CN100406112C - Liquid film colliding type jet reactor - Google Patents
Liquid film colliding type jet reactor Download PDFInfo
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- CN100406112C CN100406112C CNB2006100072378A CN200610007237A CN100406112C CN 100406112 C CN100406112 C CN 100406112C CN B2006100072378 A CNB2006100072378 A CN B2006100072378A CN 200610007237 A CN200610007237 A CN 200610007237A CN 100406112 C CN100406112 C CN 100406112C
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Abstract
The present invention relates to a liquid film colliding type jet reactor which comprises the following components: feed ports (1a and 1b), a central shaft (2), an internal ring pipe (3), a middle ring pipe (4), and a mixed head (8), wherein the central shaft (2), the internal ring pipe (3), and the middle ring pipe (4) are coaxially arranged from inside to outside; the mixed head (8) is connected with the lower end of the central shaft (2); an internal ring gap is formed between the lower end of the internal ring pipe and the central shaft, and a middle ring gap is formed between the lower end of the middle ring pipe and the lower end of the internal ring pipe. The reactor can realize the rapid mixing and the rapid reaction of liquid, and the yield and the quality of purpose products are increased.
Description
Technical field
The present invention relates to rapid mixing, rapid-action injection reactor between a kind of realization liquid, more particularly, is a kind of liquid film colliding type liquid rapid mixing injection reactor.
Background technology
In some chemical process, when complicated fast and parallel competitive reaction taking place between liquid phase or contacting competitive reaction fast, product or intermediate product and raw material component may further react; The CONCENTRATION DISTRIBUTION situation of degree that these reactions are carried out and various materials has direct relation.So the initial mixing effect between the liquid material can influence greatly that final product distributes, the yield and the quality of purpose product, and influence indexs such as the design of all round process and energy consumption simultaneously.When for example adopting phosgenation processes to produce isocyanates (MDI or TDI), this course of reaction mainly comprises cold light gasifying stage and hot phosgenation stage.At the cold light gasifying stage, the polyamines photoreactive gas is dissolved in respectively in the atent solvent, for example chlorobenzene, dichloro-benzenes, toluene, chlorinated naphthalene, 1,2,4-trichloro-benzenes etc., and they are reacted under 0～70 ℃ low temperature.In this stage, mainly generate the hydrochloride of acid amides and polyamines, and a spot of carbamide compounds.Key reaction is as follows:
RNH
2+COCl
2→RNHCOCl+HCl (1)
RNH
2+HCl→RNH
2·HCl (2)
RNH
2+RNHCOCl→RNCO+RNH
2·HCl (3)
RNH
2+RNCO→RNHCONHR (4)
In the cold stage of reaction, polyamines at first reacts with phosgene (1), generates carbamyl chloride, and this is a quick exothermic reaction, is reflected at moment to finish; Simultaneously, HCl and polyamines generation fast reaction (2) that reaction (1) produces generate the polyamines hydrochloride.Carbamyl chloride and polyamines hydrochloride all are the solid matters that is insoluble to reaction system.When the local mixed effect of phosgene and polyamines is relatively poor, local excessive polyamines will react (3) and (4) with carbamyl chloride or isocyanates in the solution, generation accessory substance urea, and urea is the thick material that is not dissolved in reaction system.This process is complicated multistep series connection competitive reaction.Main reaction is the moment reaction, and the time scale of its reaction is at Millisecond or following; The product that generates further with raw material generation fast reaction, generate the accessory substance of the system that is not dissolved in.Therefore, the initial mixing effect of two kinds of raw materials will directly influence the yield and the selectivity of principal product.Successfully design quick liquid reactant mixture device, improve the initial mixing effect of two strands of feed streams, for the yield and the selectivity that increase principal product, the generation that reduces the thick material of by-product has great importance.
It is a kind of important method that realizes rapid mixing between liquid that two strands of (or multiply) liquid are clashed in some way fast.By with quick flowing liquid fierce bump of moment, realize the quick dissipation of energy; Simultaneously, can in the segregation degree that reduces rapidly on the less space scale between the fluid, reach the purpose of rapid mixing by reducing the preceding space scale of fluid contact.
BP GB1238669 discloses a kind of reactor (as Fig. 1) that is used to produce isocyanates, and wherein the thin liquid layer that forms after by two narrow runners of two fluid streams is realized the rapid mixing between the material whereby with certain angle bump fast mutually.
U.S. Pat 3507626 discloses a kind of venturi reactor that is used to produce isocyanates, and runner is designed to the Venturi tube form, utilizes undergauge to increase the flowing velocity of two fluid streams.This blender is formed (as shown in Figure 2) by two coaxial Venturi tubes, wherein first fluid streams flows between the slit that inside and outside Venturi tube forms, second fluid streams flows from the Venturi tube of the inside, Venturi tube undergauge place in inside, second fluid streams is mixed with the collision of first fluid streams after slit or the outflow of equally distributed aperture, realizes the rapid mixing between the material.
Fluid space yardstick before U.S. Pat 4735359 described reactors will mix further reduces, it is sheet liquid film about 100 microns that two fluid streams are formed thickness after by two highly pressurised liquid nozzles, and two liquid films clash into mutually, mix in the mixed zone.
By above analysis as can be seen, clash into mutually, can realize the rapid mixing between the liquid material to a certain extent by making liquid film or thin liquid layer.But, because the competitive reaction system generally requires the incorporation time yardstick between the material to reach Millisecond even lower fast, therefore, need the more efficiently Fast Mixing Equipment of exploitation, to guarantee the carrying out of main reaction, inhibition side reaction as far as possible.Meanwhile, also need to create suitable condition, reduce the back-mixing degree of mixing liquid film as far as possible, and its form with similar laminar flow is flowed for follow-up course of reaction.
Summary of the invention
The object of the present invention is to provide a kind of novel liquid film colliding type jet reactor,, improve the yield and the quality of purpose product to strengthen main reaction, to suppress side reaction.
Reactor provided by the present invention is based on following design concept: making the material more than two strands or two strands is several millimeters annulus, liquid film bump, rapid mixing, reaction mutually in the first hybrid reaction district of formation by thickness respectively; Proceed in the second hybrid reaction district in the uncompleted mixing in the first hybrid reaction district, course of reaction; The second hybrid reaction district is a mixing head surface of expanding gradually, by mixing head being designed to the cambered surface form of flaring, for example conical butt, the cambered surface taper of protruding side, the taper of concave side cambered surface or side are the form of the cambered surface taper of convex-concave combination, make mixing liquid film from the first hybrid reaction district in adherent motion process along mixing head, the rapid attenuate of thickness that mixes liquid film, less turbulence aggravation in the liquid film simultaneously, further strengthened the mixed process of liquid film, the incorporation time yardstick of material can reach the Millisecond level; Provide the second hybrid reaction district also can make complete mixed material in the process of adherent motion, proceed reaction, and require the length in the design second hybrid reaction district (mixing head) according to the time scale of reaction with the form of laminar flow.
The basic structure of injection reactor provided by the present invention comprises with lower member: two charging aperture 1a and 1b, central shaft 2, interior endless tube 3, middle endless tube 4 and mixing head 8; Wherein, two charging aperture 1a and 1b are communicated with described central shaft 2, interior endless tube 3 and the coaxial setting in 4 from-inner-to-outer ground of middle endless tube respectively with interior endless tube 3 and middle endless tube 4; Circumferential weld crack in forming between endless tube lower end and the central shaft in described, and circumferential weld crack in forming between middle endless tube lower end and the interior endless tube lower end; The lower end outlet of two annular slots is in essentially identical horizontal level, at least the lower end at middle endless tube has a part that closes up gradually to central shaft 2, shape a in an angle between circumferential weld crack and the middle circumferential weld crack makes the lower end exit of two annular slots form the first hybrid reaction district 7 in making; Described mixing head 8 smoothly links to each other with the lower end of central shaft 2, forms the second hybrid reaction district on the surface of mixing head 8, and described mixing head (8) is the cambered surface of flaring.In the first hybrid reaction district 7, therefrom the ring-shaped liquid film shape material that flows out in the circumferential weld crack outlet and the ring-shaped liquid film shape material that flows out from the outlet of interior circumferential weld crack carry out after impacting type mixes and react, and enter the second hybrid reaction district and continue to finish mixing and react.
Except the reactor of above-mentioned biliquid film, reactor provided by the present invention can also be designed to three liquid films, four liquid films according to the specific requirement of course of reaction or have the reactor of more multi-layered liquid film.For example, when reactor of the present invention was designed to three liquid film reactors, this reactor also further comprised another charging aperture 1c and the outer endless tube 5 that is communicated with this another charging aperture 1c; Described central shaft 2, interior endless tube 3, middle endless tube 4 and the coaxial setting in 5 from-inner-to-outer ground of outer endless tube; Form the outer shroud slit between described outer endless tube lower end and the middle endless tube lower end; The lower end outlet of three annular slots is in essentially identical horizontal level, the lower end of endless tube has a part that closes up gradually to central shaft 2 outside, make between outer shroud slit and the middle circumferential weld crack shape b in an angle, make the lower end exit of three annular slots form the first hybrid reaction district 7.Described mixing head 8 smoothly links to each other with the lower end of central shaft 2, forms the second hybrid reaction district on the surface of mixing head 8.In the first hybrid reaction district 7, from the outer shroud slit, in the circumferential weld crack outlet ring-shaped liquid film shape material that flows out and the ring-shaped liquid film shape material that flows out from the outlet of interior circumferential weld crack carry out after impacting type mixes and react, enter the second hybrid reaction district and continue to finish mixing and react.
Four liquid films or have the structure of more multi-layered liquid film reactor and the structure of three liquid film reactors similar, corresponding ring-type feed pipe and charging aperture are set up in the outside of endless tube 5 outside, get final product thereby the quantity of the annulus that is constituted is increased.
In reactor provided by the present invention, the bottom of described interior endless tube 3 is preferably designed as the undergauge structure, for example, can pass through to increase the diameter of central shaft and/or increase the pipe thickness of interior endless tube bottom, thereby realize the adjusting of internal endless tube annulus thickness.
In reactor provided by the present invention, the bottom that is preferably in central shaft is provided with the fin 6 that the multi-disc height equates, to guarantee the homogeneity of formed interior circumferential weld crack thickness between central shaft 2 and the interior endless tube 3.The structure of described fin, quantity, material etc. can be determined according to concrete reaction requirement and in conjunction with the general knowledge of this area by those skilled in the art, for example, the quantity N of fin 6 〉=3 slice, and fin is measure-alike, the thickness in circumferential weld crack radially was fixed on it on central shaft equably in its thickness was slightly less than.
In reactor provided by the present invention, the lower end of described central shaft 2 is provided with mixing head 8, and seamlessly transits between described central shaft and the mixing head.It is cambered surface taper of convex-concave combination etc. that described mixing head 8 can be designed as conical butt, the cambered surface taper of protruding side, the taper of concave side cambered surface or side.Cambered surface taper described here both can be the cambered surface taper with concave shape lateral surface, also can be the cambered surface taper with convex lateral surface, can also be the cambered surface taper of male and female face combination.Mixing head can also be designed to the combination of different curve according to the flow of material, its physico-chemical property etc., for example, the curved surface of convex-shaped or concavo-convex combination, but the top of curved surface all need adopt continuous cambered surface to be connected with the bottom of central shaft 2, to guarantee that fluid is membranaceous continuous-flow along mixing head.When mixing head was designed to have the cambered surface taper of concave shape lateral surface, the radius R size of its cambered surface was: R=1.1-2.0h, h are the height of mixing head 8; The lower diameter l of mixing head 8
2Be mixing head 8 upper diameter l
12-5 doubly.When mixing head was designed to taper, the top of its taper adopted continuous cambered surface to be connected with the bottom of central shaft 2.
When reactor adopted the design of biliquid film, the angle a in it between circumferential weld crack and the outer shroud slit was designed to the 20-90 degree.Simultaneously with the thickness (d in interior circumferential weld crack
1) be designed to 0.5-5mm, the thickness (d in middle circumferential weld crack
2) be designed to 0.5-3mm.Definite principle of two annulus thickness is: the momentum ratio (Q of the liquid material in circumferential weld crack and interior circumferential weld crack in the process
BV
B: Q
CV
C) be 3: 1-20: 1, be preferably 4: 1-10: 1.
When reactor adopts the design of three liquid films, angle a in it between circumferential weld crack and the middle circumferential weld crack is designed to the 20-60 degree, angle b between middle circumferential weld crack and the outer shroud slit is designed to the 10-60 degree, and the total angle (a+b) between interior circumferential weld crack and the outer shroud slit is between the 30-90 degree.Simultaneously with the thickness (d in interior circumferential weld crack
1) be designed to 0.5-5mm, the thickness (d in middle circumferential weld crack
2) be designed to 0.5-3mm, the thickness (d in outer shroud slit
3) be designed to 0.5-3mm.The design principle of three annulus thickness sizes is: the momentum ratio (Q of the liquid material in circumferential weld crack and interior circumferential weld crack in the process
BV
B: Q
CV
C) be 3: 1-20: 1, be preferably 4: 1-10: 1; Momentum ratio (the Q of the liquid material in process outer shroud slit and middle circumferential weld crack
AV
A: Q
BV
B) be 1: 4-4: 1, be preferably 1: 1-4: 1.
In reactor provided by the present invention, the formed material outlet in each annulus place is the first hybrid reaction district 7, and the lateral wall of the mixing head 8 that links to each other with the central shaft lower end is the second hybrid reaction district.Reactor of the present invention can make from the mixing liquid film in the first hybrid reaction district 7 and proceed in the second hybrid reaction district to mix, react.
In reactor provided by the present invention, interior circumferential weld crack can also be designed to have the passage of cyclone structure, to strengthen mixed process.
Compared with prior art, liquid film colliding type jet reactor provided by the present invention has following beneficial effect:
The liquid film of annulus by several millimeters thick of (1) two strand or the raw material more than two strands, formation is at the strong mutually bump of first reaction zone, the space scale of bump mixed zone is in several millimeter, by the space scale of reduction and strong liquid film colliding, realize efficient for the first time mixing, reaction between the material, the time scale of mixing is at Millisecond;
(2) at second reaction zone, by being designed to the mixing head of flaring, mix liquid film in the adherent motion process in mixing head surface, the rapid attenuate of the thickness of liquid film, and the increase of the less turbulence in the liquid film have further been strengthened mixed process;
(3) in the adherent process of moving, mix the back-mixing degree minimum of liquid film along mixing head at the mixing liquid film, approach desirable " laminar flow " form;
(4) by retraining the outlet shape in the first hybrid reaction district, different mixing requirements can be satisfied, as when requiring the time scale of mixing smaller, stronger outlet constraint can be taked, when bigger, can adopt more weak outlet constraint for the time scale of mixing;
(5), can adapt to different reaction time yardstick requirements by the length that changes mixing head for different reaction time yardstick requirements;
(6) for the process that has gaseous by-product to produce, mix liquid film in adherent the moving in mixing head surface of flaring, help the rapid effusion of gaseous by-product.
Description of drawings
Fig. 1 is the disclosed structure of reactor schematic diagram of GB1238669;
Fig. 2 is the disclosed structure of reactor schematic diagram of USP3507626;
Fig. 3 is the structural representation (biliquid film) of injection reactor provided by the present invention;
Fig. 4 is the structural representation (three liquid films) of injection reactor provided by the present invention;
Fig. 5 to 8 is annulus profiles of injection reactor provided by the present invention;
Fig. 9 to 11 is mixing head structural representations of injection reactor provided by the present invention.
The specific embodiment
Enumerate several concrete embodiments below, further specifying injection reactor provided by the present invention, but therefore the present invention is not subjected to any restriction.
Embodiment A:
As shown in Figure 3, this reactor comprises charging aperture 1a and 1b, central shaft 2, interior endless tube 3, middle endless tube 4 and mixing head 8; Described central shaft 2, interior endless tube 3 and the coaxial setting in 4 from-inner-to-outer ground of middle endless tube; Described mixing head 8 links to each other with the lower end of central shaft 2; Circumferential weld crack in forming between endless tube lower end and the central shaft in described, and circumferential weld crack in forming between middle endless tube lower end and the interior endless tube lower end.
Reactor shown in Figure 3 is worked in the following manner: two gangs of raw material C and B inject the interior endless tube 3 and the endless tube 4 of this reactor respectively through charging aperture 1a and 1b, and flow downward along interior endless tube and middle endless tube.By the interior circumferential weld crack and the middle circumferential weld crack of several millimeters thick, their formed liquid films clash into mutually in the first hybrid reaction district 7 respectively for raw material C and B.The space scale in the first hybrid reaction district, is realized efficient for the first time mixing between the material, is reacted by the space scale of reduction and strong liquid film colliding in several millimeter, and the time scale of mixing is a Millisecond.The logistics of leaving the first hybrid reaction district flows downward and enters second reaction zone.By the mixing head that extends gradually, mix liquid film in the adherent motion process in mixing head surface, the rapid attenuate of the thickness of liquid film, and the increase of the less turbulence in the liquid film have further been strengthened mixed process.In the adherent process of moving, mix the back-mixing degree minimum of liquid film along mixing head at the mixing liquid film, approach desirable " laminar flow " form.From the terminal collecting reaction product of mixing head, after separating, can obtain the final purpose product.
Embodiment B:
As shown in Figure 4, this reactor comprises charging aperture 1a, 1b and 1c, central shaft 2, interior endless tube 3, middle endless tube 4, outer endless tube 5 and mixing head 8; Described central shaft 2, interior endless tube 3, middle endless tube 4 and the coaxial setting in 5 from-inner-to-outer ground of outer endless tube; Described mixing head 8 links to each other with the lower end of central shaft 2; Circumferential weld crack in forming between endless tube lower end and the central shaft in described, circumferential weld crack in forming between middle endless tube lower end and the interior endless tube lower end, and form the outer shroud slit between outer endless tube lower end and the middle endless tube lower end.
Reactor shown in Figure 4 is worked in the following manner: three gangs of raw material C, B and A respectively through charging aperture 1a, 1b and 1c inject this reactor interior endless tube 3, endless tube 4 and outside endless tube 5, and along interior endless tube, middle endless tube and outside endless tube flow downward.By interior circumferential weld crack, middle circumferential weld crack and the outer shroud slit of several millimeters thick, their formed liquid films clash into mutually, mix in the first hybrid reaction district 7 respectively for raw material C, B and A.The space scale in the first hybrid reaction district, is realized efficient for the first time mixing between the material, is reacted by the space scale of reduction and strong liquid film colliding in several millimeter, and the time scale of mixing is a Millisecond.The logistics of leaving the first hybrid reaction district flows downward and enters second reaction zone.By the mixing head that extends gradually, mix liquid film in the adherent motion process in mixing head surface, the rapid attenuate of the thickness of liquid film, and the increase of the less turbulence in the liquid film have further been strengthened mixed process.In the adherent process of moving, mix the back-mixing degree minimum of liquid film along mixing head at the mixing liquid film, approach desirable " laminar flow " form.From the terminal collecting reaction product of mixing head, after separating, can obtain the final purpose product.
Embodiment C:
The structure of reactor as shown in Figure 4.Be that with the difference of embodiment B this embodiment is only handled two strands of raw materials, wherein, endless tube 3 and outer endless tube 5 in raw material C is injected respectively by charging aperture 1a and 1c, and raw material B injects endless tube 4 through charging aperture 1b.Remaining course of reaction is identical with embodiment B.Such logistics arrangement can make two strands of liquid streams realize mixing more fully and reacting.
Embodiment D:
Adopt the injection reactor with four layers of liquid film of the present invention.This embodiment is only handled two kinds of raw materials, and promptly A and B make them inject two feed pipes by two charging apertures respectively, and make raw material A and the formed liquid film of B space.Remaining course of reaction is identical with embodiment B.Such logistics arrangement also can make two strands of liquid streams realize mixing more fully and reacting.The structural representation in the first hybrid reaction district is referring to Fig. 8 in this embodiment.
The following examples will give further instruction to injection reactor provided by the present invention, but therefore the present invention is not subjected to any restriction.
Laser Induced Fluorescence Technology is to estimate a kind of advanced person's of liquid mixed effect method for quantitatively evaluating, its cardinal principle is, utilize some fluorescent materials (as rhodamine B or rhodamine 6G) to excite the visible light wave that produces certain wavelength down, take the picture in flow field again with the high speed digital camera continuously at induced with laser.When the concentration of rhodamine in the solution when certain value is following, the concentration of rhodamine solution is linear with the gray value of corresponding picture pixel, therefore can be by the picture in captured flow field be analyzed, draw the CONCENTRATION DISTRIBUTION of fluorescent material in the flow field, and then the mixing situation between the analysing fluid.Estimated the mixed effect of liquid film colliding type liquid rapid mixing injection reactor of the present invention with this evaluation method.Testing the model that used laser instrument adopts Dantec company to produce is the solid state laser of P I V-100, and the laser intensity of generation is 100mJ; The model of digital camera is a Hisense PIV/PLIF C4742-53-12NRB digital camera, and its resolution ratio is 1280 * 1024 pixels; The fluorescent material that adopts is a rhodamine B.Under described experiment condition, when the concentration of rhodamine B in the solution during in the 0-140 micrograms per litre, the concentration of rhodamine B is linear with corresponding picture pixel gray value size.
Adopt liquid film colliding type liquid rapid mixing injection reactor of the present invention shown in Figure 4, the diameter of its central shaft bottom is 50mm, the size in interior circumferential weld crack is 3mm, the size in middle circumferential weld crack is 1.5mm, the size in outer shroud slit is 1.5mm, angle a between interior circumferential weld crack and the middle circumferential weld crack is designed to 40 degree, and the angle b between middle circumferential weld crack and the outer shroud slit is designed to 30 degree, and the form of acylic motion is adopted in interior circumferential weld crack.Stronger constraint is as shown in Figure 6 adopted in exit, first mixed zone, and mixing head adopts the cambered surface design of flaring as shown in Figure 9, and its height h is 100mm, and the radius R of cambered surface is 130mm.The tracer rhodamine B is from connecting liquid delivery tube (the liquid delivery tube long enough of charging aperture 1c and charging aperture 1a, to guarantee before tracer enters charging aperture fully, to be blended in the current equably) top injects continuously, its concentration is 100 micrograms per litre, and the pressure of import department's water is 3.5kg/cm
2, the flow that charging aperture 1c contains at the place water of tracer is 5m
3The flow that/hr, charging aperture 1a contain at the place water of tracer is 5m
3/ hr.Charging aperture 1b advances running water with constant speed, and the pressure of import department's water is 3.5kg/cm
2, water yield size is 10m
3/ hr.Have the aqueous solution of tracer rhodamine B and the mixed effect between the running water with the laser Induced Fluorescence Technology evaluation, in exit, first mixed zone, the segregation degree of the mixing liquid film that three fluid streams form (represents that with IOS promptly reach when mixing fully when a plurality of fluids, the IOS value is 0; When fluid complete when unmixed, segregation degree value is 1) be 56%, two fluid streams reach the required elapsed time of 95% mixed effect (this moment, degree of segregation IOS value was 5%, the gray value unanimity of mixed zone 95% on the image) (counting from beginning to clash into) and are about 2.2 milliseconds.If do not establish the mixing head of flaring, and adopt columned mixing head as second mixing, reaction zone (body diameter is identical with the central shaft lower diameter), other structure is identical with the structure of reactor described in the embodiment 1, and two fluid streams reach 95% mixed effect needs elapsed time to be about 8.5 milliseconds.
Adopt liquid film colliding type liquid rapid mixing injection reactor of the present invention shown in Figure 4, the diameter of its central shaft bottom is 100mm, the size in interior circumferential weld crack is 2.5mm, the size in middle circumferential weld crack is 1mm, the size in outer shroud slit is 1.5mm, angle a between interior circumferential weld crack and the middle circumferential weld crack is designed to 50 degree, and the angle b between middle circumferential weld crack and the outer shroud slit is designed to 25 degree, and eddy flow design (angle of eddy flow direction and central shaft radial direction is 20 degree) is adopted in interior circumferential weld crack.More weak constraint is as shown in Figure 7 adopted in exit, first mixed zone, and mixing head adopts the cambered surface design form of flaring as shown in Figure 9, and its height h is 100mm, and the radius R of cambered surface is 150mm.The tracer rhodamine B is from connecting liquid delivery tube (the liquid delivery tube long enough of charging aperture 1c and charging aperture 1a, to guarantee before tracer enters charging aperture fully, to be blended in the current equably) top injects continuously, its concentration is 120 micrograms per litre, and the pressure of import department's water is 3.5kg/cm
2, the flow that charging aperture 1c contains at the place water of tracer is 8m
3The flow that/hr, charging aperture 1a contain at the place water of tracer is 10m
3/ hr.Charging aperture 1b advances running water with constant speed, and the pressure of import department's water is 3.5kg/cm
2, water yield size is 10m
3/ hr.Have the aqueous solution of tracer rhodamine B and the mixed effect between the running water with the laser Induced Fluorescence Technology evaluation, exit in first mixed zone, the IOS value of the mixing liquid film that three fluid streams form is that 42%, three fluid streams reaches 95% the required elapsed time of mixed effect and is about 1.0 milliseconds.If do not establish the mixing head of flaring, and adopt columned mixing head as second mixing, reaction zone (body diameter is identical with the central shaft lower diameter), other structure is identical with the structure of reactor described in the embodiment 2, and three fluid streams reach 95% mixed effect needs elapsed time to be about 6.3 milliseconds.
Adopt liquid film colliding type liquid rapid mixing injection reactor of the present invention shown in Figure 3, the diameter of its central shaft bottom is 80mm, and the size in interior circumferential weld crack is 4mm, and the size in middle circumferential weld crack is 2mm, no outer shroud slit (as shown in Figure 3); Angle a between interior circumferential weld crack and the middle circumferential weld crack is designed to 45 degree, and the form of acylic motion design is adopted in interior circumferential weld crack.Mixing head adopts conical design as shown in figure 10, and its height h is 100mm, the bottom surface diameter l of taper
2Be 200mm.The tracer rhodamine B is from connecting liquid delivery tube (the liquid delivery tube long enough of charging aperture 1b, to guarantee before tracer enters charging aperture fully, to be blended in the current equably) top injects continuously, its concentration is 120 micrograms per litre, and the pressure of import department's water is 3.5kg/cm
2, the flow that charging aperture 1b contains at the place water of tracer is 20m
3/ hr.Charging aperture 1a advances running water with constant speed, and the pressure of import department's water is 3.5kg/cm
2, water yield size is 10m
3/ hr.Have the aqueous solution of tracer rhodamine B and the mixed effect between the running water with the laser Induced Fluorescence Technology evaluation, exit in first mixed zone, the IOS value of the mixing liquid film that two fluid streams form is that 63%, two fluid streams reaches 95% the required elapsed time of mixed effect and is about 3.5 milliseconds.If do not establish the mixing head of flaring, and adopt columned mixing head as second mixing, reaction zone (body diameter is identical with the central shaft lower diameter), other structure is identical with the structure of reactor described in the embodiment 3, and two fluid streams reach 95% mixed effect needs elapsed time to be about 12.8 milliseconds.
Claims (11)
1. a liquid film colliding type jet reactor comprises with lower member: two charging apertures (1a and 1b), central shaft (2), interior endless tube (3), middle endless tube (4) and mixing head (8); Wherein, two charging apertures (1a and 1b) are communicated with interior endless tube (3) and middle endless tube (4) respectively, described central shaft (2), interior endless tube (3) and the coaxial setting in middle endless tube (4) from-inner-to-outer ground; Circumferential weld crack in forming between endless tube lower end and the central shaft in described, and circumferential weld crack in forming between middle endless tube lower end and the interior endless tube lower end; The lower end outlet of two annular slots is in essentially identical horizontal level, at least the lower end at middle endless tube has a part that closes up gradually to central shaft (2), shape a in an angle between circumferential weld crack and the middle circumferential weld crack makes the lower end exit of two annular slots form the first hybrid reaction district (7) in making; Described mixing head (8) smoothly links to each other with the lower end of central shaft (2), forms the second hybrid reaction district on the surface of mixing head (8); Described mixing head (8) is the cambered surface of flaring.
2. according to the described reactor of claim 1, it is characterized in that described mixing head (8) is that conical butt, the cambered surface taper of protruding side, the taper of concave side cambered surface or side are the cambered surface taper of convex-concave combination.
3. according to the described reactor of claim 2, it is characterized in that, when described mixing head is the taper of concave side cambered surface, the radius R of its concave side cambered surface=1.1～2.0h, the lower diameter l of mixing head
2Be mixing head upper diameter l
12～5 times; H is the vertical height of mixing head.
4. according to the described reactor of claim 3, it is characterized in that the bottom of described central shaft is provided with fin (6), and the thickness of fin be slightly less than in the thickness in circumferential weld crack, the quantity N of fin 〉=3 slice.
5. according to the described reactor of claim 4, it is characterized in that the bottom of described interior endless tube (3) is by diameter that increases central shaft and/or the pipe thickness formation undergauge structure that increases interior endless tube bottom.
6. according to the described reactor of claim 5, it is characterized in that the angle a between described interior circumferential weld crack and the middle circumferential weld crack is 20～90 degree; The thickness d in interior circumferential weld crack
1Be 0.5～5mm, the thickness d in middle circumferential weld crack
2Be 0.5～3mm.
7. according to the described reactor of one of claim 1～6, it is characterized in that described interior circumferential weld crack is the passage that has cyclone structure.
8. according to the described reactor of one of claim 1～6, it is characterized in that, this reactor also comprises another charging aperture (1c) and the outer endless tube (5) that is communicated with this another charging aperture (1c), described central shaft (2), interior endless tube (3), middle endless tube (4) and the coaxial setting in outer endless tube (5) from-inner-to-outer ground; Form the outer shroud slit between described outer endless tube lower end and the middle endless tube lower end; The lower end outlet of three annular slots is in essentially identical horizontal level, the lower end of endless tube has a part that closes up gradually to central shaft (2) outside, make between outer shroud slit and the middle circumferential weld crack shape b in an angle, make the lower end exit of three annular slots form the first hybrid reaction district (7).
9. according to the described reactor of claim 8, it is characterized in that the middle circumferential weld crack of this reactor and the angle b between the outer shroud slit are 10～60 degree, the total angle (a+b) between interior circumferential weld crack and the outer shroud slit is 30～90 degree; The thickness d in its outer shroud slit
3Be 0.5～3mm.
10. according to the described reactor of claim 9, it is characterized in that described interior circumferential weld crack is the passage that has cyclone structure.
11., it is characterized in that this reactor also comprises ring-type feed pipe that one or more layers is arranged at outer endless tube (5) outside and the corresponding charging aperture that is communicated with respectively with this ring-type feed pipe according to the described reactor of claim 8.
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| CN101153015B (en) * | 2006-09-28 | 2010-06-16 | 宁波万华聚氨酯有限公司 | Hole shooting flow type reactor and method for producing isocyanic ester by using the reactor |
| CN101209405B (en) * | 2006-12-27 | 2013-08-28 | 宁波万华聚氨酯有限公司 | Hole jet type injecting reactor |
| CN101811019B (en) * | 2010-04-19 | 2012-01-18 | 烟台万华聚氨酯股份有限公司 | Dynamic hole jet reactor and method for preparing isocyanate by adopting dynamic hole jet reactor |
| CN104226202B (en) * | 2014-09-20 | 2017-03-29 | 中北大学 | Clash into flow structure and percussion flow-rotary packed bed device |
| CN107042077B (en) * | 2017-05-19 | 2020-03-10 | 温州华菲食品机械科技有限公司 | Adder for material additive |
| CN107803125B (en) * | 2017-12-15 | 2023-08-22 | 上海梵坤环保科技发展有限公司 | Combined gas-liquid fusion device of serial venturi tube |
| CN110075779B (en) * | 2019-05-31 | 2024-02-09 | 昆明理工大学 | Jet reactor for powder material synthesis and powder synthesis method |
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| CN1327905A (en) * | 2001-05-22 | 2001-12-26 | 华东理工大学 | Stirring-spraying fluidized bed and its application in preparing fibre reinforced composite material |
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