is that liquid phase flows out with the fluid issuing of dispersed from main distributor 10 by downward shearing and rubbing action.
When liquid phase flow increases further, liquid level on tower tray 4 increases further, owing to inhaling the effect of stream section 12, namely when the minimum diameter D2 of this suction stream section 12 and the first diameter D1 meets certain condition, minimum diameter D2 place pressure will be less than main distributor 10 external pressure, now, the liquid on tower tray 4 will be sucked the minimum diameter D2 place being sent to main distributor 10, gas phase and liquid phase occur mixing and and flow to flow out from fluid issuing.
The lower end of main distributor 10 is positioned at the below of tower tray 4, and the distance between the fluid issuing of lower end and tower tray 4 is within certain limit.As too small in the distance between the fluid issuing of lower end and tower tray 4, the liquid phase fluid then flowed out from the fluid issuing of lower end is easy to be attached to the bottom of tower tray 4 due to tension force effect and assemble brokenly, and causes fluid distribution uniformity on beds cross section to decline.As excessive in the distance between the fluid issuing of lower end and tower tray 4, the liquid phase fluid then flowed out from the fluid issuing of lower end needs larger spacing mutual to make up distributional effects to adjust after outflow, and cause the minimizing of beds loadings or reactor manufacture highly to increase, and then improve operating cost.In the utility model, inventor have passed through repetition test, obtains aforesaid preferred setting data.
Further, in utility model, the shape being arranged on the top cap portion 20 on main distributor 10 can be reverse U shape or J-shaped, and particularly, can be formed by lamina tecti 21 and occlusion part 22, wherein lamina tecti 21 also can be circular slab or rectangular slab.Meanwhile, diameter or the length of the fluid intake at main distributor 10 top is greater than by the diameter or length making this lamina tecti 21, with the coverage making the fluid intake of main distributor 10 be positioned at lamina tecti 21.
Meanwhile, be formed with side (annular) gap from lamina tecti 21 between the occlusion part 22 of downward-extension and main distributor 10, this side clearance is preferably the 1/8-1/2 of main distributor 10 diameter, is preferably 1/4-1/3.And the gap between the end face of lamina tecti 21 and distribution body 10 is the 1/8-2/3 of occlusion part 22 length, be preferably 1/4-1/2.And the length of occlusion part 22 is the 1/10-1/2 of main distributor 10 length, be preferably 1/5-2/5.
Further, in utility model, the base plate 30 be arranged on below main distributor 10 can be the various shapes such as dull and stereotyped or corrugated sheet.Base plate 30 can be provided with the multiple bottom plate holes 31 such as circle, triangle, rectangle simultaneously.The magnitude setting of this bottom plate hole 31 and size etc. can set according to process conditions, and its layout type can be equilateral triangle, square, circular etc. multiple.Utilize this base plate 30 and the liquid phase liquid collision flowed out from the fluid issuing below main distributor, and by above-mentioned bottom plate hole 31, logistics disperseed further and be evenly distributed to underlying catalyst solid particle bed.
Known by foregoing description, the utility model passes through said structure, make reactant fluidic distributor can in quite wide liquid phase load range, all can the uniformity of liquid phase flow velocity in the liquid level of single reactant fluidic distributor and main distributor 10 at utmost low maintenance tower tray 4, reliably improve the allocation performance of solid particle bed reactor.Meanwhile, it is simple that the utility model also has structure, feature easy for installation.While not only can improving beds flow distribution significantly, less pressure drop can also be had, thus be specially adapted to the flow distribution in solid particle bed reactor.
About reactant fluidic distributor, the utility model provides multiple combination scheme.Meanwhile, inventor provides following 2 preferred embodiments.
Embodiment 1 (as shown in Figure 1)
In the preferred embodiment, reactant fluidic distributor comprises: be formed as the top cap portion 20 of reverse U shape, include the main distributor 10 of the suction stream section 12 being formed as segmental arc (bus is the revolution shape of circular arc line) and the fluid output 16 being formed as vertical section (cylindric), the corrugated base plate 30 be connected to by connecting rod 24 on main distributor 10.
Particularly, top cap portion 20 comprises the lamina tecti 21 as horizontal segment being formed as circular flat board, this lamina tecti 21 is provided with the circular hole for penetrating connecting rod 24, this lamina tecti 21 is connected by the upper end of nut with connecting rod 24, thus be fixedly attached on connecting rod 24 by support, wherein this connecting rod 24 can be connected on the madial wall of main distributor 10 by spoke etc.This circular slab length is 1.4-3 times of fluid inlet diameter, is preferably 1.6-2.2 doubly.
Suction stream section 12 in main distributor 10 is provided with a row or multi-row circular open as fluid intake 11.These circular holes major part under low liquid phase flow condition is used for liquid communication, part is used for gas phase circulation, and under high liquid phase flow condition, this suction stream section 12 is submerged in the accumulation liquid phase on tower tray 4, all circular holes are all for liquid communication, and preferably this Circularhole diameter is 6-40mm.In addition, when circular hole is multiple, these circular holes are distributed in the both sides of minimum diameter D2 as far as possible symmetrically, to realize larger swabbing action.
Distance between base plate 30 and main distributor 10 is preferably 10-30mm, thus can either avoid conflux adhewsive action and the part plume formed because of connecting rod 24, can also strengthen the allocation performance of gas-liquid two-phase logistics on underlying catalyst bed.
When being arranged in solid particle bed reactor by the reactant fluidic distributor in embodiment 1, its concrete arrangement can adopt various ways.Affect the reduction of logistics integral dispensing in order to ensure eliminating because gas-liquid logistics makes to be attached to tower tray 4 lower surface because of the reason such as viscous force, surface tension when the fluid issuing of main distributor 10 flows out, need to make the distance c between the fluid issuing of main distributor 10 and tower tray lower end plane be in a more than minimum.Meanwhile, in order to mate suitable spray angle, within distance c should be in maximum.Wherein, spacing between this spray angle with reactant fluidic distributor is relevant, should, under the prerequisite meeting tower tray cross section distributing uniformity, adopt less spacing to arrange, thus maximize beds loadings and the plant investment minimizing solid particle bed reactor.
Embodiment 2 (as shown in Figure 2)
In the preferred embodiment, reactant fluidic distributor comprises: be formed as J-shaped top cap portion 20, include the suction stream section 12 that formed by reducing diameter part 13 and wide diameter portion 14 as main distributor 10, the horizontal base plate 30 be connected to by connecting rod 24 on main distributor 10.
Particularly, push up cap portion 20 and comprise the lamina tecti 21 as horizontal segment being formed as rectangular flat, the longer shielding part 22 being formed as rectangular flat and the shorter fixed part being formed as rectangular flat.Wherein, shorter rectangular flat is welded in the top of main distributor 10, is formed with gap between longer rectangular flat and main distributor.
In the present embodiment, although top cap portion 20 by shorter rectangular flat and be supported on main distributor 10, also can utilize the mode identical with embodiment simultaneously, this reinforcement between the two fixing.The rectangular flat length of preferred levels section is 1.2-2 times of fluid inlet diameter, is preferably 1.3-1.5 doubly.
In main distributor 10, reducing diameter part 13 is provided with auxiliary fluid inlet 15, this auxiliary three-dimensional entrance level is offered.The size of the auxiliary fluid inlet that these levels are offered can be identical or different.It is readily understood that reducing diameter part 13 is formed as the round platform cylinder wide at the top and narrow at the bottom that hull shape one-tenth is taken out at center, meanwhile, the top end opening of reducing diameter part 13 is as fluid intake, and wide diameter portion 14 is formed as the up-narrow and down-wide round platform cylinder that hull shape one-tenth is taken out at center.In the present embodiment, reducing diameter part 13 is all positioned on tower tray 4 plane; Wide diameter portion 14 part is positioned on tower tray 4, and part is positioned under tower tray 4, and ratio is between the two 1.5-10, is preferably 3-8.About other features all with embodiment 1 in similar.
About solid particle bed reactor, the utility model is formed as shape shown in embodiment 2 for top cap portion 20, and reactant fluidic distributor provides a kind of new layout type, as shown in Figure 3-4.
Diameter 2000-5000mm, be highly 8000-30000mm hydrocarbons hydrogenation reactor in, be provided with 3-10 section catalyst solid particle layers 3, solid particle bed 3 is positioned at above supporting disk 2, one or several tower tray 4 is installed between solid particle bed 3, this tower tray 4 is connected with reactor wall 1 by the fixed form such as fillet welding frame, bracing ring common in the art, and support tower tray 2 generally comprises grid, porous plate etc. and can be used in liquid communication and stop the porous material element that catalyst passes through.Solid particle bed 3 is made up of protective agent, desulphurization and denitrification catalyst etc. usually.
The layout density of reactant fluidic distributor 20 on tower tray 4 be often 4-50/square metre, layout type can be the modes such as equilateral triangle, square, circumference uniform distribution.Such as when layout is equilateral triangle, distributor interval S is generally 60-300mm.Because the top cap portion 20 in reactant fluidic distributor 20 is formed as J-shaped, therefore, the Way out that occlusion part 22 in reactant fluidic distributor 20 is formed is expressed as the direction indicated by black triangle in the diagram, that is, along the direction that reactant fluidic distributor 20 and tower tray 4 line of centres are outside.
Particularly, main distributor 10 diameter is 40-150mm, and above tower tray, main distributor 10 length is 100-200mm, and below tower tray, main distributor 10 length is 10-50mm.Main distributor 10 reducing diameter part 13 is provided with auxiliary fluid inlet 15, and its width is at 3-12mm, and length is 20-80mm.Main distributor 10 minimum diameter place diameter is 10-100mm.Lamina tecti is positioned at 10-80mm position above main distributor 10, the liquid flowed down by top beds can be avoided to flow directly in pipe and cause bias current, carries liquid phase circulation simultaneously provide annular space passage for gas phase on tower tray.
Because the component of liquid phase mass flow and two-phase determines fluid intake 11 quantity, size and position, when normally working, on tower tray 4, liquid level is at least 10 times of fluid intake 11 diameter, should be positioned on minimum rows of openings level height, fluid intake 11 spacing should be not less than 2 times of fluid intake diameter.Base plate 30 is a circular flat board, and its diameter is greater than the fluid outlet diameter of main distributor 10, is generally 60-200mm.Base plate 30 is provided with Homogeneous Circular perforate, and diameter is 4-16mm.The position of these perforates and layout are optimized according to the actual size of downspout, flow to distributing uniformity on underlying catalyst bed to further enhance gas-liquid two-phase logistics.
The distributivity of reactant fluidic distributor described in the utility model can be investigated by cold model test.The following describes by testing on the cold model test device of diameter 500mm, when investigation utilizes embodiment described in the utility model, to the improvement situation of fluid distribution uniformity, the cross section of tower tray 4 is divided into the identical measurement of fluid flow district of 12 pieces of areas, is characterized the performance quality of reactant fluidic distributor by the fluid flow difference measured in different subregion.Its result can from Fig. 8 and Fig. 9 relatively draw: compared with prior art, the flow deviation of the utility model in each measurement of fluid flow district is in more among a small circle, this illustrate the utility model there is better fluid distribution uniformity.
In addition, in the figure 7, X-axis is different liquid phase load (liquid level on tower tray), Y-axis is sensitiveness, P line represents that the sensitivity curves that the distributor of reaction mass shown in the utility model changes tower tray liquid level, Q line represent the sensitivity curves that contrast reaction mass distributor changes tower tray liquid level.Visible, no matter how liquid level changes, adopt reaction mass distributor described in the utility model all can reduce the sensitiveness changed tower tray liquid level, thus make reactant fluidic distributor in quite wide liquid phase load range, can reliably improve the allocation performance of solid particle bed reactor.
Below preferred embodiment of the present utility model is described by reference to the accompanying drawings in detail; but; the utility model is not limited to the detail in above-mentioned embodiment; within the scope of technical conceive of the present utility model; can carry out multiple simple variant to the technical solution of the utility model, these simple variant all belong to protection domain of the present utility model.
It should be noted that in addition, each concrete technical characteristic described in above-mentioned detailed description of the invention, in reconcilable situation, can be combined by any suitable mode, in order to avoid unnecessary repetition, the utility model illustrates no longer separately to various possible combination.
In addition, also can be combined between various different embodiment of the present utility model, as long as it is without prejudice to thought of the present utility model, it should be considered as content disclosed in the utility model equally.
Claims (34)
1. a reactant fluidic distributor, this reactant fluidic distributor comprises main distributor (10), this main distributor is provided with reactant circulation passage in (10), and this main distributor (10) is provided with the fluid intake and fluid issuing that are communicated with described reactant circulation passage, it is characterized in that, being formed as at least partially between described fluid intake and described fluid issuing of described reactant circulation passage inhales stream section (12), the passage section area change of this suction stream section (12) and large in two, middle little of to form venturi conduit structure, and described main distributor (10) is also provided with inhales with described the fluid intake (11) flowing section (12) and be communicated with, this fluid intake (11) is between described fluid intake and described fluid issuing on the bearing of trend of described reactant circulation passage.
2. reactant fluidic distributor according to claim 1, it is characterized in that, described suction flows the pipe passageway that section (12) is formed as diameter change, this suction stream section (12) is reduced to minimum diameter D2 gradually by the first diameter D1, then expands Second bobbin diameter D3 gradually to by described minimum diameter D2.
3. reactant fluidic distributor according to claim 2, is characterized in that, described first diameter D1 is 1.2-2.4 times of described minimum diameter D2, and described first diameter D1 is equal with described Second bobbin diameter D3.
4. reactant fluidic distributor according to claim 3, is characterized in that, described first diameter D1 is 1.4-1.8 times of described minimum diameter D2.
5. reactant fluidic distributor according to claim 2, it is characterized in that, described suction stream section (12) has the cylindrical channel section (17) that internal diameter is described minimum diameter D2, and described fluid intake (11) is arranged on described cylindrical channel section (17).
6. reactant fluidic distributor according to claim 2, it is characterized in that, described suction stream section (12) comprises the reducing diameter part (13) that diameter is reduced to minimum diameter D2 by the first diameter D1 and the wide diameter portion (14) expanded from described minimum diameter D2 to described Second bobbin diameter D3, described reducing diameter part (13) and described wide diameter portion (14) are all formed as truncated cone-shaped, and described fluid intake (11) is arranged on described wide diameter portion (14).
7. reactant fluidic distributor according to claim 6, it is characterized in that, described first diameter D1 is 30-260mm, and the circular hole that described fluid intake (11) is diameter 4-30mm described reducing diameter part (13) is provided with auxiliary fluid inlet (15).
8. reactant fluidic distributor according to claim 7, it is characterized in that, described first diameter D1 is 120-200mm, the circular hole that described fluid intake (11) is diameter 10-20mm, described auxiliary fluid inlet (15) is rectangular aperture, the length of this rectangular aperture is 20-80mm, and width is 3-12mm, and the length direction of this rectangular aperture is perpendicular to the central axis of described reactant circulation passage.
9. reactant fluidic distributor according to claim 2, is characterized in that, described suction stream section (12) is formed as the revolution shape that bus is circular arc line, and described fluid intake (11) is arranged on described minimum diameter D2 place.
10. reactant fluidic distributor according to claim 9, is characterized in that, described fluid intake (11) for 1-10 circular hole, this Circularhole diameter be 4-40mm.
11. reactant fluidic distributors according to claim 10, is characterized in that, described circular hole is 2-8, and this Circularhole diameter is 12-26mm.
12. reactant fluidic distributors according to claim 9, it is characterized in that, described reactant circulation passage also comprises and is formed as columned fluid output (16), and the position corresponding to this fluid output (16) of described main distributor (10) is provided with the auxiliary fluid inlet (15) be communicated with this fluid output (16).
13. reactant fluidic distributors according to claim 12, it is characterized in that, described auxiliary fluid inlet (15) is 1-8 rectangular aperture, and the length of this rectangular aperture is 10-100mm and length direction is bearing of trend along described fluid output (16).
14. reactant fluidic distributors according to claim 13, is characterized in that, described auxiliary fluid inlet (15) is 2-6 rectangular aperture, and the length of this rectangular aperture is 20-60mm.
15. reactant fluidic distributors according to claim 1, it is characterized in that, described fluid issuing is arranged on the lower surface of described main distributor, this reactant fluidic distributor also comprises and is arranged on described main distributor (10) below and aims at the base plate (30) of described fluid issuing, and this base plate (30) is configured in the position of 5-50mm below the lower surface apart from described main distributor (10).
16. reactant fluidic distributors according to claim 15, is characterized in that, described base plate (30) is configured in the position of 10-20mm below the lower surface apart from described main distributor (10).
17. reactant fluidic distributors according to claim 15, is characterized in that, described base plate (30) is for being provided with flat board or the corrugated sheet of through hole.
18. reactant fluidic distributors according to claim 17, it is characterized in that, described base plate (30) is circular slab, the area of this circular slab is greater than the area of described fluid issuing, and described through hole is the circular port of diameter 4-16mm.
19. reactant fluidic distributors according to claim 18, is characterized in that, the diameter of described circular slab is 60-200mm.
20. according to the reactant fluidic distributor in claim 1-17 described in any one, it is characterized in that, described fluid intake is arranged at the upper surface of described main distributor (10), this reactant fluidic distributor also comprises the top conducting element be arranged on described main distributor (10), this top conducting element is cover the top cap portion (20) of described main distributor (10) side at least partially or be installed to the top deflector (40) of described main distributor (10) upper surface by arranging bar (41)
Wherein, described top cap portion (20) comprises lamina tecti (21) and occlusion part (22), described lamina tecti (21) be arranged on described main distributor (10) upper surface top and and be separated with preset distance with fluid intake described in cover cap between the upper surface of described main distributor (10), described occlusion part (22) extends downwards from described lamina tecti (21) and exceedes the upper surface of described main distributor (10) downwards, and has interval between the lateral surface of described occlusion part (22) and described main distributor (10).
21. reactant fluidic distributors according to claim 20, it is characterized in that, described lamina tecti (21) is circular slab, the area of this circular slab is 1.96-9 times of the area of described fluid intake, described occlusion part (22) is tubular annular slab, and described preset distance is 10-80mm.
22. reactant fluidic distributors according to claim 21, is characterized in that, described preset distance is 15-40mm, and the area of this circular slab is 2.56-4.84 times of the area of described fluid intake.
23. according to the reactant fluidic distributor in claim 1-19 described in any one, it is characterized in that, described fluid intake is arranged at the upper surface of described main distributor (10), this reactant fluidic distributor also comprises the top cap portion (20) be arranged on described main distributor (10), this top cap portion (20) comprises lamina tecti (21), occlusion part (22) and fixed part (25), described lamina tecti (21) be arranged on described main distributor (10) upper surface top and and be separated with preset distance with fluid intake described in cover cap between the upper surface of described main distributor (10), described fixed part (25) abuts with the upper surface of described main distributor (10) and fixes, described occlusion part (22) extends downwards from described lamina tecti (21) and exceedes the upper surface of described main distributor (10) downwards, between the lateral surface of described occlusion part (22) and described main distributor (10), there is interval, thus guiding channel is formed between described main distributor (10) and described occlusion part (22).
24. reactant fluidic distributors according to claim 23, it is characterized in that, described lamina tecti (21) is rectangular slab, the area of this rectangular slab is 1.44-4 times of the area of described fluid intake, described occlusion part (22) and described fixed part (25) are for being connected to the rectangular slab in the both side ends of described lamina tecti length direction, and described preset distance is 10-80mm.
25. reactant fluidic distributors according to claim 24, is characterized in that, described preset distance is 15-40mm, and the area of this rectangular slab is 1.69-2.25 times of the area of described fluid intake.
26. 1 kinds of solid particle bed reactors, this solid particle bed reactor comprises reactor wall (1), be connected to supporting disk (2) on described reactor wall (1) and tower tray (4), it is characterized in that, described tower tray (4) is provided with according to the reactant fluidic distributor (5) in claim 1-20 described in any one.
27. solid particle bed reactors according to claim 26, it is characterized in that, the described main distributor (10) of described reactant fluidic distributor (5) is 1.2-10 times of the below length that described main distributor (10) stretches out downwards from the lower surface of described tower tray (4) from the upper length that the upper surface of described tower tray (4) protrudes upward.
28. solid particle bed reactors according to claim 27, it is characterized in that, described tower tray (4) is provided with according to claim 6 reactant fluidic distributor (5) time, described upper length be the 2-4 of described below length doubly.
29. solid particle bed reactors according to claim 27, it is characterized in that, when described tower tray (4) being provided with according to claim 9 or 12 reactant fluidic distributor (5), described upper length is 3-8 times of described below length.
30. solid particle bed reactors according to claim 26, it is characterized in that, described solid particle bed reactor is set to make when normal work the liquid level on described tower tray (4) to be at least 10 times of described fluid intake (11) diameter, and higher than fluid intake described at least one (11).
31. 1 kinds of solid particle bed reactors, this solid particle bed reactor comprises reactor wall (1), be connected to supporting disk (2) on described reactor wall (1) and tower tray (4), it is characterized in that, described tower tray (4) is provided with reactant fluidic distributor (5) according to claim 23, and reactant fluidic distributor (5) described in each is arranged so that on described tower tray (4) respective described guiding channel is positioned at the side back to described tower tray (4) center of described reactant fluidic distributor (5).
32. solid particle bed reactors according to claim 31, it is characterized in that, the described main distributor (10) of described reactant fluidic distributor (5) is 1.2-10 times of the below length that described main distributor (10) stretches out downwards from the lower surface of described tower tray (4) from the upper length that the upper surface of described tower tray (4) protrudes upward.
33. solid particle bed reactors according to claim 32, it is characterized in that, described tower tray (4) is provided with according to when quoting reactant fluidic distributor (5) according to claim 23 of claim 8, described upper length is 2-4 times of described below length, described first diameter D1 is 40-150mm, described minimum diameter D2 is 10-100mm, described tower tray (4) is provided with according to when quoting reactant fluidic distributor (5) according to claim 23 of claim 11 or 14, described upper length be the 3-8 of described below length doubly.
34. solid particle bed reactors according to claim 31, it is characterized in that, described solid particle bed reactor is set to make when normal work the liquid level on described tower tray (4) to be at least 10 times of described fluid intake (11) diameter, and higher than fluid intake described at least one (11).
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| CN201520382278.XU CN205095757U (en) | 2015-06-05 | 2015-06-05 | Reaction commodity circulation distributor and solid particle bed reactor |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN106281724A (en) * | 2016-08-29 | 2017-01-04 | 繁昌县健文电子商务有限公司 | A kind of material multi mixed reactor |
| CN108339673A (en) * | 2018-02-10 | 2018-07-31 | 太原理工大学 | A kind of cavitation jet flotation bubble generator and flotation unit |
| CN109647289A (en) * | 2019-01-16 | 2019-04-19 | 华陆工程科技有限责任公司 | A kind of iris type vinyl ethers product reactor |
| CN112546967A (en) * | 2020-11-16 | 2021-03-26 | 中国科学院过程工程研究所 | Downcomer and suction type, overflow type and mixed type gas-liquid distributor |
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2015
- 2015-06-05 CN CN201520382278.XU patent/CN205095757U/en active Active
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106281724A (en) * | 2016-08-29 | 2017-01-04 | 繁昌县健文电子商务有限公司 | A kind of material multi mixed reactor |
| CN106281724B (en) * | 2016-08-29 | 2019-11-29 | 繁昌县健文电子商务有限公司 | A kind of material multi mixed reactor |
| CN108339673A (en) * | 2018-02-10 | 2018-07-31 | 太原理工大学 | A kind of cavitation jet flotation bubble generator and flotation unit |
| CN108339673B (en) * | 2018-02-10 | 2023-11-21 | 内蒙古科灵时代矿业技术有限公司 | Cavitation jet flow flotation bubble generator and flotation device |
| CN109647289A (en) * | 2019-01-16 | 2019-04-19 | 华陆工程科技有限责任公司 | A kind of iris type vinyl ethers product reactor |
| CN112546967A (en) * | 2020-11-16 | 2021-03-26 | 中国科学院过程工程研究所 | Downcomer and suction type, overflow type and mixed type gas-liquid distributor |
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