CN114392586B - Device and method for manufacturing oligomeric phosphate water-soluble fertilizer - Google Patents
Device and method for manufacturing oligomeric phosphate water-soluble fertilizer Download PDFInfo
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- CN114392586B CN114392586B CN202210036562.6A CN202210036562A CN114392586B CN 114392586 B CN114392586 B CN 114392586B CN 202210036562 A CN202210036562 A CN 202210036562A CN 114392586 B CN114392586 B CN 114392586B
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- soluble fertilizer
- air pressure
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- 238000000034 method Methods 0.000 title claims abstract description 45
- 239000003337 fertilizer Substances 0.000 title claims abstract description 40
- 229910019142 PO4 Inorganic materials 0.000 title claims abstract description 30
- NBIIXXVUZAFLBC-UHFFFAOYSA-K phosphate Chemical compound [O-]P([O-])([O-])=O NBIIXXVUZAFLBC-UHFFFAOYSA-K 0.000 title claims abstract description 30
- 239000010452 phosphate Substances 0.000 title claims abstract description 30
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 26
- 238000006243 chemical reaction Methods 0.000 claims abstract description 159
- 239000006260 foam Substances 0.000 claims abstract description 58
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 claims description 114
- 229910000147 aluminium phosphate Inorganic materials 0.000 claims description 57
- 239000007788 liquid Substances 0.000 claims description 31
- XSQUKJJJFZCRTK-UHFFFAOYSA-N Urea Chemical compound NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 claims description 24
- 239000004202 carbamide Substances 0.000 claims description 24
- 230000008859 change Effects 0.000 claims description 24
- 238000010438 heat treatment Methods 0.000 claims description 15
- 238000003860 storage Methods 0.000 claims description 15
- 238000001704 evaporation Methods 0.000 claims description 14
- 230000008020 evaporation Effects 0.000 claims description 13
- 238000007738 vacuum evaporation Methods 0.000 claims description 10
- 238000002156 mixing Methods 0.000 claims description 7
- 229920002842 oligophosphate Polymers 0.000 claims description 6
- UNXRWKVEANCORM-UHFFFAOYSA-N triphosphoric acid Polymers OP(O)(=O)OP(O)(=O)OP(O)(O)=O UNXRWKVEANCORM-UHFFFAOYSA-N 0.000 claims description 6
- 239000011148 porous material Substances 0.000 claims 1
- 230000002349 favourable effect Effects 0.000 abstract description 12
- 239000000243 solution Substances 0.000 description 99
- 239000007789 gas Substances 0.000 description 65
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 38
- 239000002253 acid Substances 0.000 description 22
- 229910021529 ammonia Inorganic materials 0.000 description 17
- 238000004891 communication Methods 0.000 description 16
- 238000006116 polymerization reaction Methods 0.000 description 10
- 230000009286 beneficial effect Effects 0.000 description 9
- 230000008569 process Effects 0.000 description 9
- 239000011324 bead Substances 0.000 description 8
- 230000006870 function Effects 0.000 description 8
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 8
- 238000005265 energy consumption Methods 0.000 description 7
- 238000010586 diagram Methods 0.000 description 6
- 238000009835 boiling Methods 0.000 description 5
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 4
- 238000004590 computer program Methods 0.000 description 4
- 238000009833 condensation Methods 0.000 description 4
- 230000005494 condensation Effects 0.000 description 4
- 230000008030 elimination Effects 0.000 description 4
- 238000003379 elimination reaction Methods 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- 239000000047 product Substances 0.000 description 4
- 230000005540 biological transmission Effects 0.000 description 3
- 239000000919 ceramic Substances 0.000 description 3
- 230000008878 coupling Effects 0.000 description 3
- 238000010168 coupling process Methods 0.000 description 3
- 238000005859 coupling reaction Methods 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 238000012545 processing Methods 0.000 description 3
- 230000009467 reduction Effects 0.000 description 3
- 230000000630 rising effect Effects 0.000 description 3
- 239000002893 slag Substances 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 230000009471 action Effects 0.000 description 2
- MXZRMHIULZDAKC-UHFFFAOYSA-L ammonium magnesium phosphate Chemical compound [NH4+].[Mg+2].[O-]P([O-])([O-])=O MXZRMHIULZDAKC-UHFFFAOYSA-L 0.000 description 2
- 238000002485 combustion reaction Methods 0.000 description 2
- 230000007797 corrosion Effects 0.000 description 2
- 238000005260 corrosion Methods 0.000 description 2
- 238000005187 foaming Methods 0.000 description 2
- 239000011259 mixed solution Substances 0.000 description 2
- 238000007711 solidification Methods 0.000 description 2
- 230000008023 solidification Effects 0.000 description 2
- 229910052567 struvite Inorganic materials 0.000 description 2
- 230000001360 synchronised effect Effects 0.000 description 2
- 238000012546 transfer Methods 0.000 description 2
- 206010020880 Hypertrophy Diseases 0.000 description 1
- 229910000831 Steel Inorganic materials 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000001419 dependent effect Effects 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 239000000178 monomer Substances 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 229910000069 nitrogen hydride Inorganic materials 0.000 description 1
- 230000003287 optical effect Effects 0.000 description 1
- 230000000149 penetrating effect Effects 0.000 description 1
- 150000003013 phosphoric acid derivatives Chemical class 0.000 description 1
- 230000000379 polymerizing effect Effects 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
Classifications
-
- 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
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D19/00—Degasification of liquids
- B01D19/0042—Degasification of liquids modifying the liquid flow
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D19/00—Degasification of liquids
- B01D19/02—Foam dispersion or prevention
-
- 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
- B01J19/0006—Controlling or regulating processes
-
- 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
- B01J19/0053—Details of the reactor
-
- C—CHEMISTRY; METALLURGY
- C05—FERTILISERS; MANUFACTURE THEREOF
- C05B—PHOSPHATIC FERTILISERS
- C05B17/00—Other phosphatic fertilisers, e.g. soft rock phosphates, bone meal
Abstract
The application relates to fertilizer production technical field discloses a device for making oligomeric phosphate water-soluble fertilizer, include: a reaction tank, a microporous gas collection assembly and a defoaming assembly. The reaction tank is used for placing a solution; the microporous gas collecting component is arranged in the reaction tank, and part of the microporous gas collecting component can be immersed in the solution in the reaction tank; the defoaming component is rotatably arranged in the reaction tank and is positioned on the upper side of the solution surface and used for eliminating foam generated by solution reaction. In this application, can collect the gas that releases after breaking up the bubble through micropore gas collection subassembly, reduce the bubble volume in the solution, eliminate the foam of solution level upside through defoaming subassembly simultaneously to through eliminating the bubble in the solution and the bubble of solution level upside, be favorable to reducing bubble content, improve output. The application also discloses a method for manufacturing the oligomeric phosphate water-soluble fertilizer.
Description
Technical Field
The application relates to the technical field of fertilizer production, for example to a device and a method for manufacturing an oligomeric phosphate water-soluble fertilizer.
Background
At present, along with the growth of population, the demand for grains is also higher and the planting land is gradually reduced, so that the demand for grains is met, the development of fertilizer is indispensable, the phosphate water-soluble fertilizer is a relatively efficient fertilizer at present, and the condensation method of phosphoric acid and urea is mainly adopted in the production of phosphate water-soluble hypertrophy.
In the related art, the specific synthesis process of the condensation method of phosphoric acid and urea is as follows: adding phosphoric acid and urea with certain mass ratio into a reaction kettle, mixing and dissolving in the kettle, then entering a boiling bed for boiling polymerization, adjusting ammonia discharge amount after foaming materials, keeping ammonia pressure in the boiling bed, polymerizing and solidifying the materials along with the rising of temperature, continuously controlling temperature and pressure, preserving heat, finally cooling and discharging to obtain a crisp white product, and finally crushing to obtain a finished product, wherein urea is adopted as a condensing agent by a condensation method of phosphoric acid and urea, and a large amount of NH3 and CO2 gases can be discharged in a short time under high temperature, so that a large amount of foaming materials are extremely easy to overflow in the reaction process, and the monomer volume yield of the reactor is too low.
Therefore, how to reduce foam and improve yield in the production process of phosphate water-soluble fertilizer becomes a technical problem to be solved by the technicians in the field.
Disclosure of Invention
The following presents a simplified summary in order to provide a basic understanding of some aspects of the disclosed embodiments. This summary is not an extensive overview, and is intended to neither identify key/critical elements nor delineate the scope of such embodiments, but is intended as a prelude to the more detailed description that follows.
The embodiment of the disclosure provides a device and a method for manufacturing an oligomeric phosphate water-soluble fertilizer, which are used for solving the technical problems of reducing foam and improving yield in the production process of the phosphate water-soluble fertilizer.
In some embodiments, an apparatus for making an oligomeric phosphate water-soluble fertilizer comprises: a reaction tank, a microporous gas collection assembly and a defoaming assembly. The reaction tank is used for placing a solution; the microporous gas collecting component is arranged in the reaction tank, and part of the microporous gas collecting component can be immersed in the solution in the reaction tank; the defoaming component is rotatably arranged in the reaction tank and is positioned on the upper side of the solution surface and used for eliminating foam generated by solution reaction.
In some embodiments, a method for making an oligomeric phosphate water-soluble fertilizer comprises:
heating the reaction tank to enable the concentrated phosphoric acid to react with urea in a mixing way;
acquiring the temperature in the reaction tank, and controlling the rotating speed of the defoaming component according to the temperature in the reaction tank;
And acquiring the air pressure in the reaction tank, and controlling the exhaust speed according to the air pressure in the reaction tank.
The device and the method for manufacturing the oligomeric phosphate water-soluble fertilizer provided by the embodiment of the disclosure can realize the following technical effects:
the solution is placed in the reaction tank to enable the solution to be fully dissolved and reacted in the reaction tank, the solution can be foamed in the reaction tank, part of bubbles can exist in the solution, and the rest of bubbles can exist on the upper side of the solution level, so that the microporous gas collecting component arranged in the reaction tank can fully contact with the bubbles in the solution through the part immersed in the solution in the reaction tank to enable the bubbles to be cracked and release gas, and the released gas after the bubbles are cracked can enter the microporous gas collecting component to be collected, so that the bubble quantity in the solution is reduced, and meanwhile, the defoaming component arranged in the reaction tank is rotated to be contacted with the rest of bubbles on the upper side of the solution level to enable the bubbles on the upper side of the solution level to be cracked, so that bubbles on the upper side of the solution level are eliminated, the bubble content is reduced, and the yield is improved.
The foregoing general description and the following description are exemplary and explanatory only and are not restrictive of the application.
Drawings
One or more embodiments are illustrated by way of example and not limitation in the figures of the accompanying drawings, in which like references indicate similar elements, and in which like reference numerals refer to similar elements, and in which:
FIG. 1 is a schematic cross-sectional view of an apparatus for producing an oligomeric phosphate water-soluble fertilizer according to an embodiment of the present disclosure;
FIG. 2 is a schematic view of the external structure of an apparatus for producing an oligomeric phosphate water-soluble fertilizer provided in an embodiment of the present disclosure;
FIG. 3 is a schematic structural view of a microporous gas collection assembly and a defoaming assembly provided by embodiments of the present disclosure;
FIG. 4 is a schematic view of a configuration of a centralized collection portion provided by an embodiment of the present disclosure;
FIG. 5 is a schematic view of a drive device provided by an embodiment of the present disclosure;
FIG. 6 is a schematic view of the structure of a hollow spike provided in an embodiment of the present disclosure;
FIG. 7 is a schematic view of the hollow spike from another perspective provided by embodiments of the present disclosure;
FIG. 8 is a schematic diagram of a phosphoric acid concentration assembly provided in an embodiment of the present disclosure;
FIG. 9 is a schematic illustration of a method for making an oligomeric phosphate water-soluble fertilizer provided in an embodiment of the present disclosure;
Fig. 10 is a schematic view of an apparatus for producing an oligomeric phosphate water-soluble fertilizer provided in an embodiment of the present disclosure.
Reference numerals:
100. a processor (processor); 101. a memory (memory); 102. a communication interface (Communication Interface); 103. a bus; 200. a reaction tank; 300. a microporous gas collection assembly; 301. a microporous suction part; 302. a centralized collection unit; 303. micropores; 304. a first collection tube; 305. a second collection tube; 306. a centralized collecting pipe; 400. a defoaming assembly; 401. a rotating bracket; 402. a hollow spike; 403. a rotating shaft; 404. a driving device; 405. a transmission gear; 406. a drive gear; 407. a driving motor; 408. an open slot; 500. a phosphoric acid concentration assembly; 501. a first stage concentrating structure; 502. a second stage concentrating structure; 503. and a third stage of concentration structure.
Detailed Description
So that the manner in which the features and techniques of the disclosed embodiments can be understood in more detail, a more particular description of the embodiments of the disclosure, briefly summarized below, may be had by reference to the appended drawings, which are not intended to be limiting of the embodiments of the disclosure. In the following description of the technology, for purposes of explanation, numerous details are set forth in order to provide a thorough understanding of the disclosed embodiments. However, one or more embodiments may still be practiced without these details. In other instances, well-known structures and devices may be shown simplified in order to simplify the drawing.
The terms first, second and the like in the description and in the claims of the embodiments of the disclosure and in the above-described figures are used for distinguishing between similar objects and not necessarily for describing a particular sequential or chronological order. It is to be understood that the data so used may be interchanged where appropriate in order to describe embodiments of the present disclosure. Furthermore, the terms "comprise" and "have," as well as any variations thereof, are intended to cover a non-exclusive inclusion.
The term "plurality" means two or more, unless otherwise indicated.
In the embodiment of the present disclosure, the character "/" indicates that the front and rear objects are an or relationship. For example, A/B represents: a or B.
The term "and/or" is an associative relationship that describes an object, meaning that there may be three relationships. For example, a and/or B, represent: a or B, or, A and B.
The term "corresponding" may refer to an association or binding relationship, and the correspondence between a and B refers to an association or binding relationship between a and B.
In the embodiment of the disclosure, the intelligent home appliance refers to a home appliance formed after a microprocessor, a sensor technology and a network communication technology are introduced into the home appliance, and has the characteristics of intelligent control, intelligent sensing and intelligent application, the operation process of the intelligent home appliance often depends on the application and processing of modern technologies such as the internet of things, the internet and an electronic chip, for example, the intelligent home appliance can realize remote control and management of a user on the intelligent home appliance by connecting the electronic appliance.
In the disclosed embodiment, the terminal device refers to an electronic device with a wireless connection function, and the terminal device can be in communication connection with the intelligent household electrical appliance through connecting with the internet, or can be in communication connection with the intelligent household electrical appliance through Bluetooth, wifi and other modes. In some embodiments, the terminal device is, for example, a mobile device, a computer, or an in-vehicle device built into a hover vehicle, etc., or any combination thereof. The mobile device may include, for example, a cell phone, smart home device, wearable device, smart mobile device, virtual reality device, etc., or any combination thereof, wherein the wearable device includes, for example: smart watches, smart bracelets, pedometers, etc.
Referring to fig. 1-7, an embodiment of the present disclosure provides an apparatus for producing an oligomeric phosphate water-soluble fertilizer, comprising: a reaction tank 200, a microporous gas collection assembly 300, and a defoaming assembly 400. The reaction tank 200 is used for placing a solution; the microporous gas collection assembly 300 is disposed in the reaction tank 200 and may be partially immersed in the solution in the reaction tank 200; the defoaming assembly 400 is rotatably disposed in the reaction tank 200 above the solution surface for eliminating foam generated by the solution reaction.
By adopting the device for manufacturing the water-soluble fertilizer of the oligomeric phosphate salt, provided by the embodiment of the disclosure, the solution can be fully dissolved and reacted in the reaction tank 200 by placing the solution in the reaction tank 200, part of bubbles can be foamed in the solution in the reaction process in the reaction tank 200, and the rest of bubbles can be in the upper side of the solution surface, so that the microporous gas collecting assembly 300 arranged in the reaction tank 200 can fully contact with the bubbles in the solution through the part immersed in the solution in the reaction tank 200 to enable the bubbles to be cracked and release gas, and the released gas after the bubbles are cracked can enter the microporous gas collecting assembly 300 to be collected, so that the reduction of the amount of the bubbles in the solution is facilitated, and meanwhile, the defoaming assembly 400 arranged in the reaction tank 200 is rotated to be contacted with the rest of the bubbles on the upper side of the solution surface to crack the bubbles on the upper side of the solution surface, so that the bubbles on the upper side of the solution surface are eliminated, the bubbles in the solution and the bubbles on the upper side of the solution surface are eliminated, so that the content of the bubbles in the solution and the bubbles on the upper side of the solution are reduced are facilitated, and the yield is improved.
Optionally, the microporous gas collection assembly 300 includes: a microporous getter portion 301 and a centralized collection portion 302. The micropore suction part 301 is of a cylindrical structure with one end closed and the other end open, the side wall is provided with micropores 303 communicated with the hollow area inside, the aperture of each micropore 303 can allow gas to pass through, and the micropore suction part 301 is provided with a plurality of micropores; the collective collection portion 302 communicates with the open ends of the plurality of microporous suction portions 301. Thus, when the microporous suction part 301 is immersed in the solution, the side wall of the microporous suction part 301 contacts and rubs with bubbles in the solution, so that the bubbles are broken, gas released after the bubbles are broken enters a hollow area inside the microporous suction part 301 through micropores 303 on the side wall of the microporous suction part 301, flows to one end of an opening of the microporous suction part along the hollow area of the microporous suction part 301, and flows into the centralized collecting part 302 through the opening end of the microporous suction part 301, thereby realizing the collection of the gas generated by the bubbles in the solution due to the breakage, reducing the content of the bubbles generated by the solution in the reaction process, and being beneficial to improving the yield; meanwhile, the plurality of micropore air suction parts 301 are arranged, the concentrated collecting parts 302 are communicated with the open ends of the plurality of micropore air suction parts 301, the micropore air suction parts 301 can be fully contacted with the solution in the reaction tank 200, the coverage range of contact friction between the micropore air suction parts 301 and the bubbles in the solution is improved, further, the bubbles in the solution are fully broken and the gas released after the bubbles are broken is collected, the collecting efficiency of the gas is improved, and the bubble content in the solution is effectively reduced.
Alternatively, the micro holes 303 are provided in plurality, and the plurality of micro holes 303 are uniformly circumferentially provided on the side wall of the micro hole suction part 301. In this way, after the bubbles in the solution are broken by contact friction between the microporous suction part 301 and the bubbles in the solution, the gas released by the broken bubbles can enter the hollow area in the microporous suction part 301 through the micropores 303, and then enter the centralized collection part 302 through the open end for gas collection, which is beneficial to improving the coverage of the microporous suction part 301 for gas collection, further improving the gas collection efficiency and effectively reducing the content of bubbles in the solution.
Alternatively, the micro holes 303 are provided in a circular structure, and protrusions are provided at outer side edges of the micro holes 303. In this way, when the micropore suction part 301 is immersed in the solution in the reaction tank 200, the protrusions at the outer edges of the micropores 303 are firstly in contact with the bubbles to break the bubbles, and then the gas released after the break of the bubbles enters the hollow area in the micropore suction part 301 through the circular micropores 303 to collect, so that the phenomenon that the outer edges of the micropores 303 are too smooth and the bubbles are attached to the outer edges of the micropores 303 and are not broken can be avoided, and the efficiency of breaking the bubbles is improved.
Optionally, the centralized collecting part 302 includes: a first collection tube 304, a second collection tube 305, and a central collection tube 306. The first collecting pipe 304 and the second collecting pipe 305 are arranged in a cross-shaped communication manner, and the bottoms of the first collecting pipe 304 and the second collecting pipe 305 are communicated with the opening end of the micropore suction part 301; the bottom of the concentration tube 306 communicates with the junction of the first and second collection tubes 304, 305, and the top of the concentration tube 306 has an opening. In this way, the first collecting pipe 304 and the second collecting pipe 305 are in cross-shaped communication, and the bottoms of the first collecting pipe 304 and the second collecting pipe 305 are communicated with the opening ends of the micropore suction parts 301, so that the bottom of the first collecting pipe 304 and the bottom of the second collecting pipe 305 are provided with the communication micropore suction parts 301, the coverage area for collecting gas is improved, the gas entering the hollow area inside the micropore suction parts 301 can enter the first collecting pipe 304 and the second collecting pipe 305 through the opening ends thereof to be collected, and the bubble content in the solution is reduced; meanwhile, the gas collected by the first collecting pipe 304 and the second collecting pipe 305 can enter the centralized collecting pipe 306 and be further discharged through the opening at the top of the centralized collecting pipe 306, so that the gas released after the gas bubbles in the solution are broken is collected and discharged, and the content of the gas bubbles in the solution is effectively reduced.
Alternatively, the bottoms of the first collecting pipe 304 and the second collecting pipe 305 are each provided with a plurality of microporous suction portions 301, and each microporous suction portion 301 is spaced apart from each other. In this way, by providing the plurality of microporous suction parts 301 at the bottoms of the first collecting pipe 304 and the second collecting pipe 305, the suction coverage of the microporous suction parts 301 can be improved, the bubble content in the solution can be effectively reduced, and each microporous suction part 301 has a space therebetween, so that when the solution passes through the space, the solution can contact and rub the microporous suction parts 301 at two sides of the space, further the bubbles in the solution are broken and release the gas, and then the gas is collected through the micropores 303 on the microporous suction parts 301, thereby being beneficial to improving the collection efficiency of the gas.
Alternatively, the first collecting pipe 304 and the second collecting pipe 305 are disposed perpendicular to each other, and the concentrated collecting pipe 306 is disposed perpendicular to the junction of the first collecting pipe 304 and the second collecting pipe 305. Thus, the gas which enters the first collecting pipe 304 and the second collecting pipe 305 through the micropore suction part 301 is convenient to enter the centralized collecting pipe 306 smoothly, the smoothness of gas flow is improved, and meanwhile, the two sides of the centralized collecting pipe 306 can be provided with mounting spaces, so that other structures can be mounted conveniently.
Alternatively, the first collecting pipe 304 and the second collecting pipe 305 have the same length, and the axial center of the first collecting pipe 304 and the axial center of the second collecting pipe 305 are disposed in communication with each other. In this way, the lengths of both sides at the axial center of the first collecting pipe 304 and the lengths of both sides at the axial center of the second collecting pipe 305 can be made the same, and when the gas sucked through the microporous suction portion 301 enters into the first collecting pipe 304 and the second collecting pipe 305, the gas can uniformly flow to the concentrated collecting pipe 306, which is advantageous for improving the uniformity of gas collection of the first collecting pipe 304 and the second collecting pipe 305, so that the gas can be kept uniform when flowing inside both.
Optionally, the first collecting pipe 304 and the second collecting pipe 305 are arranged perpendicular to each other, and the concentrated collecting pipe 306 is vertically connected to the connection between the first collecting pipe 304 and the second collecting pipe 305. Thus, after the gas sucked through the microporous suction part 301 enters the first collecting pipe 304 and the second collecting pipe 305, the gas can enter the centralized collecting pipe 306 from the bottom thereof, and then is collected and discharged through the centralized collecting pipe 306, which is beneficial to improving the flow consistency of the gas and improving the efficiency of gas collection.
Alternatively, the microporous getter 301 is entirely made of nano-ceramics. Thus, the nano ceramic has the characteristics of high temperature resistance and the like, the whole structure of the micropore suction part 301 is made of the nano ceramic, so that the micropore suction part 301 is applicable to the high temperature environment in the reaction tank 200, the damage of the micropore suction part 301 caused by the high temperature environment in the reaction tank 200 can be avoided, the service life of the whole structure of the micropore suction part 301 is influenced, the micropore suction part 301 can be immersed in a solution under the high temperature environment in the reaction tank 200, and contacts and rubs with bubbles in the solution to break and release gas, thereby being beneficial to improving the suction efficiency of the micropore suction part 301 and effectively reducing the bubble content in the solution.
Optionally, the defoaming assembly 400 includes: a rotating support 401 and a hollow spike 402. The rotating support 401 is horizontally arranged in the reaction tank 200 and is positioned above the liquid level of the solution; the hollow spike 402 is fixedly arranged on the lower side of the rotary support 401. Thus, the rotary support 401 is horizontally arranged in the reaction tank 200 and is positioned below the liquid level of the solution, and the hollow pricker 402 is arranged on the lower side of the rotary support 401, so that the hollow pricker 402 on the lower side of the rotary support 401 can be driven to rotate when the rotary support 401 rotates, meanwhile, the hollow pricker 402 is fully contacted with the liquid level of the solution, and foam on the liquid level of the solution is pricked in the rotating process, so that the foam is broken, thereby being beneficial to reducing the foam content on the liquid level in the reaction process and improving the yield.
Alternatively, the tip of the concentrated collecting portion 302 passes through the center of the rotating bracket 401. Thus, the concentrated collection tube 306 can be prevented from obstructing the rotation of the rotating holder 401, and the rotating holder 401 can be rotated in order.
Alternatively, the rotary support 401 is provided in a disk-shaped structure, the hollow lancets 402 are provided in plurality, and the plurality of hollow lancets 402 are fixed to the lower side of the rotary support 401 in a ring-shaped array. In this way, the rotating support 401 is provided with a disc-shaped structure, so that the rotating support 401 is convenient to install in the reaction tank 200, and the inner side wall of the reaction tank 200 is prevented from obstructing the rotation of the rotating support 401, so that the rotating support 401 can rotate in the reaction tank 200 better; the hollow needles 402 are fixed on the lower side of the rotary support 401 in an annular array, so that the hollow needles 402 can synchronously rotate along with the rotary support 401, contact friction with foam on the liquid surface of the solution is realized, the foam is broken to release gas, the efficiency of the hollow needles 402 for piercing the foam is improved, and the foam content on the liquid surface of the solution is reduced.
Optionally, a rotating shaft 403 is fixedly connected to the center of the top end surface of the rotating bracket 401, and a driving device 404 is engaged and connected to the top edge of the rotating shaft 403. Like this, drive arrangement 404 is when the operation, can be through driving the pivot 403 rotation of meshing connection with it, and then drive the runing rest 401 with pivot 403 fixed connection and rotate to drive the hollow pjncture needle 402 of runing rest 401 downside and rotate, make hollow pjncture needle 402 puncture the foam on the liquid level of solution at pivoted in-process, be favorable to reducing the foam content on the liquid level of solution, improve output.
Optionally, a through hole is penetrated at the axis of the rotating shaft 403, and the concentrated collecting pipe 306 is located inside the through hole. Thus, through the through hole penetrating through the shaft center of the rotating shaft 403 and arranging the concentrated collecting pipe 306 in the through hole, the rotating shaft 403 can rotate under the driving of the driving device 404, and then the rotating bracket 401 is driven to rotate, the obstruction of the concentrated collecting pipe 306 to the rotation of the rotating shaft 403 can be avoided, and meanwhile, the concentrated collecting pipe 306 can collect the gas in the first collecting pipe 304 and the second collecting pipe 305, so that the gas collecting efficiency is improved.
Optionally, the driving device 404 includes: a transmission gear 405, a drive gear 406 and a drive motor 407. The drive gear 405 is provided at the top edge of the shaft 403; the driving gear 406 is disposed at one side of the rotating shaft 403 and is meshed with the transmission gear 405; the driving motor 407 is fixedly installed on the sidewall of the reaction tank 200, and an output end of the driving motor 407 is fixedly connected with one end of the driving gear 406. Like this, when driving motor 407 is in operation, can drive gear 406 through its output and rotate, and then drive the drive gear 405 who is connected with drive gear 406 meshing and rotate, drive gear 405 can drive pivot 403 and rotate at pivoted in-process to drive rather than fixed connection's runing rest 401 and rotate, realize driving runing rest 401 downside's hollow pjncture needle 402 and rotate, contact the friction repeatedly to the foam on the liquid level of solution, and puncture the foam, be favorable to reducing the foam content on the liquid level of solution, improve output.
Optionally, the tip of the hollow spike 402 is offset to one side and an open slot 408 is provided in the sidewall of the hollow spike 402. In this way, the needle tip of the hollow needle 402 is arranged in a way of shifting to one side, so that the hollow needle 402 can fully contact with the foam on the liquid level of the solution in the process of rotating along with the rotating bracket 401, is inserted from the side face of the foam and breaks the foam, and meanwhile, the hollow needle 402 can be prevented from being directly inserted into the foam, and the foam is prevented from being increased due to the stirring effect on the foam in the rotating process, so that the hollow needle 402 can fully puncture the foam, and the foam content on the liquid level of the solution is reduced; the open slot 408 is arranged on the side wall of the hollow pricker 402, so that when the hollow pricker 402 arranged in an offset way pierces foam, liquid beads generated by foam breakage enter the solution along the open slot 408 under the action of centrifugal force, thereby realizing that the foam content on the liquid level of the solution can be reduced, the loss of the solution can not be caused, and the yield can be improved.
Alternatively, the hollow spike 402 is a hollow structure, and both the tip and the end of the hollow spike 402 have openings. Thus, when the hollow lance 402 pierces the foam, the gas released after the foam breaks flows to the end of the hollow lance 402 along the inner part of the hollow lance 402 and is discharged through the opening of the end, so that the content of the foam on the liquid surface of the solution is reduced, and the efficiency of piercing the foam is improved.
Optionally, the hollow lancet 402 has a smaller opening at its tip than at its distal end. In this way, the hollow puncture needle 402 can be prevented from leading the solution to enter the hollow puncture needle 402 when contacting with the liquid level of the solution in the process of rotating and puncturing the foam, thereby being beneficial to reducing the loss of the solution and improving the yield, and the gas released after the foam is ruptured can enter from the opening at the needle point position of the hollow puncture needle 402 and then be discharged through the opening at the tail end position, so that the puncturing efficiency of the foam is effectively improved, and the foam content on the liquid level of the solution is reduced.
Alternatively, the tip of the hollow spike 402 is disposed to protrude from the top end face of the rotary support 401. In this way, the end of the hollow spike 402 can be located on the top end surface of the rotating bracket 401, and the obstruction of the rotating bracket 401 to the gas discharge inside the hollow spike 402 is avoided, so that the gas inside the hollow spike 402 can be smoothly discharged through the opening at the end.
Optionally, a plurality of open slots 408 are provided, and the plurality of open slots 408 are located on a side wall of the hollow spike 402 facing away from the direction of rotation thereof. In this way, since the small liquid beads are sputtered to the periphery when the foam breaks, a plurality of open slots 408 are arranged on the side wall of the hollow puncture needle 402, and the open slots 408 are all positioned on the side wall of the hollow puncture needle 402 facing away from the rotating direction, so that the sputtered small liquid beads after the foam breaks can flow into the reaction tank 200 along the open slots 408 under the action of centrifugal force; meanwhile, the plurality of open grooves 408 can improve the coverage area of the small liquid beads, so that the small liquid beads smoothly enter the reaction tank 200 through the open grooves 408, and the small liquid beads are prevented from remaining in the hollow pricker 402, thereby being beneficial to reducing the loss of the solution and improving the yield.
Optionally, a plurality of open slots 408 are staggered on the side walls of the hollow spike 402. In this way, the discharge coverage of the open slot 408 for the beads can be increased, avoiding the beads from remaining on the inner sidewall of the hollow spike 402, thereby facilitating the reduction of residue, avoiding excessive loss of solution, and increasing yield.
As shown in conjunction with fig. 8, optionally, the apparatus for producing an oligomeric phosphate water-soluble fertilizer further comprises: phosphoric acid concentration assembly 500. The discharge end of the phosphoric acid concentration assembly 500 is in communication with the reaction tank 200, and the phosphoric acid concentration assembly 500 includes a three-stage concentration structure, wherein the first stage concentration structure 501 and the second stage concentration structure 502 are forced circulation vacuum evaporators and the third stage concentration structure 503 is a direct heating evaporator. In this way, the phosphoric acid is subjected to forced circulation vacuum evaporation concentration through the first-stage concentration structure 501 to reduce the moisture content, then the phosphoric acid subjected to the evaporation concentration through the first-stage concentration structure 501 is subjected to secondary forced circulation vacuum evaporation concentration through the second-stage concentration structure 502 to reduce the moisture content in the phosphoric acid, finally the phosphoric acid subjected to the twice forced circulation vacuum evaporation is subjected to direct heating evaporation through the third-stage concentration structure 503 to further reduce the moisture content in the phosphoric acid and improve the concentration of the phosphoric acid, so that the mutual cooperation of the forced circulation vacuum evaporation and the direct heating evaporation is used for carrying out multistage compression to effectively reduce the moisture content in the phosphoric acid, thereby being beneficial to improving the concentration of the phosphoric acid, meanwhile, the forced circulation vacuum evaporator can reduce the atmospheric pollution and obtain useful byproducts fluosilicic acid, and steam and hot water are used as heat sources, the low-level heat energy of a nearby sulfuric acid device can be fully utilized, the operation is carried out at a lower temperature, the use of steel lining rubber equipment with low price is allowed, the direct heating evaporator is used for concentration in a simple mode, phosphoric acid directly enters from the top of the tower and directly contacts with hot gas from a combustion furnace, the problems of corrosion and scaling caused by indirect heat transfer evaporation can be overcome, the first-stage concentration structure 501 and the second-stage concentration structure 502 are arranged as forced circulation vacuum evaporators, the third-stage concentration structure 503 is arranged as the direct heating evaporator, the excellent characteristics of the forced circulation vacuum evaporators and the direct heating evaporator can be effectively utilized, the energy consumption can be reduced, the equipment damage can be avoided, the concentration of phosphoric acid can be improved, the phosphoric acid after three-stage concentration is discharged into the reaction tank 200, the reaction efficiency and the quality of the solution in the reaction tank 200 can be improved, the yield is improved.
It will be appreciated that, upon concentration in the first stage concentrate structure 501, dilute phosphoric acid (22% P) 2 O 5 ) Metering, adding into a forced circulation vacuum evaporation loop of the concentrating part, mixing with a large amount of heated circulating acid, introducing into an evaporator, evaporating water, and controlling the intermediate acid P 2 And (3) the O5 is 40%, part of concentrated acid is taken as intermediate acid and is sent out from a circulation loop to an intermediate acid clarifying tank by an intermediate acid pump, a large amount of circulating acid is sent into an acid heater by means of a concentration circulation pump, the acid heater is heated by low-pressure steam after temperature and pressure reduction, the circulating is continued in the concentration circulation loop, and steam condensate of the acid heater returns to a desalted water station, so that the desalted water consumption is saved.
After the intermediate acid (40% P2O 5) is settled and separated in an intermediate acid clarifying tank, the bottom slag acid is pumped to a slag acid storage tank by the intermediate acid slag acid and finally is sent to a magnesium ammonium phosphate device to be used as a raw material for producing magnesium ammonium phosphate, the clear acid (40% P2O 5) is pumped to a second-stage concentration structure 502 by the intermediate acid conveying pump, the intermediate acid of 40% P2O5 is concentrated to 55% P2O5, then the intermediate acid which is concentrated to 55% P2O5 by the first-stage concentration structure 501 and the second-stage concentration structure 502 is conveyed to a third-stage concentration structure 503 by the intermediate acid conveying pump to be concentrated to 87% P2O5, and thus the concentrated phosphoric acid with higher purity is obtained.
Like this, can carry out evaporation concentration to phosphoric acid through first order concentrated structure 501 and second level concentrated structure 502, reduce the moisture in the phosphoric acid effectively, be favorable to improving the concentrated purity of phosphoric acid, simultaneously first order concentrated structure 501 and second level concentrated structure 502 can increase the load and the energy consumption of equipment to the concentrated in-process of phosphoric acid evaporation concentration, consequently, after concentrating through first order concentrated structure 501 and second level concentrated structure 502, further carry the concentrated phosphoric acid to third level concentrated structure 503 in evaporation concentration, can utilize the low load and the low energy consumption of the direct heating evaporation of third level concentrated structure 503, make up the high load and the high energy consumption of first order concentrated structure 501 and second level concentrated structure 502, on first order and second level concentrated basis, further improve the concentrated concentration of phosphoric acid through third level concentrated structure 501, second level concentrated structure 502 and third level concentrated structure 503, thereby realize carrying out tertiary concentrated concentration to phosphoric acid, effectively improve output.
As shown in connection with fig. 9, an embodiment of the present disclosure provides a method for manufacturing an oligomeric phosphate water-soluble fertilizer, comprising:
S01, heating the reaction tank to enable the concentrated phosphoric acid to be mixed with urea for reaction;
s02, acquiring the temperature in the reaction tank, and controlling the rotating speed of the defoaming component according to the temperature in the reaction tank;
s03, acquiring the air pressure in the reaction tank, and controlling the exhaust speed according to the air pressure in the reaction tank.
By adopting the method for manufacturing the oligomeric phosphate water-soluble fertilizer, provided by the embodiment of the disclosure, the temperature in the reaction tank can reach a better reaction temperature by controlling the heating of the reaction tank, so that the concentrated phosphoric acid and urea are fully mixed for reaction, and the mixing reaction efficiency of the phosphoric acid and the urea is improved; meanwhile, when the temperature in the reaction tank is high, the mixed solution of phosphoric acid and urea is boiled and foam is generated, and when the temperature in the reaction tank is low, the mixed solution of phosphoric acid and urea is gradually cooled and foam is reduced, so that the temperature in the reaction tank is obtained, the rotating speed of the defoaming component is controlled according to the temperature in the reaction tank, the rotating speed of the defoaming component is controlled to be high when the temperature in the reaction tank is high, the foam on the liquid level of the solution is quickly eliminated, the efficiency of eliminating the foam is improved, and when the temperature in the reaction tank is low, the rotating speed of the defoaming component is controlled to be reduced, the defoaming component is fully contacted with the foam on the liquid level of the solution, the eliminating efficiency of the foam is improved, and therefore the foam content on the liquid level of the solution is reduced, and the yield is improved; and can acquire the atmospheric pressure in the retort to according to the atmospheric pressure control exhaust velocity in the retort, can make its inside atmospheric pressure rise when the temperature in the retort is too high, can improve according to the atmospheric pressure control exhaust velocity in the retort this moment for exhaust velocity, avoid the atmospheric pressure in the retort too high, can make its inside atmospheric pressure reduce when the temperature in the retort is too low, can reduce according to the atmospheric pressure control exhaust velocity in the retort this moment, make the atmospheric pressure in the retort reach the preferred state at the in-process of gradually rising temperature, thereby make the atmospheric pressure in the retort remain in the balanced state of preferred throughout, be favorable to phosphoric acid and urea abundant mixed reaction, improve output.
Optionally, phosphoric acid is mixed with urea in a molar ratio of 1/1.8. Thus, the mixing proportion of phosphoric acid and urea is more reasonable, the urea is less in use amount, incomplete in condensation, low in polymerization degree and low in nitrogen content; the urea consumption is large, the ammonia loss is increased, and the solidification is difficult, so that the molar ratio of phosphoric acid to urea is set to be 1/1.8, the ammonia loss can be reduced, the solidification effect is improved, and the polymerization degree is improved.
It is understood that the temperature in the reaction tank is obtained by a temperature sensor provided in the reaction tank.
Optionally, controlling the rotation speed of the defoaming assembly according to the temperature in the reaction tank includes: the rotation speed of the defoaming component is controlled to be in direct proportion to the temperature in the reaction tank. Like this, because the higher the temperature in the retort, the solution in the retort can be continuous boiling and produce a large amount of foams on the liquid level of solution, consequently control defoaming subassembly's rotational speed and the temperature in the retort are directly proportional, can control defoaming subassembly's rotational speed in the in-process that the temperature in the retort risees and improve to make defoaming subassembly rotate fast and with the foam contact on the liquid level of solution, make a large amount of foams break, reduce foam content, and then be favorable to improving output.
Alternatively, every 1 degree of temperature rise in the reaction tank, the rotational speed of the defoaming assembly is correspondingly increased by 1 revolution per second. Like this, can control the rotational speed of defoaming subassembly and improve along with the temperature in the retort is synchronous, to the solution in the retort because of the temperature rising boiling, rotate the elimination at a large amount of foams that produce on the liquid level to the foam that solution in the retort produced in the reaction process is reduced effectively, avoids the solution to take place the overflow because of the foam is too much in the reaction process, and then is favorable to improving output.
Optionally, controlling the rotation speed of the defoaming assembly according to the temperature in the reaction tank includes: and determining the rotating speed of the defoaming component corresponding to the temperature in the reaction tank according to the corresponding relation between the rotating speed of the defoaming component and the temperature. Like this, can be according to the correspondence of the rotational speed of defoaming subassembly and temperature, after confirming the temperature in the retort, the rotational speed of control defoaming subassembly is corresponding with the temperature in the retort, make the rotational speed of defoaming subassembly can be along with the temperature in the retort corresponding change, thereby can be when the temperature in the retort reduces, reduce the energy consumption, when the temperature in the retort risees, the rotational speed of control defoaming subassembly improves, carry out quick rotation elimination to the foam on the liquid level of solution, reduce foam content, can avoid the temperature in the retort to be too low when the defoaming subassembly still be in high rotational speed, thereby reduce the operation load of defoaming subassembly, can also prevent simultaneously that the defoaming subassembly still be in low rotational speed, the speed that leads to foam to produce is greater than the elimination speed of defoaming subassembly, be favorable to making the rotational speed of defoaming subassembly change along with the temperature synchronization in the retort, improve the elimination efficiency to the foam.
Optionally, the concentrated phosphoric acid is obtained by three-stage concentration, wherein the first-stage concentration and the second-stage concentration are forced circulation vacuum evaporation concentration, and the third-stage concentration is direct heating evaporation concentration. Thus, the concentration of the obtained phosphoric acid can be effectively improved through three-stage concentration, the yield of the oligomeric phosphate water-soluble fertilizer is further improved, meanwhile, the evaporation capacity is large in the concentration process, the concentrated phosphoric acid is obtained through three-stage concentration, the load of equipment can be effectively reduced, the energy consumption is reduced, in the first-stage concentration stage and the second-stage concentration stage, forced circulation vacuum evaporation concentration can be carried out by using low-pressure steam and hot water as heat sources and fully using low-level heat energy of a nearby sulfuric acid device, the forced circulation vacuum evaporation concentration is carried out, the energy consumption is favorably reduced, the atmospheric pollution is reduced, in the third-stage concentration stage, the direct heating evaporation concentration can be utilized, the phosphoric acid can be directly contacted with hot gas from a combustion furnace when the phosphoric acid enters, the problems of corrosion and scaling caused by forced circulation vacuum evaporation can be overcome, the equipment loss is avoided, and the efficiency of the evaporation concentration is favorably improved.
Alternatively, the first stage is concentrated to 40% P2O5, the second stage is concentrated to 55% P2O5, and the third stage is concentrated to 87% P2O 5. Thus, the concentration degree of the phosphoric acid is improved, the water content of the phosphoric acid is reduced, and the polymerization difficulty of the phosphoric acid and the urea is increased due to the existence of water, so that the polymerization degree of the phosphoric acid and the urea can be improved by reducing the water content of the phosphoric acid.
Optionally, acquiring the air pressure in the reaction tank, and controlling the exhaust speed according to the air pressure in the reaction tank, including: and acquiring the air pressure change speed in the reaction tank, and controlling the exhaust speed of the reaction tank to be in direct proportion to the air pressure change speed. Like this, the speed of gas production in the retort can be reflected to the variation rate of atmospheric pressure, according to the internal atmospheric pressure variation rate of retort of obtaining, the exhaust speed and the atmospheric pressure variation rate of control retort are in direct proportion to when the atmospheric pressure variation rate is great in the retort, the exhaust speed of control retort improves, reduce the ammonia content in the retort, when the atmospheric pressure variation rate is less in the unit time in the retort, the exhaust speed of control retort reduces, make the slow discharge of ammonia in the retort, thereby make the atmospheric pressure in the retort keep at balanced state, be favorable to the solution intensive mixing reaction in the retort, improve output.
Optionally, obtaining the air pressure change speed in the reaction tank, controlling the exhaust speed of the reaction tank to be in direct proportion to the air pressure change speed, and including:
acquiring the air pressure change speed in the reaction tank after the solution in the reaction tank starts to react and before the reaction tank does not start to exhaust;
under the condition that the air pressure in the reaction tank reaches the set air pressure, the reaction tank is controlled to start exhausting, and the exhausting speed is in direct proportion to the air pressure change speed. Therefore, after the reaction of the solution in the reaction tank, a large amount of ammonia gas can be generated, the ammonia pressure can be quickly increased, so that the air pressure change speed in the reaction tank is obtained after the reaction of the solution in the reaction tank is started and before the exhaust of the reaction tank is started, the obtained air pressure change speed is more accurate, meanwhile, the air pressure change condition in the reaction tank can be better judged through the obtained air pressure change speed, then under the condition that the air pressure in the reaction tank reaches the set air pressure, the reaction tank is controlled to start to exhaust, the exhaust speed is in direct proportion to the air pressure change speed, the ammonia pressure in the reaction tank can be kept in an equilibrium state, the situation that the ammonia pressure in the reaction tank is too low or too high is avoided, and the mixed reaction of the solution is not facilitated, so that the inside of the reaction tank is kept in a better ammonia pressure environment, and the reaction efficiency of the solution is improved is facilitated.
Alternatively, the exhaust speed is proportional to the average air pressure change speed for a set period of time before the reaction tank starts to exhaust. Therefore, the higher the average air pressure change speed in the set period of time before the reaction tank starts to exhaust, the more ammonia gas is generated, so that the exhaust speed is in direct proportion to the average air pressure change speed in the set period of time before the reaction tank starts to exhaust, and the exhaust speed can be increased when the average air pressure change speed is higher, or the exhaust speed can be reduced when the average air pressure change speed is lower, so that the ammonia pressure in the reaction tank is kept in a better balance state, and the improvement of the reaction efficiency of the solution is facilitated.
Alternatively, the set time period is greater than or equal to 10 seconds and less than or equal to 30 seconds. Preferably, the set duration is 20 seconds. Thus, the set time length is set in a better numerical value, which is favorable for accurately acquiring the average air pressure change speed, reducing the error of the acquired average air pressure change speed, further accurately controlling the exhaust speed according to the average air pressure change speed, keeping the inside of the reaction tank in a better ammonia pressure balance state and improving the reaction efficiency of the solution.
Optionally, the exhaust speed is proportional to the air pressure change speed, including: and calculating the gas increasing speed in the reaction tank according to the gas pressure changing speed, and controlling the exhaust speed to be the same as the gas increasing speed. Therefore, the gas increasing speed in the reaction tank is calculated, and the exhaust speed is controlled to be the same as the gas increasing speed, so that the exhaust speed is synchronous with the gas increasing speed, and ammonia generated after the reaction of the solution in the reaction tank is orderly discharged, so that the reaction tank is kept in a better ammonia pressure balance state, and the reaction efficiency of the solution is improved.
Optionally, acquiring the air pressure in the reaction tank, and controlling the exhaust speed according to the air pressure in the reaction tank, further comprises: after the reaction tank is determined to start exhausting, the real-time air pressure in the reaction tank is obtained, and the exhausting speed of the reaction tank is controlled according to the relation between the set air pressure and the real-time air pressure. Therefore, after the reaction tank starts to exhaust, the internal air pressure of the reaction tank can be changed due to the exhaust, the real-time air pressure in the reaction tank is obtained, and the exhaust speed of the reaction tank is controlled according to the relation between the set air pressure and the real-time air pressure, so that the exhaust speed can be controlled within a reasonable range, and the imbalance of the ammonia pressure in the reaction tank caused by the excessively high or excessively low exhaust speed is avoided, so that the ammonia pressure in the reaction tank is kept in a better balance state, and the polymerization efficiency of phosphoric acid and urea is improved.
Optionally, in the case that the real-time air pressure is greater than the set air pressure, increasing the exhaust speed; and under the condition that the real-time air pressure is smaller than the set air pressure, reducing the exhaust speed. Therefore, the real-time air pressure in the reaction tank can be controlled in a better range, and the phenomenon that the polymerization efficiency of phosphoric acid and urea is low due to the fact that the real-time air pressure in the reaction tank is too low or too high is prevented, so that the real-time air pressure in the reaction tank is more favorable for the polymerization reaction of the phosphoric acid and the urea, and the reaction efficiency is improved.
Optionally, the magnitude of the increase in the exhaust speed, and the magnitude of the decrease in the exhaust speed, are proportional to the difference between the real-time air pressure and the set air pressure. Therefore, when the difference between the real-time air pressure and the set air pressure is too large, the exhaust speed is increased or the exhaust speed is reduced, the gas discharge speed in the reaction tank is increased, when the difference between the real-time air pressure and the set air pressure is too small, the exhaust speed is reduced or the exhaust speed is increased, and the gas discharge speed in the reaction tank is reduced, so that the real-time air pressure in the reaction tank is kept in a better range, the ammonia pressure in the reaction tank is more favorable for the polymerization reaction of phosphoric acid and urea, and the polymerization reaction efficiency is improved.
Referring to fig. 10, an embodiment of the present disclosure provides an apparatus for manufacturing an oligomeric phosphate water-soluble fertilizer, including a processor (processor) 100 and a memory (memory) 101. Optionally, the apparatus may further comprise a communication interface (Communication Interface) 102 and a bus 103. The processor 100, the communication interface 102, and the memory 101 may communicate with each other via the bus 103. The communication interface 102 may be used for information transfer. Processor 100 may invoke logic instructions in memory 101 to perform the method for manufacturing an oligomeric phosphate water-soluble fertilizer of the above-described embodiments.
Further, the logic instructions in the memory 101 described above may be implemented in the form of software functional units and may be stored in a computer readable storage medium when sold or used as a stand alone product.
The memory 101 is a computer readable storage medium that can be used to store a software program, a computer executable program, such as program instructions/modules corresponding to the methods in the embodiments of the present disclosure. The processor 100 performs functional applications and data processing by executing program instructions/modules stored in the memory 101, i.e., implements the method for manufacturing the oligophosphate water-soluble fertilizer in the above-described embodiment.
The memory 101 may include a storage program area and a storage data area, wherein the storage program area may store an operating system, at least one application program required for a function; the storage data area may store data created according to the use of the terminal device, etc. Further, the memory 101 may include a high-speed random access memory, and may also include a nonvolatile memory.
Embodiments of the present disclosure provide a computer-readable storage medium storing computer-executable instructions configured to perform the above-described method for manufacturing an oligomeric phosphate water-soluble fertilizer.
The disclosed embodiments provide a computer program product comprising a computer program stored on a computer readable storage medium, the computer program comprising program instructions which, when executed by a computer, cause the computer to perform the above-described method for manufacturing an oligomeric phosphate water-soluble fertilizer.
The computer readable storage medium may be a transitory computer readable storage medium or a non-transitory computer readable storage medium.
Embodiments of the present disclosure may be embodied in a software product stored on a storage medium, including one or more instructions for causing a computer device (which may be a personal computer, a server, or a network device, etc.) to perform all or part of the steps of a method according to embodiments of the present disclosure. And the aforementioned storage medium may be a non-transitory storage medium including: a plurality of media capable of storing program codes, such as a usb disk, a removable hard disk, a Read-Only Memory (ROM), a random access Memory (RAM, randomAccess Memory), a magnetic disk, or an optical disk, or a transitory storage medium.
The above description and the drawings illustrate embodiments of the disclosure sufficiently to enable those skilled in the art to practice them. Other embodiments may involve structural, logical, electrical, process, and other changes. The embodiments represent only possible variations. Individual components and functions are optional unless explicitly required, and the sequence of operations may vary. Portions and features of some embodiments may be included in, or substituted for, those of others. Moreover, the terminology used in the present application is for the purpose of describing embodiments only and is not intended to limit the claims. As used in the description of the embodiments and the claims, the singular forms "a," "an," and "the" (the) are intended to include the plural forms as well, unless the context clearly indicates otherwise. Similarly, the term "and/or" as used in this application is meant to encompass any and all possible combinations of one or more of the associated listed. Furthermore, when used in this application, the terms "comprises," "comprising," and/or "includes," and variations thereof, mean that the stated features, integers, steps, operations, elements, and/or components are present, but that the presence or addition of one or more other features, integers, steps, operations, elements, components, and/or groups thereof is not precluded. Without further limitation, an element defined by the phrase "comprising one …" does not exclude the presence of other like elements in a process, method or apparatus comprising such elements. In this context, each embodiment may be described with emphasis on the differences from the other embodiments, and the same similar parts between the various embodiments may be referred to each other. For the methods, products, etc. disclosed in the embodiments, if they correspond to the method sections disclosed in the embodiments, the description of the method sections may be referred to for relevance.
Those of skill in the art will appreciate that the various illustrative elements and algorithm steps described in connection with the embodiments disclosed herein may be implemented as electronic hardware, or combinations of computer software and electronic hardware. Whether such functionality is implemented as hardware or software depends upon the particular application and design constraints imposed on the solution. The skilled artisan may use different methods for each particular application to achieve the described functionality, but such implementation should not be considered to be beyond the scope of the embodiments of the present disclosure. It will be clearly understood by those skilled in the art that, for convenience and brevity of description, specific working procedures of the above-described systems, apparatuses and units may refer to corresponding procedures in the foregoing method embodiments, which are not repeated herein.
In the embodiments disclosed herein, the disclosed methods, articles of manufacture (including but not limited to devices, apparatuses, etc.) may be practiced in other ways. For example, the apparatus embodiments described above are merely illustrative, and for example, the division of the units may be merely a logical function division, and there may be additional divisions when actually implemented, for example, multiple units or components may be combined or integrated into another system, or some features may be omitted, or not performed. In addition, the coupling or direct coupling or communication connection shown or discussed with each other may be through some interface, device or unit indirect coupling or communication connection, which may be in electrical, mechanical or other form. The units described as separate units may or may not be physically separate, and units shown as units may or may not be physical units, may be located in one place, or may be distributed on a plurality of network units. Some or all of the units may be selected according to actual needs to implement the present embodiment. In addition, each functional unit in the embodiments of the present disclosure may be integrated in one processing unit, or each unit may exist alone physically, or two or more units may be integrated in one unit.
The flowcharts and block diagrams in the figures illustrate the architecture, functionality, and operation of possible implementations of systems, methods and computer program products according to embodiments of the present disclosure. In this regard, each block in the flowchart or block diagrams may represent a module, segment, or portion of code, which comprises one or more executable instructions for implementing the specified logical function(s). In some alternative implementations, the functions noted in the block may occur out of the order noted in the figures. For example, two blocks shown in succession may, in fact, be executed substantially concurrently, or the blocks may sometimes be executed in the reverse order, depending upon the functionality involved. In the description corresponding to the flowcharts and block diagrams in the figures, operations or steps corresponding to different blocks may also occur in different orders than that disclosed in the description, and sometimes no specific order exists between different operations or steps. For example, two consecutive operations or steps may actually be performed substantially in parallel, they may sometimes be performed in reverse order, which may be dependent on the functions involved. Each block of the block diagrams and/or flowchart illustration, and combinations of blocks in the block diagrams and/or flowchart illustration, can be implemented by special purpose hardware-based systems which perform the specified functions or acts, or combinations of special purpose hardware and computer instructions.
Claims (8)
1. An apparatus for producing an oligomeric phosphate water-soluble fertilizer, comprising:
a reaction tank (200) for holding a solution;
a microporous gas collection assembly (300) disposed within the reaction tank (200) and partially submerged within the solution of the reaction tank (200); the microporous gas collection assembly (300) comprises a microporous gas suction part (301) and a centralized collection part (302), wherein the microporous gas suction part (301) is of a cylindrical structure with one end closed and the other end open, micropores (303) communicated with an internal hollow area are formed in the side wall, the pore diameter of each micropore (303) can allow gas to pass through, and a plurality of microporous gas suction parts (301) are arranged; the centralized collecting part (302) is communicated with the opening ends of the microporous air suction parts (301);
the defoaming component (400) is rotatably arranged in the reaction tank (200) and is positioned above the solution level, and is used for eliminating foam generated by solution reaction; the defoaming assembly (400) comprises a rotary support (401) and a hollow puncture needle (402); the rotary support (401) is horizontally arranged in the reaction tank (200) and is positioned above the liquid level of the solution; the hollow pricker (402) is fixedly arranged at the lower side of the rotary support (401).
2. The apparatus for producing an oligophosphate water-soluble fertilizer according to claim 1, wherein the microporous getter portion (301) is integrally made of a nanoceramic.
3. The apparatus for manufacturing an oligophosphate water-soluble fertilizer according to claim 1, wherein the tip of the hollow spike (402) is offset to one side, and an open groove (408) is provided on the side wall of the hollow spike (402).
4. An apparatus for producing an oligophosphate water-soluble fertilizer according to any one of claims 1 to 3, further comprising:
the phosphoric acid concentration assembly (500) is communicated with the reaction tank (200) at the discharge end, the phosphoric acid concentration assembly (500) comprises a three-stage concentration structure, wherein the first-stage concentration structure (501) and the second-stage concentration structure (502) are forced circulation vacuum evaporators, and the third-stage concentration structure (503) is a direct heating evaporator.
5. A method for producing an oligomeric phosphate water-soluble fertilizer, applied to the apparatus for producing an oligomeric phosphate water-soluble fertilizer as defined in any one of claims 1 to 4, characterized by comprising:
heating the reaction tank to enable the concentrated phosphoric acid to react with urea in a mixing way;
Acquiring the temperature in the reaction tank, and controlling the rotating speed of the defoaming component according to the temperature in the reaction tank;
and acquiring the air pressure in the reaction tank, and controlling the exhaust speed according to the air pressure in the reaction tank.
6. The method for producing an oligophosphate water-soluble fertilizer according to claim 5, wherein the concentrated phosphoric acid is obtained by three-stage concentration, wherein the first-stage concentration and the second-stage concentration are forced circulation vacuum evaporation concentration, and the third-stage concentration is direct heating evaporation concentration.
7. The method for producing an oligophosphate water-soluble fertilizer according to claim 5, wherein the air pressure in the reaction tank is obtained, and the exhaust speed is controlled according to the air pressure in the reaction tank, comprising:
and acquiring the air pressure change speed in the reaction tank, and controlling the exhaust speed of the reaction tank to be the same as the air pressure change speed.
8. A storage medium storing program instructions which, when executed, perform the method for manufacturing an oligomeric phosphate water-soluble fertilizer according to any one of claims 5 to 7.
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