CN112537761B - External circulation ammonification reactor and ammonium phosphate production method - Google Patents
External circulation ammonification reactor and ammonium phosphate production method Download PDFInfo
- Publication number
- CN112537761B CN112537761B CN202011281053.7A CN202011281053A CN112537761B CN 112537761 B CN112537761 B CN 112537761B CN 202011281053 A CN202011281053 A CN 202011281053A CN 112537761 B CN112537761 B CN 112537761B
- Authority
- CN
- China
- Prior art keywords
- lifting pipe
- gas
- ammonia
- slurry
- sedimentation separator
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B25/00—Phosphorus; Compounds thereof
- C01B25/16—Oxyacids of phosphorus; Salts thereof
- C01B25/26—Phosphates
- C01B25/28—Ammonium phosphates
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/18—Stationary reactors having moving elements inside
Abstract
The invention discloses an external circulation ammonification reactor and an ammonium phosphate production method. The reactor comprises a sedimentation separator, a stirring device, a lifting pipe, a return pipe, a circulating pump and two gas ammonia nozzles; the two gas-ammonia nozzles are vertically arranged on the lifting pipe and are positioned on the same plane, the two gas-ammonia nozzles are respectively arranged on the side walls of the two sides of the lifting pipe and are not positioned on the same semicircular side wall, the air injection directions of the two gas-ammonia nozzles are the same as the eccentric distance e of the circle center of the lifting pipe on the plane, and the lifting pipe is also provided with a phosphoric acid inlet; the stirring device is used for mixing and stirring the slurry in the sedimentation separator. The invention adopts the gas ammonia nozzle which is relatively eccentric and is vertical to the lifting pipe of the reactor to ensure that gas ammonia enters the sedimentation separator to form rotational flow, reduce the viscosity of slurry and improve the blocking problem, and the slurry of the sedimentation separator generates forced rotational flow under the action of the stirring device, so that flocculent solid particles are crushed, the problem that the slurry blocks a pipeline is greatly improved, and the mixing reaction is more uniform.
Description
Technical Field
The invention relates to the technical field of phospham production, in particular to an external circulation ammonification reactor and a phospham production method.
Background
The industrial monoammonium phosphate is widely applied to the industries of flame retardants, fire extinguishing agents, flame retardance of textiles, papermaking processing and the like, and has great market demands. The phosphoric acid production mainly comprises a thermal method and 2 wet processes, the thermal method phosphoric acid is gradually eliminated due to large pollution and high cost, and the wet method phosphoric acid production of ammonium phosphate has become the necessary trend of industry development. The external circulation ammonification reactor has the advantages of no internal parts, uniform material mixing, severe turbulence, high bubble dispersion degree, large mass transfer area and the like, and is a key device for producing ammonium phosphate by a wet method. Along with the improvement of production load, the quality of phosphorite is reduced, the impurity content is increased, the viscosity of slurry is increased, the fluidity is poor, the slurry is easy to scale and block the air inlet hole of the gas distributor, the phosphoric acid and ammonia are not fully reacted, the ammonia escape rate is high, and the yield of phospham is low. The escape of ammonia gas causes the waste of resources and environmental pollution. Thus, the phospham industry is rapidly developing, but generally is still at a level of high input, high pollution, high consumption, low output, and low benefit, at the expense of high consumption of phosphorus resources, ecological damage, and environmental pollution. The key factor determining the production efficiency of the external circulation ammoniation reactor is gas-liquid mass transfer. By increasing the gas-liquid interface area or mass transfer coefficient, mass transfer can be improved, and productivity can be improved. On the one hand, reducing the bubble diameter can increase the gas-liquid interface area; on the other hand, enhancing turbulence can increase the probability of large bubbles collapsing and increase the surface update frequency of the bubbles, thereby increasing the mass transfer coefficient. Therefore, research and development of a novel efficient external circulation ammoniation reactor strengthens gas-liquid mass transfer, reduces ammonia loss, eliminates slurry blocking a pipeline and an air inlet, and becomes a problem to be solved in the current ammonium phosphate industry.
Disclosure of Invention
The invention aims to solve the defects of the prior art and provides an external circulation ammoniation reactor and a production method of ammonium phosphate, which improve the mass transfer reaction efficiency and also improve the problem that slurry blocks a pipeline and an air inlet.
An external circulation ammonification reactor comprises a sedimentation separator, a stirring device, a lifting pipe, a return pipe, a circulating pump and two gas ammonia nozzles;
the sedimentation separator is provided with a circulating inlet and a circulating outlet which are communicated with the inside of the sedimentation separator, one end of the return pipe is communicated with the liquid inlet of the circulating pump, the other end of the return pipe is communicated with the circulating outlet, one end of the lifting pipe is communicated with the liquid outlet of the circulating pump, and the other end of the lifting pipe is communicated with the circulating inlet; the top of the sedimentation separator is provided with a steam outlet, and the bottom of the sedimentation separator is provided with a slurry outlet and a slag discharge outlet;
the two gas-ammonia nozzles are vertically arranged on the lifting pipe and are positioned on the same plane, the two gas-ammonia nozzles are respectively arranged on the side walls of the two sides of the lifting pipe and are not positioned on the same semicircular side wall, the air injection directions of the two gas-ammonia nozzles are the same as the eccentric distance e of the circle center of the lifting pipe on the plane, and the lifting pipe is also provided with a phosphoric acid inlet;
the stirring device is used for mixing and stirring the slurry in the sedimentation separator.
Further, the eccentricity e is 0.2-0.3 times of the diameter D of the lifting pipe.
Further, the inner wall of the lifting pipe is provided with a diversion spiral sheet extending spirally along the axial direction of the lifting pipe.
Further, the pitch H of the diversion spiral sheet is 0.1-0.2 times of the diameter D of the lifting pipe.
Further, the thickness S of the diversion spiral sheet is 0.2-0.3 times of the screw pitch H, and the width W of the diversion spiral sheet is 1-2 times of the thickness S.
Further, the phosphoric acid inlet is positioned below the two ammonia gas nozzles.
Furthermore, the lifting pipe is positioned on a pipeline between the gas ammonia nozzle and the circulating pump and is also provided with a regulating valve.
Further, the circulation inlet is positioned below the circulation outlet.
Further, agitating unit includes driving piece, rotation axis and a plurality of blade, the rotation axis is vertical to be set up in the sedimentation separator, a plurality of the blade is installed around the rotation axis bottom, the top of rotation axis stretches out the sedimentation separator with the driving piece transmission is connected, the driving piece drive the rotation axis drives the blade is rotatory.
An ammonium phosphate production method uses the external circulation ammonification reactor.
According to the invention, nozzles which are relatively eccentric and are perpendicular to a lifting pipe of the reactor are adopted, so that gas ammonia enters a sedimentation separator to form rotational flow, the air injection directions of the two gas ammonia nozzles are the same as the center of the lifting pipe on the plane, the eccentric distance is increased, the slurry speed around the nozzles is obviously layered under the tangential speed action of ammonia bubbles, the speed gradient is increased to form rotational flow, the gas-liquid turbulence is enhanced, the particle size of the bubbles is reduced under the action of liquid phase shearing force, the specific surface area is increased, the update rate of fluid on the surface of the bubbles is accelerated, the mixing and mass transfer of gas and liquid are enhanced, the chemical reaction efficiency of ammonia and phosphoric acid solution is improved, and the ammonia loss is reduced; meanwhile, turbulence and shear force enhancement are also beneficial to breaking the flocculation net structure of the slurry, reducing the viscosity of the slurry and improving the blocking problem; the nozzle is perpendicular to the riser, so that slurry is not easy to block the air inlet, and therefore, the invention not only improves the mass transfer reaction efficiency, but also improves the problem that the slurry blocks the pipeline and the air inlet.
The slurry of the sedimentation separator generates forced rotational flow under the action of the stirring device, the flocculent solid particles are crushed and are settled and separated, and the flocculent solid particles are discharged from a bottom slag discharge port, so that the problem that the slurry blocks a pipeline is greatly improved, the mixing reaction is more uniform, the slurry is output to the next procedure at the lower end of the sedimentation separator, and part of unreacted clear liquid is conveyed to a riser tube from a circulating outlet above the sedimentation separator for reaction again, thereby improving the yield of ammonium phosphate.
Drawings
FIG. 1 is a schematic diagram of an external circulation ammonification reactor according to the present invention;
fig. 2 is an enlarged view at B in fig. 1;
fig. 3 is a schematic structural diagram of an ammonia gas nozzle of an external circulation ammonification reactor according to the present invention.
1. A sedimentation separator; 11. a circulation inlet; 12. a circulation outlet; 13. a steam outlet; 14. a slurry outlet; 15. a slag discharge port; 2. a stirring device; 21. a driving member; 22. a rotation shaft; 23. a blade; 3. a riser; 31. a phosphoric acid inlet; 4. a return pipe; 5. a circulation pump; 6. a gas ammonia nozzle; 7. a flow guiding spiral sheet; 8. and (3) regulating the valve.
Detailed Description
The following are specific embodiments of the present invention and the technical solutions of the present invention will be further described with reference to the accompanying drawings, but the present invention is not limited to these embodiments.
As shown in fig. 1, an external circulation ammonification reactor of the invention comprises a sedimentation separator 1, a stirring device 2, a lifting pipe 3, a return pipe 4, a circulating pump 5 and two gas ammonia nozzles 6;
the sedimentation separator 1 is provided with a circulating inlet 11 and a circulating outlet 12 which are communicated with the inside of the sedimentation separator, one end of a return pipe 4 is communicated with a liquid inlet of the circulating pump 5, the other end of the return pipe is communicated with the circulating outlet 12, one end of a lifting pipe 3 is communicated with a liquid outlet of the circulating pump 5, and the other end of the lifting pipe is communicated with the circulating inlet 11; the top of the sedimentation separator 1 is provided with a steam outlet 13, and the bottom is provided with a slurry outlet 14 and a slag discharge outlet 15;
the two gas ammonia nozzles 6 are vertically arranged on the lifting pipe 3 and are positioned on the same plane, the two gas ammonia nozzles 6 are respectively arranged on the side walls of the two sides of the lifting pipe 3 and are not positioned on the same semicircular side wall, the air injection directions of the two gas ammonia nozzles 6 are the same as the eccentric distance e of the circle center of the lifting pipe 3 on the plane, and the lifting pipe 3 is also provided with a phosphoric acid inlet 31;
the stirring device 2 is used for mixing and stirring the slurry in the sedimentation separator 1.
According to the invention, nozzles which are relatively eccentric and are perpendicular to the lifting pipe 3 of the reactor are adopted, so that gas ammonia enters the sedimentation separator 1 to form rotational flow, the air injection directions of the two gas ammonia nozzles 6 are the same as the center of the lifting pipe 3 on the plane, the eccentric distance is increased, the slurry speed around the nozzles is obviously layered under the tangential speed action of ammonia bubbles, the speed gradient is increased, rotational flow is formed, the turbulence of gas and liquid is enhanced, the particle size of the bubbles is reduced under the action of liquid phase shearing force, the specific surface area is increased, the update rate of the fluid on the surface of the bubbles is accelerated, the mixing and mass transfer of gas and liquid are enhanced, the chemical reaction efficiency of ammonia and phosphoric acid solution is improved, and the ammonia loss is reduced; meanwhile, turbulence and shear force enhancement are also beneficial to breaking the flocculation net structure of the slurry, reducing the viscosity of the slurry and improving the blocking problem; the nozzle is arranged perpendicular to the riser pipe 3, so that the slurry is not easy to block the air inlet, and therefore, the invention not only improves the mass transfer reaction efficiency, but also improves the problem that the slurry blocks the pipeline and the air inlet.
The slurry of the sedimentation separator 1 generates forced rotational flow under the action of the stirring device 2, the flocculent solid particles are crushed and are settled and separated, and the flocculent solid particles are discharged from the bottom slag discharge outlet 15, so that the problem that the slurry blocks a pipeline is greatly improved, the mixing reaction is more uniform, the slurry is output to the next process at the lower end of the sedimentation separator 1, and part of unreacted clear liquid is conveyed to the riser tube 3 from the circulating outlet 12 above the sedimentation separator 1 for further reaction, thereby improving the yield of ammonium phosphate.
As shown in fig. 3, the eccentricity e may be 0.2-0.3 times the diameter D of the riser 3, and the eccentricity is too small, so that the effect of reinforcing the swirling flow is weak; the eccentricity is too large, the processing and the manufacturing are difficult, and the effect of strengthening the rotational flow is also weakened.
The inner wall of the lifting pipe 3 can be provided with a diversion spiral sheet 7 which extends and spirals along the axial direction of the lifting pipe to strengthen rotational flow, so that the gas-liquid turbulent intensity is greatly increased, large bubbles are broken into small bubbles under the action of strong shearing force of a flow field, and the specific surface area of the bubbles is increased; the rotating fluid can also enhance the mixing of the fluids, the entrainment capacity and the mixing effect are larger than those of no rotational flow, the mass transfer coefficient is improved, the reaction of the phosphoric acid solution and the ammonia gas is more sufficient, and the ammonia escape rate is reduced. Under the action of strong turbulence, the flocculation net structure of the slurry is disassembled by the shearing force of the fluid, the viscosity is reduced, and the probability of blocking the pipeline by the slurry is greatly reduced;
as shown in fig. 2, the pitch H of the guiding spiral 7 may be 0.1 to 0.2 times the diameter D of the riser 3. The number of turns of the diversion spiral sheet 7 can be adjusted, the height of the lifting pipe 3 is certain, the number of turns is increased, the screw pitch is reduced, the rotation of fluid is increased, entrainment and mixing of surrounding fluid are enhanced, the fluid shear force is increased, the average particle size of bubbles is reduced, and the gas-liquid mass transfer reaction is enhanced. The ammonia gas bubbles spiral along the riser 3, when no flow guiding spiral sheet 7 exists, the axial length of the bubbles for completing spiral periodic variation is 3D, the screw pitch H is set to be 0.1-0.2 times of the diameter D of the riser 3, so that the axial length of the bubbles for completing the spiral periodic variation is reduced, the rotational flow and turbulence intensity of fluid are improved, and the particle size of the bubbles is reduced.
The thickness S of the flow guiding spiral sheet 7 may be 0.2 to 0.3 times the pitch H, and the width W of the flow guiding spiral sheet 7 may be 1 to 2 times the thickness S. The thickness of the diversion spiral sheet 7 can be adjusted, the thickness is increased, the longitudinal flow resistance of the fluid is increased, the spiral rising speed of ammonia gas bubbles in slurry is reduced, the residence time of the ammonia gas bubbles is prolonged, and the reaction is more complete; on the other hand, the thickening of the diversion spiral sheet 7 also causes the increase of the liquid slurry velocity gradient around the diversion spiral sheet, the increase of the disturbance to the fluid micro-clusters, the increase of the turbulence intensity, the increase of the shearing force suffered by the bubbles, the breaking of the large bubbles and the enhancement of the mixing, so that the reaction is more sufficient and the ammonia escape is reduced. The flight thickness cannot be excessive, avoiding the formation of flow dead zones.
The width of the diversion spiral sheet 7 can be adjusted, the width is increased, the wall effect of the spiral sheet is enhanced, the deformation of bubbles and the formation of wake vortexes are limited, the symmetrical vortex shedding and the transition of the bubble path from spiral to zigzag movement are inhibited, so that the residence time of the bubbles is prolonged, and the mass transfer and reaction are enhanced. Too large a flight width increases the flow resistance and reduces the distribution of bubbles near the wall. The width W of the spiral sheet can be 1S-2S, S is the thickness of the spiral sheet.
The flow rate of the steam outlet 13 is measured by a flowmeter, the mass fraction of ammonia at the steam outlet 13 is measured by a Nahner reagent spectrophotometry, and the ammonia escape amount can be obtained through calculation, if the ammonia escape amount exceeds the standard, the thickness and the width of the spiral sheet are increased, so that the turbulence intensity and the residence time of bubbles are improved, and finally the yield of ammonium phosphate is improved and the ammonia loss is reduced.
The phosphoric acid inlet 31 may be located below the two ammonia gas nozzles 6. The phosphoric acid inlet 31 is arranged below the gas ammonia nozzle 6, the phosphoric acid is mixed with ammonia gas bubbles under the action of strong turbulent motion energy under the drive of the circulating pump 5, a large amount of heat is discharged, turbulent flow and mixing are further enhanced, the reaction is more sufficient, the ammonia escape rate is reduced,
the lifting pipe 3 is positioned on a pipeline between the gas ammonia nozzle 6 and the circulating pump 5 and can be further provided with a regulating valve 8, and the equivalent diameter of the lifting pipe is changed, so that the equivalent diameter ratio of the lifting pipe and the sedimentation separator is changed, the equivalent diameter ratio is reduced, and the circulating liquid speed is increased. The regulating valve and the circulating pump regulate the circulating liquid speed in the riser together, so as to change the rising speed and the turbulent intensity of ammonia bubbles in the riser. When the viscosity of the slurry is increased, the regulating valve needs to be reduced, the equivalent diameter of the lifting pipe is reduced, the rotating speed of the circulating pump is increased, and the slurry is prevented from blocking the pipeline.
The circulating inlet 11 is positioned below the circulating outlet 12, and the escaped ammonia gas can further react with the residual phosphoric acid in the sedimentation separator 1, so that the yield of ammonium phosphate is improved, and the ammonia loss is further reduced.
The stirring device 2 has various structures, but not limited to, in this embodiment, the stirring device 2 may include a driving member 21, a rotation shaft 22, and a plurality of blades 23, where the rotation shaft 22 is vertically disposed in the sedimentation separator 1, the plurality of blades 23 are installed around the bottom end of the rotation shaft 22, the top end of the rotation shaft 22 extends out of the sedimentation separator 1 and is in transmission connection with the driving member 21, and the driving member 21 drives the rotation shaft 22 to rotate with the blades 23. The driving piece 21 can be a motor, and the rotating speed of the motor can be adjusted, so that the rotating speed of the rotating shaft 22 and the rotating speed of the blades 23 are adjusted, the fluid in the sedimentation separator 1 generates forced rotational flow, the turbulence of gas and liquid is enhanced, the flocculent solid particles in the sedimentation separator 1 can be detached, the viscosity is further reduced, the turbulence diffusion coefficient is improved, and the slurry is more uniformly mixed; the insufficiently reacted ammonia gas escaping from the circulation outlet 12 breaks down under the action of strong rotational flow shearing to form small bubbles, which continue to react with phosphoric acid in the sedimentation separator 1. Fe, ca, mg, al, siO in wet phosphoric acid 2 、S0 4 2- Impurities such as F and the like generate insoluble solid impurity particles in the ammonia neutralization process, and the solid impurity particles are settled along the settlement separator 1 under the centrifugal force of the forced rotational flow and can be discharged from the slag discharge port 15, and the cleaner slurry is output from the slurry outlet 14 to the next process. The supernatant is output from the circulation outlet 12 and flows through the bottom return pipe 4 to enter the riser 3 for re-reaction.
The method for producing ammonium phosphate uses the external circulation ammoniation reactor, wherein the flow rate of the steam outlet 13 can be measured by a flowmeter, the mass fraction of ammonia at the steam outlet 13 can be measured by adopting a Nami reagent spectrophotometry, and the ammonia escape amount can be obtained through calculation, if the ammonia escape amount exceeds the standard, the eccentricity e can be properly increased, the thickness and the width of the diversion spiral sheet 7 can be increased, and the screw pitch of the diversion spiral sheet can be reduced.
The above is not relevant and is applicable to the prior art.
While certain specific embodiments of the present invention have been described in detail by way of example, it will be appreciated by those skilled in the art that the foregoing examples are provided for the purpose of illustration only and are not intended to limit the scope of the invention, and that various modifications or additions and substitutions to the described specific embodiments may be made by those skilled in the art without departing from the scope of the invention or exceeding the scope of the invention as defined in the accompanying claims. It should be understood by those skilled in the art that any modification, equivalent substitution, improvement, etc. made to the above embodiments according to the technical substance of the present invention should be included in the scope of protection of the present invention.
Claims (6)
1. An external circulation ammonification reactor, which is characterized in that: comprises a sedimentation separator (1), a stirring device (2), a lifting pipe (3), a return pipe (4), a circulating pump (5) and two gas-ammonia nozzles (6);
the sedimentation separator (1) is provided with a circulating inlet (11) and a circulating outlet (12) which are communicated with the inside of the sedimentation separator, one end of the return pipe (4) is communicated with a liquid inlet of the circulating pump (5), the other end of the return pipe is communicated with the circulating outlet (12), one end of the lifting pipe (3) is communicated with a liquid outlet of the circulating pump (5), and the other end of the lifting pipe is communicated with the circulating inlet (11); the top of the sedimentation separator (1) is provided with a steam outlet (13), and the bottom is provided with a slurry outlet (14) and a slag discharge outlet (15);
the two gas ammonia nozzles (6) are vertically arranged on the lifting pipe (3) and are positioned on the same plane, the two gas ammonia nozzles (6) are respectively arranged on the side walls of the two sides of the lifting pipe (3) and are not positioned on the same semicircular side wall, the air injection directions of the two gas ammonia nozzles (6) and the circle center of the lifting pipe (3) positioned on the plane have the same eccentric distance e, and the lifting pipe (3) is also provided with a phosphoric acid inlet (31);
the stirring device (2) is used for mixing and stirring the slurry in the sedimentation separator (1);
the eccentricity e is 0.2-0.3 times of the diameter D of the lifting pipe (3);
the inner wall of the lifting pipe (3) is provided with a diversion spiral sheet (7) which extends spirally along the axial direction of the lifting pipe;
the phosphoric acid inlet (31) is positioned below the two ammonia gas nozzles (6);
the circulation inlet (11) is positioned below the circulation outlet (12).
2. An external circulation ammonification reactor according to claim 1, wherein: the screw pitch H of the diversion spiral sheet (7) is 0.1-0.2 times of the diameter D of the lifting pipe (3).
3. An external circulation ammonification reactor according to claim 2, wherein: the thickness S of the diversion spiral sheet (7) is 0.2-0.3 times of the screw pitch H, and the width W of the diversion spiral sheet (7) is 1-2 times of the thickness S.
4. An external circulation ammonification reactor according to claim 1, wherein: the lifting pipe (3) is positioned on a pipeline between the gas ammonia nozzle (6) and the circulating pump (5) and is also provided with a regulating valve (8).
5. An external circulation ammonification reactor according to claim 1, wherein: stirring device (2) are in including driving piece (21), rotation axis (22) and a plurality of blade (23), rotation axis (22) are vertical to be set up in subside separator (1), a plurality of blade (23) are installed around rotation axis (22) bottom, the top of rotation axis (22) stretches out subside separator (1) with driving piece (21) transmission is connected, driving piece (21) drive rotation axis (22) drive blade (23) are rotatory.
6. A production method of ammonium phosphate is characterized in that: use of an external circulation ammonification reactor according to any of claims 1-5.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202011281053.7A CN112537761B (en) | 2020-11-16 | 2020-11-16 | External circulation ammonification reactor and ammonium phosphate production method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202011281053.7A CN112537761B (en) | 2020-11-16 | 2020-11-16 | External circulation ammonification reactor and ammonium phosphate production method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN112537761A CN112537761A (en) | 2021-03-23 |
| CN112537761B true CN112537761B (en) | 2023-06-02 |
Family
ID=75014108
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202011281053.7A Active CN112537761B (en) | 2020-11-16 | 2020-11-16 | External circulation ammonification reactor and ammonium phosphate production method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN112537761B (en) |
Family Cites Families (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103773441B (en) * | 2012-10-24 | 2015-09-30 | 中国石油化工股份有限公司 | A kind of ebullated bed liquid-phase hydrogenatin treatment process |
| CN103551087B (en) * | 2013-11-08 | 2015-11-18 | 神马实业股份有限公司 | A kind of Ammoximation reaction system for the preparation of cyclohexanone oxime |
| CN205773362U (en) * | 2016-06-27 | 2016-12-07 | 宜昌富升化工有限公司 | A kind of ammoniation reactor of good antiscale property |
| CN106216126B (en) * | 2016-09-11 | 2018-06-19 | 中国计量大学 | Suitable for the effervescent atomizer of shear shinning non-newtonian fluid |
-
2020
- 2020-11-16 CN CN202011281053.7A patent/CN112537761B/en active Active
Also Published As
| Publication number | Publication date |
|---|---|
| CN112537761A (en) | 2021-03-23 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| Wang et al. | Hydrodynamics of froth flotation and its effects on fine and ultrafine mineral particle flotation: A literature review | |
| CN103768980B (en) | A kind of sweep short blade composite stirrer | |
| WO2020186635A1 (en) | Enhanced emulsion reaction system on oil-coal co-hydrogenation micro-interface | |
| CN108671875A (en) | A kind of multiphase flow reinforcing mass transfer reaction device | |
| CN110237794A (en) | Ultrasound-enhanced shooting flow type reactor | |
| CN112537761B (en) | External circulation ammonification reactor and ammonium phosphate production method | |
| CN106621901A (en) | Sludge treatment chemical adding pipeline mixer | |
| CN113413846A (en) | Ultrasonic-enhanced reverse vortex flow impinging stream reactor | |
| CN109224512B (en) | Impact extraction device and extraction method thereof | |
| WO2020186636A1 (en) | Micro-interface emulsification bed enhanced reaction system for hydrogenation of coal tar | |
| CN201823495U (en) | Gas-filling stirring device | |
| CN216703990U (en) | Vortex type liquid raw material online static mixer | |
| CN216890150U (en) | Variable-circulation multi-directional-flow efficient mixing reaction device | |
| CN108325493A (en) | A kind of granular medicine action system and method based on strong turbulence cycle | |
| CN210171247U (en) | Liquid mixing tank | |
| CN108642275A (en) | A kind of efficient leaching tanks of gold mine ore pulp | |
| CN112221459B (en) | Polyether neutralization reactor | |
| CN209155170U (en) | A kind of rapid crystallization equipment of potassium fluotitanate | |
| CN114105381A (en) | Collision type uniform cavitation sewage treatment device and method thereof | |
| CN112657451A (en) | External circulation ammoniation reactor | |
| CN211487221U (en) | Jet stirring device | |
| CN110681275B (en) | Rotational flow stirring and mixing device and method | |
| CN201598320U (en) | Gold-containing copper pyrite reaction device | |
| CN208906069U (en) | A kind of multiphase flow reinforcing mass transfer reaction device | |
| CN208244736U (en) | A kind of granular medicine action system based on strong turbulence circulation |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |