CN102674281A - Phosphoric acid refining device - Google Patents
Phosphoric acid refining device Download PDFInfo
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- CN102674281A CN102674281A CN2012101477786A CN201210147778A CN102674281A CN 102674281 A CN102674281 A CN 102674281A CN 2012101477786 A CN2012101477786 A CN 2012101477786A CN 201210147778 A CN201210147778 A CN 201210147778A CN 102674281 A CN102674281 A CN 102674281A
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Abstract
The invention discloses a phosphoric acid refining device. The phosphoric acid refining device comprises a phosphoric acid solvent analyzing device, a phosphoric acid concentration device, a phosphoric acid defluorination device and a tail gas washing system with a vacuum device, wherein the phosphoric acid solvent analyzing device comprises a phosphoric acid heater, an analytic supergravity reactor, an analytic gas phase cooler, a split phase tank, a water phase surge tank, an oil phase surge tank and an analytic acid surge tank; the phosphoric acid concentration device comprises a concentration device heater, a flash chamber, a circulating pump, a concentrated acid surge tank, a concentration device gas phase condenser and a concentration device acid condensate surge tank; the phosphoric acid defluorination device comprises a defluorination supergravity reactor, a defluorination phosphoric acid surge tank, a defluorination device gas phase condenser and a defluorination device condensate surge tank; and noncondensable gas outlets in coolers of the devices are connected with the tail gas washing system with the vacuum device. Due to the phosphoric acid refining device, the equipment can be miniaturized, the mass transfer efficiency of the equipment is high, a purification effect on the phosphoric acid is good, and the equipment investment is saved.
Description
Technical field
The present invention relates to a kind of phosphoric acid refining plant, particularly a kind of phosphoric acid by wet process extracting and purifying back extraction phosphoric acid refining plant.
Background technology
SX is the common technology of wet phosphoric acid purifying, solvent collection method generally be with wet method crude phosphoric acid through operations such as pretreatment process, extracting and purifying, aftertreatment are refining, raw phosphoric acid purified becomes PHOSPHORIC ACID TECH.GRADE or food additive grade phosphoric acid; Because of adopting the solvent extraction purification technology, the general concentration of back extraction acid that the extracting and purifying operation is come out is lower and contain a spot of extraction agent and fluorion impurity, for reaching food additive grade phosphoric acid quality standard; The aftertreatment refining step generally need carry out the solvent parsing to back extraction acid, concentrate and degree of depth defluorinate processing, mainly adopts tray column to operate in back extraction acid solvent parsing and phosphoric acid degree of depth defluorinate device at present, in these tray columns; The contact of vapour-liquid is in gravity field, to carry out with flowing; Its mobility status mainly receives the influence of gravity and surface tension of liquid, and liquid-flow is slow, and Surface Renewal is slow; It is low that this has been directed at vapour-liquid mass efficient; Equipment is very huge, and because of phosphoric acid corrosion property is strong, equipment material requires high; Cause facility investment big, this also is a major cause that influences wet phosphoric acid purifying technology popularization.
The ultimate principle of hypergravity mass transfer technology is to utilize unique flow behavior of polyphasic flow system under the hypergravity condition; Strengthen between phase and phase speed of relative movement be in contact with one another; Thereby realize mass transfer process chemical reaction process efficiently, the mode that obtains hypergravity mainly is the formation centrifuge field of turning through high speed rotating.High-gravity technology has obtained application at chemical field at present, and the mass-transfer performance of hypergravity equipment high efficiency can be realized device miniaturization, and equipment layout is simple, and facility investment is little.
Summary of the invention
The object of the present invention is to provide a kind of phosphoric acid refining plant, to reach device miniaturization, equipment layout is simple, invests little requirement.
Technical scheme of the present invention is: a kind of phosphoric acid refining plant comprises the washing tail gas system of phosphoric acid solvolysis analysis apparatus, phosphoric acid concentrating device, phosphoric acid defluorinate device and band vacuum unit; Phosphoric acid solvolysis analysis apparatus comprises the phosphoric acid well heater, resolves supergravity reactor, resolves gas phase water cooler, phase-splitting groove, water dashpot, oil phase dashpot and resolve sour dashpot; The phosphoric acid well heater comprises phosphoric acid import of phosphoric acid well heater and the outlet of phosphoric acid well heater phosphoric acid; Resolving supergravity reactor comprises the import of parsing supergravity reactor phosphoric acid, resolves the supergravity reactor steam inlet, resolves supergravity reactor mixing vapor phase exit and resolve the outlet of supergravity reactor phosphoric acid; Resolve the gas phase water cooler and comprise that resolving the gas phase water cooler mixes the vapour phase import, resolves the noncondensable gas outlet and resolve condensate outlet; Resolving the phase-splitting groove comprises the import of parsing phlegma, resolves the outlet of phase-splitting groove water and resolves the outlet of phase-splitting groove oil phase; The water dashpot comprises import of water dashpot and the outlet of water dashpot; The oil phase dashpot comprises import of oil phase dashpot and the outlet of oil phase dashpot, resolves sour dashpot and comprises that resolving the import of sour dashpot phosphoric acid resolves sour dashpot phosphoric acid outlet;
Import is connected the outlet of phosphoric acid well heater phosphoric acid with parsing supergravity reactor phosphoric acid through pipeline; Resolve supergravity reactor mixing vapor phase exit and conciliate gassing phase water cooler mixing vapour phase import connection through pipeline; Import is connected with the parsing phlegma through pipeline to resolve condensate outlet; The washing tail gas system that resolves noncondensable gas outlet and band vacuum unit is connected; Import is connected with the water dashpot through pipeline to resolve the outlet of phase-splitting groove water; Import is connected with the oil phase dashpot through pipeline to resolve the outlet of phase-splitting groove oil phase, resolve the outlet of supergravity reactor phosphoric acid through pipeline with resolve the import of sour dashpot phosphoric acid and be connected, resolve sour dashpot phosphoric acid and export and pass through pipeline and export with concentrating unit well heater phosphoric acid and be connected;
Phosphoric acid concentrating device comprises the acid phlegma dashpot of concentrating unit well heater, flashing chamber, recycle pump, gelled acid dashpot, concentrating unit gas phase condenser and concentrating unit; The concentrating unit well heater comprises phosphoric acid import of concentrating unit well heater and the outlet of concentrating unit well heater phosphoric acid; Flashing chamber comprises the import of flashing chamber phosphoric acid, flashing chamber vapour outlet, the outlet of flashing chamber gelled acid and the outlet of flashing chamber recycle acid; Recycle pump comprises pump inlet and circulating-pump outlet; The gelled acid dashpot comprises import of gelled acid dashpot and the outlet of gelled acid dashpot; The concentrating unit gas phase condenser comprises that the concentrating unit gas phase condenser mixes gas phase import, the outlet of concentrating unit gas phase condenser noncondensable gas and concentrating unit gas phase condenser condensate outlet, and the acid phlegma dashpot of concentrating unit comprises acid phlegma dashpot import of concentrating unit and the acid phlegma dashpot outlet of compression apparatus;
Import is connected the outlet of concentrating unit well heater phosphoric acid with flashing chamber phosphoric acid through pipeline; The outlet of flashing chamber recycle acid is connected with pump inlet through pipeline; Import is connected circulating-pump outlet with concentrating unit well heater phosphoric acid through pipeline; The flashing chamber vapour outlet mixes the gas phase import through pipeline and concentrating unit gas phase condenser and is connected; Import is connected concentrating unit gas phase condenser condensate outlet with the acid phlegma dashpot of concentrating unit through pipeline, and the outlet of concentrating unit gas phase condenser noncondensable gas is connected through the washing tail gas system of pipeline with the band vacuum unit, and import is connected the outlet of gelled acid dashpot with defluorinate supergravity reactor phosphoric acid through pipeline;
Phosphoric acid defluorinate device comprises defluorinate supergravity reactor, phosphoric acid defluorination dashpot, defluorinate device gas phase condenser and defluorinate device phlegma dashpot;
The defluorinate supergravity reactor comprises the import of defluorinate supergravity reactor phosphoric acid, defluorinate supergravity reactor steam inlet, the fluorine-containing gaseous phase outlet of defluorinate supergravity reactor and the outlet of defluorinate supergravity reactor phosphoric acid; The phosphoric acid defluorination dashpot comprises import of phosphoric acid defluorination dashpot and the outlet of phosphoric acid defluorination dashpot; Defluorinate device gas phase condenser comprises that defluorinate device gas phase condenser mixes gas phase import, the outlet of defluorinate device gas phase condenser noncondensable gas and defluorinate device gas phase condenser condensate outlet, and defluorinate device phlegma dashpot comprises dashpot import of defluorinate device phlegma and the outlet of defluorinate device phlegma dashpot;
The fluorine-containing gaseous phase outlet of defluorinate supergravity reactor mixes the gas phase import through pipeline and defluorinate device gas phase condenser and is connected; Import is connected the outlet of defluorinate device gas phase condenser noncondensable gas with defluorinate device phlegma dashpot through pipeline; Defluorinate device gas phase condenser condensate outlet is connected through the washing tail gas system of pipeline with the band vacuum unit, and import is connected the outlet of defluorinate supergravity reactor phosphoric acid with the phosphoric acid defluorination dashpot through pipeline.
Above-mentioned defluorinate supergravity reactor is a kind of hypergravity mass transfer apparatus, and the number of patent application of this device is 200710067008.X.
Principle of the present invention is: in phosphoric acid solvent resolving; Total resistance to mass transfer of gas-liquid phase mass transfer process is resistance of gas mass transfer and resistance of liquid mass transfer sum; Resistance of gas mass transfer and resistance of liquid mass transfer are inversely proportional to volume transmission quality coefficient and quality mass transfer coefficient respectively; Under super gravity field; Volume transmission quality coefficient and quality mass transfer coefficient all have significant lifting (volume transmission quality coefficient under the super gravity field is about 10 times in the gravity field), so total resistance to mass transfer ratio of gas-liquid phase mass transfer process reduces in gravity field significantly in super gravity field.In resolving supergravity reactor; Because powerful centrifugal action; Phosphoric acid in high dispersive, mix and the environment of interface fast updating fully contacts and produce mass transfer with steam down a small amount of organic solvent of carrying secretly in the phosphoric acid and change gas phase over to and taken away, thereby completion resolving by force by steam.
When rectifying defluorinate process; In super gravity field; The work that liquid receives hypergravity flows in order to the tens of times of flow rate of liquid in common rectifying tower, and liquid receives the effect of great shearing force, forms liquid infinitesimals such as micron order to nano level liquid film, brin and drop.These liquid infinitesimals have not only produced huge phase interface, have strengthened transfer efficiency, and these phase interfacies upgraded by the dual function of hypergravity and filler friction faster, further promoted the transmission effect and the speed of vapour-liquid.The hypergravity rectifying make liquid at high dispersive, high mixing, strong turbulence and interface rapidly more under the news with gas with great speed of relative movement counter current contact in curved channel; Make vapour-liquid through filler the time, can carry out mass transfer, heat transfer efficiently; Reach fast and balance each other, realize that mixture separates purification in the short period of time.
But through the above technical scheme knowledge capital beneficial effect of the invention, adopt the present invention, can realize device miniaturization, and the equipment mass-transfer efficiency is high, phosphoric acid purification is effective, low equipment investment.
Description of drawings
Fig. 1 is a phosphoric acid solvolysis analysis apparatus structural representation of the present invention;
Fig. 2 is a phosphoric acid concentrating device structural representation of the present invention;
Fig. 3 is a phosphoric acid defluorinate apparatus structure synoptic diagram of the present invention;
Fig. 4 is an apparatus structure synoptic diagram of the present invention;
Wherein: 1, phosphoric acid well heater, 2, the import of phosphoric acid well heater phosphoric acid, 3, the outlet of phosphoric acid well heater phosphoric acid, 4, resolve supergravity reactor; 5, resolve the import of supergravity reactor phosphoric acid, 6, resolve the supergravity reactor steam inlet, 7, resolve supergravity reactor mixings vapor phase exit, 8, resolve supergravity reactor phosphoric acid and export; 9, resolve sour dashpot, 10, resolve the import of sour dashpot phosphoric acid, 11, resolve sour dashpot phosphoric acid outlet, 12, resolve the gas phase water cooler; 13, resolve the gas phase water cooler and mix the vapour phase import, 14, resolve condensate outlet, 15, resolve the noncondensable gas outlet, 16, the washing tail gas system; 17, resolve the phase-splitting groove, 18, resolve the phlegma import, 19, resolve the outlet of phase-splitting groove oil phase, 20, resolve the outlet of phase-splitting groove water; 21, water dashpot, 22, the import of water dashpot, 23, the outlet of water dashpot, 24, the oil phase dashpot; 25, oil phase dashpot import, 26, oil phase dashpot outlet, 27, the concentrating unit well heater, 28, the outlet of concentrating unit well heater phosphoric acid; 29, concentrating unit well heater phosphoric acid import, 30, flashing chamber, 31, the import of flashing chamber phosphoric acid, 32, the flashing chamber vapour outlet; 33, flashing chamber gelled acid outlet, 34, the outlet of flashing chamber recycle acid, 35, recycle pump, 36, pump inlet; 37, circulating-pump outlet, 38, the gelled acid dashpot, 39, the import of gelled acid dashpot, 40, the outlet of gelled acid dashpot; 41, concentrating unit gas phase condenser, 42, the concentrating unit gas phase condenser mixes the gas phase import, 43, the outlet of concentrating unit gas phase condenser noncondensable gas, 44, concentrating unit gas phase condenser condensate outlet; 45, the acid phlegma dashpot of concentrating unit, 46, the import of the acid phlegma dashpot of concentrating unit, 47, the acid phlegma dashpot outlet of compression apparatus, 48, the defluorinate supergravity reactor; 49, defluorinate supergravity reactor phosphoric acid import, 50, defluorinate supergravity reactor steam inlet, 51, the fluorine-containing gaseous phase outlet of defluorinate supergravity reactor, 52, the outlet of defluorinate supergravity reactor phosphoric acid; 53, phosphoric acid defluorination dashpot, 54, the import of phosphoric acid defluorination dashpot, 55, the outlet of phosphoric acid defluorination dashpot, 56, defluorinate device gas phase condenser; 57, defluorinate device gas phase condenser mixes the gas phase import, and 58, the outlet of defluorinate device gas phase condenser noncondensable gas, 59, defluorinate device gas phase condenser condensate outlet; 60, defluorinate device phlegma dashpot, 61, the import of defluorinate device phlegma dashpot, 62, the outlet of defluorinate device phlegma dashpot.
Embodiment
Embodiment 1
A kind of phosphoric acid refining plant comprises the washing tail gas system 16 of phosphoric acid solvolysis analysis apparatus, phosphoric acid concentrating device, phosphoric acid defluorinate device and band vacuum unit; Phosphoric acid solvolysis analysis apparatus comprises phosphoric acid well heater 1, resolves supergravity reactor 4, resolves gas phase water cooler 12, phase-splitting groove 17, water dashpot 21, oil phase dashpot 24 and resolve sour dashpot 9; Phosphoric acid well heater 1 comprises phosphoric acid well heater phosphoric acid import 2 and phosphoric acid well heater phosphoric acid outlet 3; Resolving supergravity reactor 4 comprises parsing supergravity reactor phosphoric acid import 5, resolves supergravity reactor steam inlet 6, resolves supergravity reactor mixing vapor phase exit 7 and resolves supergravity reactor phosphoric acid outlet 8; Resolve gas phase water cooler 12 and comprise that resolving the gas phase water cooler mixes vapour phase import 13, resolves noncondensable gas outlet 15 and resolve condensate outlet 14; Resolving phase-splitting groove 17 comprises parsing phlegma import 18, resolves phase-splitting groove water outlet 20 and resolves phase-splitting groove oil phase outlet 19; Water dashpot 21 comprises water dashpot import 22 and water dashpot outlet 23; Oil phase dashpot 24 comprises oil phase dashpot import 25 and oil phase dashpot outlet 26, resolves sour dashpot 9 and comprises that resolving sour dashpot phosphoric acid import 10 resolves sour dashpot phosphoric acid outlet 11;
The outlet 3 of phosphoric acid well heater phosphoric acid is connected with parsing supergravity reactor phosphoric acid import 5 through pipeline; Resolve supergravity reactor mixing vapor phase exit 7 and conciliate gassing phase water cooler mixing vapour phase import 13 connections through pipeline; Resolving condensate outlet 14 is connected with parsing phlegma import 18 through pipeline; The washing tail gas system 16 that resolves noncondensable gas outlet 15 and band vacuum unit is connected; Resolving the outlet 20 of phase-splitting groove water is connected with water dashpot import 22 through pipeline; Resolve the outlet 19 of phase-splitting groove oil phase and be connected with oil phase dashpot import 25 through pipeline, resolve the outlet 8 of supergravity reactor phosphoric acid through pipeline with resolve sour dashpot phosphoric acid import 10 and be connected, resolve sour dashpot phosphoric acid and export 11 and pass through pipeline and concentrating unit well heater phosphoric acid and export 28 and be connected;
Phosphoric acid concentrating device comprises the acid phlegma dashpot 45 of concentrating unit well heater 27, flashing chamber 30, recycle pump 35, gelled acid dashpot 38, concentrating unit gas phase condenser 41 and concentrating unit; Concentrating unit well heater 27 comprises concentrating unit well heater phosphoric acid import 29 and concentrating unit well heater phosphoric acid outlet 28; Flashing chamber 30 comprises flashing chamber phosphoric acid import 31, flashing chamber vapour outlet 32, the outlet 33 of flashing chamber gelled acid and flashing chamber recycle acid outlet 34; Recycle pump 35 comprises pump inlet 36 and circulating-pump outlet 37; Gelled acid dashpot 38 comprises gelled acid dashpot import 39 and gelled acid dashpot outlet 40; Concentrating unit gas phase condenser 41 comprises that the concentrating unit gas phase condenser mixes gas phase import 42, the outlet 43 of concentrating unit gas phase condenser noncondensable gas and concentrating unit gas phase condenser condensate outlet 44, and the acid phlegma dashpot 45 of concentrating unit comprises the acid phlegma dashpot outlet 47 of import 46 of the acid phlegma dashpot of concentrating unit and compression apparatus;
The outlet 28 of concentrating unit well heater phosphoric acid is connected with flashing chamber phosphoric acid import 31 through pipeline; The outlet 34 of flashing chamber recycle acid is connected with pump inlet 36 through pipeline; Circulating-pump outlet 37 is connected with concentrating unit well heater phosphoric acid import 29 through pipeline; Flashing chamber vapour outlet 32 mixes gas phase import 42 through pipeline and concentrating unit gas phase condenser and is connected; Concentrating unit gas phase condenser condensate outlet 44 is connected with the acid phlegma dashpot of concentrating unit import 46 through pipeline; The outlet 43 of concentrating unit gas phase condenser noncondensable gas is connected through the washing tail gas system 16 of pipeline with the band vacuum unit, and the outlet 40 of gelled acid dashpot is connected with defluorinate supergravity reactor phosphoric acid import 49 through pipeline;
Phosphoric acid defluorinate device comprises defluorinate supergravity reactor 48, phosphoric acid defluorination dashpot 53, defluorinate device gas phase condenser 56 and defluorinate device phlegma dashpot 60;
Defluorinate supergravity reactor 48 comprises defluorinate supergravity reactor phosphoric acid import 49, defluorinate supergravity reactor steam inlet 50, the fluorine-containing gaseous phase outlet 51 of defluorinate supergravity reactor and defluorinate supergravity reactor phosphoric acid outlet 52; Phosphoric acid defluorination dashpot 53 comprises phosphoric acid defluorination dashpot import 54 and phosphoric acid defluorination dashpot outlet 55; Defluorinate device gas phase condenser 56 comprises that defluorinate device gas phase condenser mixes gas phase import 57, the outlet 58 of defluorinate device gas phase condenser noncondensable gas and defluorinate device gas phase condenser condensate outlet 59, and defluorinate device phlegma dashpot 60 comprises defluorinate device phlegma dashpot import 61 and defluorinate device phlegma dashpot outlet 62;
The fluorine-containing gaseous phase outlet 51 of defluorinate supergravity reactor mixes gas phase import 57 through pipeline and defluorinate device gas phase condenser and is connected; The outlet 58 of defluorinate device gas phase condenser noncondensable gas is connected with defluorinate device phlegma dashpot import 61 through pipeline; Defluorinate device gas phase condenser condensate outlet 59 is connected through the washing tail gas system 16 of pipeline with the band vacuum unit, and the outlet 52 of defluorinate supergravity reactor phosphoric acid is connected with phosphoric acid defluorination dashpot import 54 through pipeline.
When use is of the present invention; Sour from the back extraction that extracting and purifying comes; After 1 heating of phosphoric acid well heater, get into desorb supergravity reactor 4 from desorb supergravity reactor phosphoric acid import 5; Steam gets into desorb supergravity reactor 4 in proportion from desorb supergravity reactor steam inlet 6; Phosphoric acid efficiently contacts in desorb supergravity reactor 4 with steam, and a small amount of organic solvent of carrying secretly in the phosphoric acid (extraction agent) becomes gas phase along with steam gets into desorb gas phase water cooler 12 from desorb supergravity reactor mixing vapor phase exit 7, through the cooling of desorb gas phase water cooler 12; Water vapor that comes out from desorb supergravity reactor mixing vapor phase exit 7 and organic vapor become liquid phase and come out to get into desorb phase-splitting grooves 17 through desorb phlegma import 18 from desorb condensate outlet 14; Through the clarification phase-splitting of desorb phase-splitting groove 17, water gets into water dashpot 21 from the outlet 20 of desorb phase-splitting groove water through water dashpot import 22, is discharged to Waste Water Treatment from water dashpot outlet 23 at last.Oil phase gets into oil phase dashpot 24 from the outlet 19 of desorb phase-splitting groove oil phase through oil phase dashpot import 25, and oil phase dashpot outlet 26 is returned extraction process and reused.Noncondensable gas is from desorb noncondensable gas outlet 15 come out to be discharged to through the pipeline washing tail gas system 16 of band vacuum unit, and noncondensable gas is discharged into atmosphere through washing after up to standard.The phosphoric acid that has removed organic solvent gets into desorb acid dashpot 9 from the outlet 8 of desorb supergravity reactor phosphoric acid through desorb acid dashpot phosphoric acid import 10, gets into phosphoric acid concentrating device from desorb acid dashpot phosphoric acid outlet 11.
At phosphoric acid concentrating device; The desorb acid of coming out from desorb acid dashpot phosphoric acid outlet 11 comprises that through flashing chamber 30 flashing chamber phosphoric acid import 31 gets into flashing chamber 30; Phosphoric acid is transported to concentrating unit well heater 27 from flashing chamber recycle acid outlet 34 through recycle pump recycle pump 35 and returns flashing chamber 30; Phosphoric acid is after 27 heating of concentrating unit well heater; Boiling in flashing chamber 30, the water in the phosphoric acid become steam and mix gas phase import 42 entering concentrating unit gas phase condensers 41 from flashing chamber vapour outlet 32 through the concentrating unit gas phase condenser, through the cooling of concentrating unit gas phase condenser 41; Water vapor becomes acid phlegma and gets into the acid phlegma dashpot 45 of concentrating unit through the acid phlegma dashpot of concentrating unit import 46, is discharged to Waste Water Treatment from the acid phlegma dashpot outlet 47 of concentrating unit at last.Noncondensable gas in the concentrating unit gas phase condenser 41 is from concentrating unit gas phase condenser noncondensable gas outlet 43 come out to be discharged to through the pipeline washing tail gas system 16 of band vacuum unit, and noncondensable gas is discharged into atmosphere through washing after up to standard.Phosphoric Acid Concentration in the flashing chamber 30 gets into gelled acid dashpots 38 from the outlet 33 of flashing chamber gelled acid through gelled acid dashpot import 39 after reaching the concentration of regulation, is transported to phosphoric acid defluorinate device from gelled acid dashpot outlet 40.
At phosphoric acid defluorinate device; The phosphoric acid that comes out from gelled acid dashpot outlet 40 gets into defluorinate supergravity reactor 48 through defluorinate supergravity reactor phosphoric acid import 49; Steam gets into defluorinate supergravity reactor 48 from defluorinate supergravity reactor steam inlet 50 in proportion; Phosphoric acid efficiently contacts in defluorinate supergravity reactor 48 with steam; The fluoride impurities of carrying secretly in the phosphoric acid becomes gas phase and gets into defluorinate device gas phase condenser 56 along with steam mixes gas phase import 57 from the fluorine-containing gaseous phase outlet 51 of defluorinate supergravity reactor through defluorinate device gas phase condenser; Cooling through defluorinate device gas phase condenser 56; Fluorine-containing steam becomes liquid phase and comes out to get into defluorinate device phlegma dashpot 60 through defluorinate device phlegma dashpot import 61 from defluorinate device gas phase condenser condensate outlet 59, is discharged to Waste Water Treatment from defluorinate device phlegma dashpot outlet 62.The phosphoric acid defluorination that has removed fluorion impurity in the defluorinate supergravity reactor 48 gets into phosphoric acid defluorination dashpot 53 from the outlet 52 of defluorinate supergravity reactor phosphoric acid through phosphoric acid defluorination dashpot import 54, and phosphoric acid defluorination is through be transported to the product storage tank from phosphoric acid defluorination dashpot outlet 55 after the assay was approved.
The noncondensable gas outlet all is connected with the washing tail gas system 16 of band vacuum unit in the water cooler of above phosphoric acid solvent desorption device, phosphoric acid concentrating device, phosphoric acid defluorinate device; So three devices all are operations under vacuum condition; Operation can reduce service temperature under vacuum condition; Can reduce equipment corrosion, reduce system capacity consumption.
Claims (2)
1. a phosphoric acid refining plant is characterized in that it comprises the washing tail gas system (16) of phosphoric acid solvolysis analysis apparatus, phosphoric acid concentrating device, phosphoric acid defluorinate device and band vacuum unit; Phosphoric acid solvolysis analysis apparatus comprises phosphoric acid well heater (1), parsing supergravity reactor (4), resolves gas phase water cooler (12), phase-splitting groove (17), water dashpot (21), oil phase dashpot (24) and resolves sour dashpot (9); Phosphoric acid well heater (1) comprises phosphoric acid well heater phosphoric acid import (2) and phosphoric acid well heater phosphoric acid outlet (3); Resolving supergravity reactor (4) comprises parsing supergravity reactor phosphoric acid import (5), resolves supergravity reactor steam inlet (6), resolves supergravity reactor mixing vapor phase exit (7) and resolves supergravity reactor phosphoric acid outlet (8); Resolve gas phase water cooler (12) and comprise that resolving the gas phase water cooler mixes vapour phase import (13), resolves noncondensable gas outlet (15) and resolve condensate outlet (14); Resolving phase-splitting groove (17) comprises parsing phlegma import (18), resolves phase-splitting groove water outlet (20) and resolves phase-splitting groove oil phase outlet (19); Water dashpot (21) comprises water dashpot import (22) and water dashpot outlet (23); Oil phase dashpot (24) comprises oil phase dashpot import (25) and oil phase dashpot outlet (26), resolves sour dashpot (9) and comprises that resolving sour dashpot phosphoric acid import (10) resolves sour dashpot phosphoric acid outlet (11);
Phosphoric acid well heater phosphoric acid outlet (3) is connected with parsing supergravity reactor phosphoric acid import (5) through pipeline; Resolve supergravity reactor mixing vapor phase exit (7) and conciliate gassing phase water cooler mixing vapour phase import (13) connection through pipeline; Resolving condensate outlet (14) is connected with parsing phlegma import (18) through pipeline; The washing tail gas system (16) that resolves noncondensable gas outlet (15) and band vacuum unit is connected; Resolving phase-splitting groove water outlet (20) is connected with water dashpot import (22) through pipeline; Resolving phase-splitting groove oil phase outlet (19) is connected with oil phase dashpot import (25) through pipeline; Resolve supergravity reactor phosphoric acid outlet (8) and be connected with parsing sour dashpot phosphoric acid import (10), resolve sour dashpot phosphoric acid outlet (11) and be connected with concentrating unit well heater phosphoric acid outlet (28) through pipeline through pipeline;
Phosphoric acid concentrating device comprises the acid phlegma dashpot (45) of concentrating unit well heater (27), flashing chamber (30), recycle pump (35), gelled acid dashpot (38), concentrating unit gas phase condenser (41) and concentrating unit; Concentrating unit well heater (27) comprises concentrating unit well heater phosphoric acid import (29) and concentrating unit well heater phosphoric acid outlet (28); Flashing chamber (30) comprises flashing chamber phosphoric acid import (31), flashing chamber vapour outlet (32), flashing chamber gelled acid outlet (33) and flashing chamber recycle acid outlet (34); Recycle pump (35) comprises pump inlet (36) and circulating-pump outlet (37); Gelled acid dashpot (38) gelled acid dashpot import (39) and gelled acid dashpot outlet (40); Concentrating unit gas phase condenser (41) comprises that the concentrating unit gas phase condenser mixes gas phase import (42), the outlet of concentrating unit gas phase condenser noncondensable gas (43) and concentrating unit gas phase condenser condensate outlet (44), and the acid phlegma dashpot of concentrating unit (45) comprises acid phlegma dashpot import (46) of concentrating unit and the acid phlegma dashpot outlet of compression apparatus (47);
Concentrating unit well heater phosphoric acid outlet (28) is connected with flashing chamber phosphoric acid import (31) through pipeline; Flashing chamber recycle acid outlet (34) is connected with pump inlet (36) through pipeline; Circulating-pump outlet (37) is connected with concentrating unit well heater phosphoric acid import (29) through pipeline; Flashing chamber vapour outlet (32) mixes gas phase import (42) through pipeline and concentrating unit gas phase condenser and is connected; Concentrating unit gas phase condenser condensate outlet (44) is connected with the acid phlegma dashpot import of concentrating unit (46) through pipeline; Concentrating unit gas phase condenser noncondensable gas outlet (43) is connected through the washing tail gas system (16) of pipeline with the band vacuum unit, and gelled acid dashpot outlet (40) is connected with defluorinate supergravity reactor phosphoric acid import (49) through pipeline;
Phosphoric acid defluorinate device comprises defluorinate supergravity reactor (48), phosphoric acid defluorination dashpot (53), defluorinate device gas phase condenser (56) and defluorinate device phlegma dashpot (60);
Defluorinate supergravity reactor (48) comprises defluorinate supergravity reactor phosphoric acid import (49), defluorinate supergravity reactor steam inlet (50), the fluorine-containing gaseous phase outlet of defluorinate supergravity reactor (51) and defluorinate supergravity reactor phosphoric acid outlet (52); Phosphoric acid defluorination dashpot (53) comprises phosphoric acid defluorination dashpot import (54) and phosphoric acid defluorination dashpot outlet (55); Defluorinate device gas phase condenser (56) comprises that defluorinate device gas phase condenser mixes gas phase import (57), the outlet of defluorinate device gas phase condenser noncondensable gas (58) and defluorinate device gas phase condenser condensate outlet (59), and defluorinate device phlegma dashpot (60) comprises defluorinate device phlegma dashpot import (61) and defluorinate device phlegma dashpot outlet (62);
The fluorine-containing gaseous phase outlet of defluorinate supergravity reactor (51) mixes gas phase import (57) through pipeline and defluorinate device gas phase condenser and is connected; Defluorinate device gas phase condenser noncondensable gas outlet (58) is connected with defluorinate device phlegma dashpot import (61) through pipeline; Defluorinate device gas phase condenser condensate outlet (59) is connected through the washing tail gas system (16) of pipeline with the band vacuum unit, and defluorinate supergravity reactor phosphoric acid outlet (52) is connected with phosphoric acid defluorination dashpot import (54) through pipeline.
2. phosphoric acid refining plant according to claim 1 is characterized in that a kind of application for a patent for invention of defluorinate supergravity reactor (48) in the phosphoric acid defluorinate device number is a kind of hypergravity mass transfer apparatus of 200710067008.x.
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| CN 201210147778 CN102674281B (en) | 2012-05-14 | 2012-05-14 | Phosphoric acid refining device |
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| CN 201210147778 CN102674281B (en) | 2012-05-14 | 2012-05-14 | Phosphoric acid refining device |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104555976A (en) * | 2014-12-24 | 2015-04-29 | 瓮福（集团）有限责任公司 | Acidic condensate using method |
| CN106006806A (en) * | 2016-07-22 | 2016-10-12 | 株洲三特环保节能有限公司 | Hot air and tubular heater combined waste acid concentration treatment method and device |
| CN109200613A (en) * | 2018-11-24 | 2019-01-15 | 无锡诚尔鑫环保装备科技有限公司 | A kind of liquid concentration collaborative device and its working method |
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| CN202185197U (en) * | 2011-07-05 | 2012-04-11 | 吴杰 | Filter used for refined wet process phosphoric acid |
| CN102424373A (en) * | 2011-12-16 | 2012-04-25 | 吴杰 | Concentration apparatus for wet method phosphoric acid refinement |
| CN202558634U (en) * | 2012-05-14 | 2012-11-28 | 瓮福（集团）有限责任公司 | Phosphoric acid refining device |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104555976A (en) * | 2014-12-24 | 2015-04-29 | 瓮福（集团）有限责任公司 | Acidic condensate using method |
| CN106006806A (en) * | 2016-07-22 | 2016-10-12 | 株洲三特环保节能有限公司 | Hot air and tubular heater combined waste acid concentration treatment method and device |
| CN109200613A (en) * | 2018-11-24 | 2019-01-15 | 无锡诚尔鑫环保装备科技有限公司 | A kind of liquid concentration collaborative device and its working method |
| CN109200613B (en) * | 2018-11-24 | 2023-11-07 | 无锡诚尔鑫环保装备科技有限公司 | Liquid concentration cooperative device and working method thereof |
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| CN102674281B (en) | 2013-08-07 |
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