CN112537761A - External circulation ammoniation reactor - Google Patents
External circulation ammoniation reactor Download PDFInfo
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- CN112537761A CN112537761A CN202011281053.7A CN202011281053A CN112537761A CN 112537761 A CN112537761 A CN 112537761A CN 202011281053 A CN202011281053 A CN 202011281053A CN 112537761 A CN112537761 A CN 112537761A
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- lifting pipe
- ammoniation reactor
- gas ammonia
- external loop
- ammonia
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- 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
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- 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
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Abstract
The invention discloses an external circulation ammoniation reactor. The reactor comprises a sedimentation separator, a stirring device, a lifting pipe, a return pipe, a circulating pump and two ammonia gas 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 have the same eccentricity e as the circle center of the lifting pipe positioned 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 settling separator. The invention adopts the relatively eccentric gas ammonia nozzle arrangement which is vertical to the riser of the reactor, so that gas ammonia forms rotational flow after entering the settling separator, the viscosity of slurry is reduced, and the blockage problem is improved.
Description
Technical Field
The invention relates to the technical field of phosphorus ammonia production, in particular to an external circulation ammoniation reactor.
Background
The industrial monoammonium phosphate is widely applied to the industries of flame retardants, fire extinguishing agents, flame retardance of textiles, paper making processing and the like, and has large market demand. The production of phosphoric acid mainly comprises 2 processes of a hot method and a wet method, the hot method phosphoric acid is gradually eliminated due to large pollution and high cost, and the production of ammonium phosphate by the wet method phosphoric acid becomes an inevitable trend of industrial development. The external circulation ammoniation reactor has the advantages of no internal parts, uniform material mixing, violent turbulence, high bubble dispersion degree, large mass transfer area and the like, and is key equipment for producing ammonium phosphate by a wet method. Along with the increase of production load, the quality of phosphorite is reduced, the impurity content is increased, the viscosity of slurry is increased, the fluidity is deteriorated, the slurry is easy to scale and block an air inlet hole of a gas distributor, the reaction of phosphoric acid and ammonia is insufficient, the ammonia escape rate is high, and the yield of phosphorus and ammonia is low. The ammonia gas escapes to cause resource waste and environmental pollution. Therefore, the industry of phosphorus and ammonia is still in the development level of high investment, high pollution, high consumption, low output and low benefit, and the development is changed by the cost of large consumption of phosphorus resources, ecological damage and environmental pollution. The key factor determining the production efficiency of the external loop 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 increased. 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 bubble collapse and increase the frequency of surface renewal of 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 from blocking a pipeline and an air inlet, and becomes a problem to be solved urgently in the current ammonium phosphate industry.
Disclosure of Invention
The present invention addresses the above-described deficiencies of the prior art by providing an external loop ammoniation reactor which has improved mass transfer reaction efficiency and which also ameliorates the problem of slurry plugging in piping and gas inlets.
An external circulation ammoniation reactor comprises a sedimentation separator, a stirring device, a lifting pipe, a return pipe, a circulating pump and two gas ammonia nozzles;
the settling separator is provided with a circulating inlet and a circulating outlet which are communicated with the interior of the settling separator, one end of the return pipe is communicated with a 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 a liquid outlet of the circulating pump, and the other end of the lifting pipe is communicated with the circulating inlet; the top of the settling separator is provided with a steam outlet, and the bottom of the settling separator is provided with a slurry outlet and a slag discharge port;
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 have the same eccentricity e as the circle center of the lifting pipe positioned 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 0.20.3 times the riser diameter D.
Furthermore, the inner wall of the riser is provided with a flow guide spiral sheet which extends and spirals along the axial direction of the riser.
Further, the pitch H of the guide spiral sheet is 0.10.2 times of the diameter D of the riser.
Further, the thickness S of the flow guiding spiral sheet is 0.20.3 times of the screw pitch H, and the width W of the flow guiding spiral sheet is 12 times of the thickness S.
Further, the phosphoric acid inlet is positioned below the two gas ammonia nozzles.
Furthermore, the pipeline of the lifting pipe between the gas ammonia nozzle and the circulating pump 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 vertical setting of rotation axis is in among the sedimentation separator, it is a plurality of the blade is installed around the rotation axis bottom, the top of rotation axis stretches out sedimentation separator with the driving piece transmission is connected, the driving piece drive the rotation axis drives the blade is rotatory.
A method for producing ammonium phosphate uses the external circulation ammoniation reactor.
The invention adopts the nozzle arrangement which is relatively eccentric and vertical to the riser of the reactor, so that gas ammonia enters a settling separator to form rotational flow, the air injection directions of two gas ammonia nozzles and the circle center of the riser on the plane have the same eccentricity e, the eccentricity is increased, slurry speed around the nozzles is obviously layered under the action of the tangential speed of ammonia bubbles, the speed gradient is increased to form rotational flow, 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 surfaces of the bubbles is increased, 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 destroying the flocculation network structure of the slurry, reducing the viscosity of the slurry and improving the blockage problem; the nozzle is perpendicular to the lifting pipe, so that the slurry is not easy to block the air inlet, the mass transfer reaction efficiency is improved, and the problem that the slurry blocks the pipeline and the air inlet is solved.
The slurry of the sedimentation separator generates forced rotational flow under the action of the stirring device, flocculent solid particles are crushed and are subjected to sedimentation separation and discharged from a bottom slag discharge port, the problem that the slurry blocks a pipeline is greatly solved, the mixed reaction is more uniform, the slurry is output to the next step at the lower end of the sedimentation separator, part of unreacted clear liquid is conveyed to the lifting pipe from a circulating outlet above the sedimentation separator to react again, and the yield of ammonium phosphate is improved.
Drawings
FIG. 1 is a schematic view of an external loop ammoniation reactor according to the present invention;
FIG. 2 is an enlarged view at B in FIG. 1;
figure 3 is a schematic diagram of a gas ammonia nozzle of an external loop ammoniation reactor according to the present invention.
1. A settling separator; 11. a circulation inlet; 12. a recycle outlet; 13. a steam outlet; 14. a slurry outlet; 15. a slag discharge port; 2. a stirring device; 21. a drive member; 22. a rotating shaft; 23. a blade; 3. a riser tube; 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 adjusting the valve.
Detailed Description
The following are specific embodiments of the present invention and are further described with reference to the drawings, but the present invention is not limited to these embodiments.
As shown in fig. 1, the external circulation ammoniation reactor of the present invention comprises a sedimentation separator 1, a stirring device 2, a riser 3, a return pipe 4, a circulation pump 5 and two gas ammonia nozzles 6;
the sedimentation separator 1 is provided with a circulation inlet 11 and a circulation outlet 12 which are communicated with the interior of the sedimentation separator, one end of a return pipe 4 is communicated with a liquid inlet of a circulation pump 5, the other end of the return pipe is communicated with the circulation outlet 12, one end of a lifting pipe 3 is communicated with a liquid outlet of the circulation pump 5, and the other end of the lifting pipe is communicated with the circulation inlet 11; the top of the settling separator 1 is provided with a steam outlet 13, and the bottom is provided with a slurry outlet 14 and a slag discharge port 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 have the same eccentricity e as the circle center of the lifting pipe 3 positioned 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.
The invention adopts the nozzle arrangement which is relatively eccentric and vertical to the riser 3 of the reactor, so that gas ammonia enters the sedimentation separator 1 to form rotational flow, the air injection directions of the two gas ammonia nozzles 6 have the same eccentricity e as the circle center of the riser 3 on the plane, the eccentricity is increased, the slurry speed around the nozzles is obviously layered under the action of the tangential speed of ammonia bubbles, the speed gradient is increased to form rotational flow, the gas-liquid turbulence is enhanced, the bubble particle size 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 the ammonia and phosphoric acid solution is improved, and the ammonia loss is reduced; meanwhile, turbulence and shear force enhancement are also beneficial to destroying the flocculation network structure of the slurry, reducing the viscosity of the slurry and improving the blockage problem; the nozzle is arranged perpendicular to the lifting pipe 3, so that the slurry is not easy to block the air inlet, and therefore, the mass transfer reaction efficiency is improved, and the problem that the pipeline and the air inlet are blocked by the slurry is also solved.
The slurry of the sedimentation separator 1 generates forced rotational flow under the action of the stirring device 2, flocculent solid particles are crushed and are subjected to sedimentation separation, the slurry is discharged from a bottom slag discharge port 15, the problem that the slurry blocks a pipeline is greatly solved, the mixed reaction is more uniform, the slurry is output to the next step at the lower end of the sedimentation separator 1, part of unreacted clear liquid is conveyed to the lifting pipe 3 from a circulating outlet 12 above the sedimentation separator 1 to react again, and the yield of ammonium phosphate is improved.
As shown in fig. 3, the eccentricity e may be 0.20.3 times of the diameter D of the riser tube 3, and if the eccentricity is too small, the effect of strengthening the swirling flow is weak; the eccentricity is too large, the processing and 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 flow guide spiral sheet 7 which extends and spirals along the axial direction of the lifting pipe to strengthen the rotational flow, so that the turbulent strength of gas and liquid is greatly increased, large bubbles are broken into small bubbles under the action of the strong shearing force of a flow field, and the specific surface area of the bubbles is increased; the rotating fluid can also enhance the mutual mixing of the fluids, the entrainment capacity and the mixing action of the fluid are larger than those of a non-rotational flow, the mass transfer coefficient is improved, the reaction of phosphoric acid solution and ammonia gas is more sufficient, and the ammonia escape rate is reduced. Under the action of strong turbulence, the flocculation network structure of the slurry is broken up by the shearing force of the fluid, the viscosity is reduced, and the probability of pipeline blockage by the slurry is greatly reduced;
as shown in fig. 2, the pitch H of the guide vanes 7 may be 0.10.2 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 fixed, the number of turns is increased, the screw pitch is reduced, the rotation degree of fluid is increased, entrainment and mixing of surrounding fluid are enhanced, the shearing force of the fluid is increased, the average particle size of bubbles is reduced, and the gas-liquid mass transfer reaction is strengthened. The ammonia gas bubble is spiral lift along riser 3, and when no water conservancy diversion flight 7, the axial length that a spiral cycle change was accomplished to the bubble is 3D, sets up pitch H for 0.10.2 times of riser 3 diameter D to reduce the axial length that spiral cycle change was accomplished to the bubble, improve fluidic whirl and turbulent intensity, reduce the bubble particle diameter.
The thickness S of the flow guiding spiral sheet 7 may be 0.20.3 times the pitch H, and the width W of the flow guiding spiral sheet 7 may be 12 times the thickness S. The thickness of the flow guide 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 bubbles in slurry is reduced, the residence time of the ammonia bubbles is increased, and the reaction is more sufficient; on the other hand, the diversion spiral sheet 7 is thickened, so that the speed gradient of the liquid slurry around the diversion spiral sheet is increased, the disturbance on fluid micelles is increased, the turbulence intensity is increased, the shearing force on bubbles is increased, the large bubbles are broken, the mixing is enhanced, the reaction is more sufficient, and the escape of ammonia is reduced. The thickness of the spiral sheet cannot be too large, and a flow dead zone is avoided.
The width of the flow guide 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 falling of symmetrical vortexes and the transition of a bubble path from spiral to zigzag movement are inhibited, so that the retention time of the bubbles is prolonged, and the mass transfer and reaction are enhanced. An excessively large width of the flight increases the flow resistance and reduces the distribution of bubbles near the wall surface. The width W of the spiral sheet can be 1S-2S, and S is the thickness of the spiral sheet.
The outlet flow of the steam outlet 13 is measured by a flowmeter, the mass fraction of ammonia at the steam outlet 13 is measured by adopting a nano-grade reagent spectrophotometry, 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 retention time of bubbles are improved, the yield of ammonium phosphate is finally improved, and the ammonia loss is reduced.
The phosphoric acid inlet 31 may be located below the two gas ammonia nozzles 6. The phosphoric acid inlet 31 is arranged below the gas ammonia nozzle 6, under the power drive of the circulating pump 5, the phosphoric acid is mixed with ammonia bubbles under the action of strong turbulent kinetic energy, a large amount of heat is released, the turbulent flow and mixing are further enhanced, the reaction is more sufficient, the ammonia escape rate is reduced,
the pipeline of the lifting pipe 3 between the gas ammonia nozzle 6 and the circulating pump 5 can be also provided with an adjusting valve 8, the equivalent diameter of the lifting pipe is changed, 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 together regulate the circulating liquid speed in the riser tube, so that the rising speed and the turbulence intensity of the ammonia bubbles in the riser tube are changed. 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 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 structure of the stirring device 2 is various, and is not limited herein, in this embodiment, the stirring device 2 may include a driving member 21, a rotating shaft 22, and a plurality of blades 23, the rotating shaft 22 is vertically disposed in the sedimentation separator 1, the plurality of blades 23 are installed around the bottom end of the rotating shaft 22, the top end of the rotating 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 rotating shaft 22 to drive the blades 23 to rotate. The driving part 21 can be a motor, and the rotating speed of the motor can be adjusted, so that the rotating speeds of the rotating shaft 22 and 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 dispersed, the viscosity is further reduced, the diffusion coefficient of turbulence is improved, and the slurry is mixed more uniformly; the insufficiently reacted ammonia gas escaping from the recycling outlet 12 is broken into small bubbles under the action of strong swirling shear, and continues to react with the phosphoric acid in the sedimentation separator 1. Fe, Ca, Mg, Al, SiO in wet-process phosphoric acid2、S04 2-Impurities such as F and the like can generate insoluble substances in the ammonia neutralization processSolid impurity particles which are settled along the settling separator 1 under the action of the centrifugal force of the forced rotational flow and can be discharged from the slag discharge port 15, and cleaner slurry is output from the slurry outlet 14 to the next process. The supernatant liquid is output from the circulating outlet 12 and flows through the bottom return pipe 4 to enter the riser pipe 3 for re-reaction.
A method for producing ammonium phosphate uses the external loop flow ammoniation reactor, wherein the mass fraction of ammonia at the steam outlet 13 is measured by a flowmeter and the mass fraction of ammonia at the steam outlet 13 is measured by a nano-grade reagent spectrophotometry, and the ammonia slip amount can be obtained through calculation, if the ammonia slip amount exceeds the standard, the eccentricity e can be properly increased, the thickness and the width of the diversion spiral piece 7 can be increased, and the screw pitch of the diversion spiral piece 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 illustration, it will be understood by those skilled in the art that the foregoing is illustrative only and is not limiting of the scope of the invention, as various modifications or additions may be made to the specific embodiments described and substituted in a similar manner by those skilled in the art without departing from the scope of the invention as defined in the appending claims. It should be understood by those skilled in the art that any modifications, equivalents, improvements and the like made to the above embodiments in accordance with the technical spirit of the present invention are included in the scope of the present invention.
Claims (10)
1. An external loop ammoniation reactor, 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 circulation inlet (11) and a circulation outlet (12) which are communicated with the interior of the sedimentation separator, one end of the return pipe (4) is communicated with a liquid inlet of the circulation pump (5), the other end of the return pipe is communicated with the circulation outlet (12), one end of the lifting pipe (3) is communicated with a liquid outlet of the circulation pump (5), and the other end of the lifting pipe is communicated with the circulation inlet (11); the top of the settling separator (1) is provided with a steam outlet (13), and the bottom of the settling separator is provided with a slurry outlet (14) and a slag discharge port (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 eccentricity 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).
2. An external loop ammoniation reactor as claimed in claim 1, wherein: the eccentricity e is 0.20.3 times of the diameter D of the riser (3).
3. An external loop ammoniation reactor as claimed in claim 2, wherein: and a flow guide spiral sheet (7) which extends and spirals along the axial direction of the lifting pipe (3) is arranged on the inner wall of the lifting pipe.
4. An external loop ammoniation reactor as claimed in claim 3, wherein: the pitch H of the diversion spiral sheet (7) is 0.10.2 times of the diameter D of the riser (3).
5. An external loop ammoniation reactor as claimed in claim 4 wherein: the thickness S of the flow guiding spiral sheet (7) is 0.20.3 times of the screw pitch H, and the width W of the flow guiding spiral sheet (7) is 12 times of the thickness S.
6. An external loop ammoniation reactor as claimed in claim 1, wherein: the phosphoric acid inlet (31) is positioned below the two gas ammonia nozzles (6).
7. An external loop ammoniation reactor as claimed in claim 1, wherein: the lifting pipe (3) is also provided with a regulating valve (8) on a pipeline between the gas ammonia nozzle (6) and the circulating pump (5).
8. An external loop ammoniation reactor as claimed in claim 1, wherein: the circulation inlet (11) is located below the circulation outlet (12).
9. An external loop ammoniation reactor as claimed in claim 1, wherein: agitating unit (2) are including driving piece (21), rotation axis (22) and a plurality of blade (23), rotation axis (22) vertical setting is in sedimentation separator (1), it is a plurality of blade (23) are installed around rotation axis (22) bottom, the top of rotation axis (22) is stretched out sedimentation separator (1) with driving piece (21) transmission is connected, driving piece (21) drive rotation axis (22) drive blade (23) are rotatory.
10. A method for producing ammonium phosphate is characterized in that: use of an external loop flow ammoniation reactor as claimed in any one of claims 1 to 9.
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| 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 |
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| Application Number | Priority Date | Filing Date | Title |
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| CN202011281053.7A CN112537761B (en) | 2020-11-16 | 2020-11-16 | External circulation ammonification reactor and ammonium phosphate production method |
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| CN112537761A true CN112537761A (en) | 2021-03-23 |
| CN112537761B CN112537761B (en) | 2023-06-02 |
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Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103551087A (en) * | 2013-11-08 | 2014-02-05 | 神马实业股份有限公司 | Ammoximation reaction system for preparing cyclohexanone-oxime |
| CN103773441A (en) * | 2012-10-24 | 2014-05-07 | 中国石油化工股份有限公司 | Boiling bed liquid phase hydrogenation treatment method |
| 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 |
| CN106216126A (en) * | 2016-09-11 | 2016-12-14 | 中国计量大学 | It is applicable to the effervescent atomizer of shear shinning non-Newtonian fluid |
-
2020
- 2020-11-16 CN CN202011281053.7A patent/CN112537761B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103773441A (en) * | 2012-10-24 | 2014-05-07 | 中国石油化工股份有限公司 | Boiling bed liquid phase hydrogenation treatment method |
| CN103551087A (en) * | 2013-11-08 | 2014-02-05 | 神马实业股份有限公司 | Ammoximation reaction system for preparing 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 |
| CN106216126A (en) * | 2016-09-11 | 2016-12-14 | 中国计量大学 | It is applicable to the effervescent atomizer of shear shinning non-Newtonian fluid |
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