CN105753744B - A kind of H acid preparation facilities with energy-saving effect - Google Patents
A kind of H acid preparation facilities with energy-saving effect Download PDFInfo
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- CN105753744B CN105753744B CN201610113728.4A CN201610113728A CN105753744B CN 105753744 B CN105753744 B CN 105753744B CN 201610113728 A CN201610113728 A CN 201610113728A CN 105753744 B CN105753744 B CN 105753744B
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- C07C303/00—Preparation of esters or amides of sulfuric acids; Preparation of sulfonic acids or of their esters, halides, anhydrides or amides
- C07C303/02—Preparation of esters or amides of sulfuric acids; Preparation of sulfonic acids or of their esters, halides, anhydrides or amides of sulfonic acids or halides thereof
- C07C303/22—Preparation of esters or amides of sulfuric acids; Preparation of sulfonic acids or of their esters, halides, anhydrides or amides of sulfonic acids or halides thereof from sulfonic acids, by reactions not involving the formation of sulfo or halosulfonyl groups; from sulfonic halides by reactions not involving the formation of halosulfonyl groups
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Abstract
The invention discloses a kind of H acid preparation facilities with energy-saving effect, the device includes extraction equipment, reduction apparatus, enrichment facility, dilution device, isolation and filter, the first outlet of extraction equipment is connected with the import of reduction apparatus, the outlet of reduction apparatus is connected with the import of enrichment facility, the outlet of enrichment facility is connected with the import of dilution device, the outlet of dilution device is connected with the first import of isolation and filter, and the second import of isolation and filter and the second outlet of extraction equipment are connected.The preparation facilities is made H acid using quantity-produced method, and production efficiency is high, saves material, reduces financial cost.
Description
Technical field
The present invention relates to the preparation field of dye material, it particularly relates to prepared by a kind of H- acid with energy-saving effect
Device.
Background technology
H- acid is the important source material of dye industry, mainly for the production of reactive dye, direct dyes, acid dyes, also may be used
For products such as production chromotropic acids.H- acid chemical name be：1- amino-8-naphthol -3,6- disulfonic acid.The chemistry knot of H- acid
Structure formula is：
The molecular formula of H- acid：C10H9NO7S2, relative molecular mass：319.3.H- acid dry products are white to gray crystals powder
End.Cold water is slightly soluble in, hot water is soluble in, the alkaline solutions such as soda ash or caustic soda are dissolved in, is in reddish brown purple with ferric trichloride effect, it is molten
It is dark green in alkaline solution.
H- acid manufactures are with a long history, but are still so far most important intermediate in naphthalene system.Current domestic production H- acid is main
To use batch process.The batch process production H- techniques that use of acid with refined naphthalene as main material, by sulfonation, nitrification, denitration, neutralization,
Reduction, press filtration, isolation, filtering, dissolving, alkali fusion, isolation, filtering, drying and other steps are obtained.Production process is with intermittently operated
Main, process route is more long, and production capacity is low, and yield is relatively low, and three wastes discharge amount is big.The country is existing generally to use the technique road
Line.
The content of the invention
Technical problem：The technical problems to be solved by the invention are：A kind of H- acid with energy-saving effect is provided and prepares dress
Put, the preparation facilities is made H- acid using quantity-produced method, production efficiency is high, saves material, reduces financial cost.
Technical scheme：In order to solve the above technical problems, the technical scheme that uses of the embodiment of the present invention for：
It is a kind of with energy-saving effect H- acid preparation facilities, the device include extraction equipment, reduction apparatus, enrichment facility,
Dilution device, isolation and filter, the first outlet of extraction equipment are connected with the import of reduction apparatus, the outlet of reduction apparatus
It is connected with the import of enrichment facility, the outlet of enrichment facility is connected with the import of dilution device, outlet and the isolation of dilution device
The first import with filter is connected, and the second import of isolation and filter and the second outlet of extraction equipment are connected.
Preferably, described extraction equipment includes the second pump, extraction reactor, the first cooling and active carbon adsorption
Device, the first dilute sulfuric acid surge tank, back extraction reactor, the second cooling and activated carbon adsorption unit, nitrobased NPK storage tank；Second
The import of pump is connected with the outlet of denitration thing surge tank, and the outlet of the second pump is connected with the first import of extraction reactor, extraction
The first outlet of reactor is connected with the first cooling with the import of activated carbon adsorption unit, and first cools down and activated carbon adsorption unit
Outlet be connected with the import of the first dilute sulfuric acid surge tank；The second outlet of extraction reactor connects with the import of back extraction reactor
Connect, the first outlet for being stripped reactor is connected with the second cooling with the import of activated carbon adsorption unit, second cools down and activity
The outlet of carbon adsorption device is connected with the import of nitrobased NPK storage tank；It is stripped the second outlet and extraction reactor of reactor
Second import is connected.
Preferably, described reduction apparatus include preheating device, hydrogenation reactor, cooling device, gas-liquid separation
Device separation, amino T acid storage tanks, filter, the material inlet of preheating device are connected with the outlet of nitrobased NPK storage tank, pre- hot charging
The outlet put is connected with the first import of hydrogenation reactor, and the outlet of hydrogenation reactor is connected with the import of cooling device, cooling
The material outlet of device is connected with the import of gas-liquid separator separates, liquid outlet and the amino T acid storages of gas-liquid separator separates
The import connection of tank, the gas vent of gas-liquid separator separates be connected with the import of filter, the outlet of filter and adds
The second import connection of hydrogen reactor.
Preferably, described enrichment facility includes the second preheating device, 5 effect adverse current enrichment facilities, dense T acid bufferings
Tank, 2 effect adverse current enrichment facilities, alkali solution surge tank, the first import of the second preheating device are connected with the delivery port of cooling device,
Second import of the second preheating device is connected with the outlet of amino T acid storage tanks, and the outlet of the second preheating device is concentrated with 5 effect adverse currents
The import connection of device, the outlet of 5 effect adverse current enrichment facilities is connected with the import of dense T acid bufferings tank；2 effect adverse current enrichment facilities
Outlet is connected with the import of alkali solution surge tank.
Preferably, described dilution device includes heat exchanger, alkali-melting vessel, preheater, the 3rd pump, dilution kettle, cold
Solidifying retracting device, stripper, methanol recovery device and alkali fusion thing surge tank, the import of described heat exchanger and alkali solution surge tank
Outlet connection, the outlet of heat exchanger is connected with the first import of alkali-melting vessel, the outlet of dense T acid bufferings tank and the second of preheater
Entrance is connected；The outlet of preheater is connected by the 3rd pump with the second import of alkali-melting vessel, outlet and the dilution kettle of alkali-melting vessel
Import is connected, and the methanol outlet for diluting kettle is connected with the import of condensate recycling device, and outlet and the methyl alcohol of condensate recycling device are returned
The first import connection of receiving apparatus；Dilute kettle alkali fusion thing outlet be connected with the entrance of stripper, the methanol outlet of stripper and
The second import connection of methanol recovery device, the outlet of methanol recovery device is connected with the import of preheater first；The alkali of stripper
Fusant outlet is connected with the import of alkali fusion thing surge tank.
Preferably, described isolation and filter include acid preparing device, the second dilute sulfuric acid surge tank, isolation
Kettle, the second cooling device, cooling reactor, filter, sulfur dioxide recovery device, wash water tank, wastewater treatment equipment；Acid preparing device
Import is connected with the outlet of the first dilute sulfuric acid surge tank, and the outlet of acid preparing device is connected with the import of the second dilute sulfuric acid surge tank,
The outlet of the second dilute sulfuric acid surge tank and the first import of separation kettle connection, the second import of separation kettle and alkali fusion thing surge tank
Outlet connection, the sulfur dioxide outlet and the import of the second cooling device of separation kettle are connected, the outlet of the second cooling device and two
The import connection of sulfur recovery unit is aoxidized, the material outlet of separation kettle is connected with the import of cooling reactor, the outlet of cooling reactor and mistake
The entrance connection of filter, the entrance connection of the first outlet and wash water tank of filter, the outlet of wash water tank and the 3rd of separation kettle the
Import is connected, the import connection of the second outlet and wastewater treatment equipment of filter.
As preference, the described acid preparation facilities of the H- with energy-saving effect, also including drying device, drying device
Import and the 3rd outlet connection of filter.
Beneficial effect：Compared with prior art, the embodiment of the present invention has the advantages that：Above-described embodiment is by extraction
Take device, reduction apparatus, enrichment facility, dilution device, isolation and filter and H- acid is obtained.Using device production H- acid tools
There is continuity, substantially increase production efficiency.Simultaneously in preparation process, part material is reclaimed, reused, significantly
Reduce financial cost.
Brief description of the drawings
Fig. 1 is a kind of structured flowchart of the embodiment of the present invention；
Fig. 2 is another structured flowchart of the embodiment of the present invention；
Fig. 3 is the structured flowchart after the embodiment of the present invention and xanthator, the assembling of nitrification installation 2, denitrification apparatus.
Have in figure：It is xanthator 1, nitrification installation 2, denitrification apparatus 3, extraction equipment 4, reduction apparatus 5, enrichment facility 6, dilute
Release device 7, isolation and filter 8, drying device 9, sulphonation kettle 101, surge tank 102, indexable sulfonation tower 103, sulfonating reaction
104, three sulfonation towers 105 of device, sulfonated bodies surge tank 106,201, two grades of nitrating pots 202, itrated compound of one-level nitrator delay
Rush tank 203, the first pump 301, Benitration reactor 302, denitration thing surge tank 303, the second pump 401, extraction reactor 402, first
Cooling and activated carbon adsorption unit 403, the first dilute sulfuric acid surge tank 404, the cooling of back extraction reactor 405, second and activated carbon
Adsorbent equipment 406, nitrobased NPK storage tank 407, preheating device 501, hydrogenation reactor 502, cooling device 503, gas-liquid separator point
From 504, amino T acid storage tanks 505, filter 506, the effect adverse current enrichment facility 602, dense T acid bufferings of the second preheating device 601,5
The effect adverse current of tank 603,2 enrichment facility 604, alkali solution surge tank 605, heat exchanger 701, alkali-melting vessel 702, preheater 703, the 3rd pump
704th, dilution kettle 705, condensate recycling device 706, stripper 707, methanol recovery device 708, alkali fusion thing surge tank 709, complex acid
Device 801, the second dilute sulfuric acid surge tank 802, separation kettle 803, the second cooling device 804, cooling reactor 805, filter 806, two
Oxidation sulfur recovery unit 807, wash water tank 808, wastewater treatment equipment 809.
Specific embodiment
With reference to embodiment, technical scheme is described in detail.
As shown in figure 1, a kind of H- acid preparation facilities with energy-saving effect of the embodiment of the present invention, the device is including extracting
Device 4, reduction apparatus 5, enrichment facility 6, dilution device 7, isolation and filter 8.The outlet of xanthator 1 and nitrification installation
2 import connection, the outlet of nitrification installation 2 is connected with the import of denitrification apparatus 3, outlet and the extraction equipment 4 of denitrification apparatus 3
Import is connected, and the first outlet of extraction equipment 4 is connected with the import of reduction apparatus 5, outlet and the enrichment facility 6 of reduction apparatus 5
Import connection, the outlet of enrichment facility 6 be connected with the import of dilution device 7, and the outlet of dilution device 7 and isolation and filtering is filled
Put 8 the first import connection, the second import of isolation and filter 8 and the second outlet connection of extraction equipment 4.
Above-described embodiment is by xanthator 1, nitrification installation 2, denitrification apparatus 3, extraction equipment 4, reduction apparatus 5, concentration
Device 6, dilution device 7, isolation and filter 8, drying device 9 are obtained H- acid.Have using device production H- acid continuous
Property.Closed reaction is used simultaneously, reduces the uncontrollable discharge of waste gas and waste liquid.
The present embodiment replaces crude salt analysis technique using solvent extraction technology, has not only saved a large amount of neutralization ammoniacal liquor, and subtract
The generation of T- acid isolation waste water is lacked.Meanwhile, the second import of isolation and filter 8 and the second outlet of extraction equipment 4 connect
Connect, the sulfuric acid that the dilute sulfuric acid that will be produced in extraction equipment 4 is used to isolate with filter 8, decrease H- acid isolations is used
Amount.Only this step can make yield improve about 10%, while saving substantial amounts of resource consumption.The present embodiment is clear using hydrogenating reduction
Clean production technology replaces iron powder reducing, product yield to improve about 3%, thoroughly eliminate the generation of iron cement, and about 60,000 can be reduced every year
The generation of ton above iron cement.
In above-described embodiment, extraction equipment 4 carries out extraction processing to denitration thing, obtains dilute sulfuric acid and extraction mixture, and
Extraction mixture is stripped, nitrobased NPK solution is obtained.Preferably, as shown in figure 1, described extraction equipment 4
Including the second pump 401, extraction reactor 402, first cooling with activated carbon adsorption unit 403, the first dilute sulfuric acid surge tank 404,
The cooling of back extraction reactor 405, second and activated carbon adsorption unit 406, nitrobased NPK storage tank 407；The import of the second pump 401 with
The outlet connection of denitration thing surge tank 303, the outlet of the second pump 401 is connected with the first import of extraction reactor 402, and extraction is anti-
The first outlet of device 402 is answered to be connected with the import of activated carbon adsorption unit 403 with the first cooling, first cools down and active carbon adsorption
The outlet of device 403 is connected with the import of the first dilute sulfuric acid surge tank 404；The second outlet of extraction reactor 402 and back extraction
The import connection of reactor 405, is stripped the first outlet and the second cooling and activated carbon adsorption unit 406 of reactor 405
Import is connected, and the second cooling is connected with the outlet of activated carbon adsorption unit 406 with the import of nitrobased NPK storage tank 407；Back extraction is negated
The second outlet of device 405 is answered to be connected with the second import of extraction reactor 402.
When extraction equipment 4 works, denitration thing, extractant and the water that denitrification apparatus 3 are generated continue through the second pump 401 and send
Enter extraction reactor 402, through four-stage counter-current extractive reaction after, obtain extract mixture and dilute sulfuric acid.Dilute sulfuric acid is cold through first
But after being processed with activated carbon adsorption unit 403, store in the first dilute sulfuric acid surge tank 404.Extraction mixture liquid caustic soda is existed
It is stripped in back extraction reactor 405, extractant and nitrobased NPK solution is obtained, by extractant by being stripped reactor
405 second outlet is returned in extraction reactor 402, carries out extractive reaction, and by nitrobased NPK solution through the second cooling and activity
After the treatment of carbon adsorption device 406, in delivering to nitrobased NPK storage tank 407.
Extractant selects TEHA, and molecular formula formula is：C24H51N.Extraction process and back extraction process are expressed with chemical equation
It is as follows：
In reactor 405 is stripped, after carrying out back extraction treatment, the extractant that will be generated returns to extraction reactor 402
In, carry out extractive reaction.Thus greatly save the extractant quantity needed during extractive reaction so that extractant is even
During continuous production H- acid, can reuse, reduce cost.
In above-described embodiment, reduction apparatus 5 are used to carry out reduction treatment to nitrobased NPK solution, obtain amino T acid solutions.
As shown in figure 1, described reduction apparatus 5 include preheating device 501, hydrogenation reactor 502, cooling device 503, gas-liquid separator
Separate 504, amino T acid storage tanks 505, filter 506.The material inlet of preheating device 501 goes out with nitrobased NPK storage tank 407
Mouthful connection, the outlet of preheating device 501 is connected with the first import of hydrogenation reactor 502, the outlet of hydrogenation reactor 502 with it is cold
But the import connection of device 503, the material outlet of cooling device 503 is connected with the import of gas-liquid separator separates 504, gas-liquid point
From device separate 504 liquid outlet be connected with the import of amino T acid storage tanks 505, the gas vent of gas-liquid separator separates 504 and
The import connection of filter 506, the outlet of filter 506 is connected with the second import of hydrogenation reactor 502.
When reduction apparatus 5 work, by catalyst, hydrogen, nitrobased NPK solution after preheating device 501 is preheated, deliver to and add
In hydrogen reactor 502, hydrogenation reduction is carried out under 170 DEG C, 20MPa.After reaction terminates, material is cooled to 90 with water
DEG C, obtain reactant mixture.In cooling device 503, the hot water produced after cooling is used for amino T acid preheating in subsequent step.Will
Reactant mixture is separated through gas-liquid separator 504, and after release, obtains amino T acid solutions and catalyst.By amino T acid solutions
In delivering to amino T acid storage tanks 505.Catalyst is reclaimed using filter 506, and it is anti-that the catalyst of recovery is recycled and reused for into hydrogenation
In answering device 502.
Preferably, catalyst is Raney's nickel.The chemical equation occurred in reduction apparatus 5 is expressed as follows：
In reduction apparatus 5, after material is cooled into 90 DEG C with water, water becomes hot water, can be used for ammonia in subsequent step
Base T acid preheatings.So be conducive to saving heat energy source.In addition, reclaiming catalyst, and the catalyst weight that will be reclaimed using filtration system
It is multiplexed in hydrogenation reactor, during continuous production H- acid, makes full use of existing material, and is reused,
Advantageously reduce cost.
In above-described embodiment, enrichment facility 6 is used to carry out concentration respectively to amino T acid solutions and liquid caustic soda, obtains dense
Amino T acid solutions and liquid caustic soda after contracting.As shown in figure 1, described enrichment facility 6 includes that the second preheating device 601,5 imitates adverse current
Enrichment facility 602, dense T acid bufferings tank 603,2 effect adverse current enrichment facility 604, alkali solution surge tank 605.Second preheating device 601
The first import be connected with the delivery port of cooling device 503, the second import of the second preheating device 601 and amino T acid storage tanks 505
Outlet connection, the outlet of the second preheating device 601 be connected with the import of 5 effect adverse current enrichment facilities 602, and 5 effect adverse currents are concentrated and filled
The outlet for putting 602 is connected with the import of dense T acid bufferings tank 603；The outlet of 2 effect adverse current enrichment facilities 604 and alkali solution surge tank
605 import connection.
When enrichment facility 6 works, the hot water flowed out using the delivery port of cooling device 503 is preheated, through 5 to amino T acid solutions
Effect adverse current enrichment facility 602 is concentrated into setting concentration, is then sent in dense T acid bufferings tank 603.Liquid caustic soda is concentrated through 2 effect adverse currents
Device 604 is concentrated into the liquid caustic soda that mass concentration is 72%, is then sent in alkali solution surge tank 605.
In above-described embodiment, amino T acid solutions and liquid caustic soda after 7 pairs of concentrations of dilution device carry out alkali fusion treatment, and carry out
Dilution is processed, the alkali fusion thing after being diluted.As shown in figure 1, described dilution device 7 include heat exchanger 701, alkali-melting vessel 702,
Preheater 703, the 3rd pump 704, dilution kettle 705, condensate recycling device 706, stripper 707, methanol recovery device 708 and alkali fusion
Thing surge tank 709.The import of described heat exchanger 701 is connected with the outlet of alkali solution surge tank 605, the outlet of heat exchanger 701
It is connected with the first import of alkali-melting vessel 702, the outlet of dense T acid bufferings tank 603 is connected with the second entrance of preheater 703；Preheating
The outlet of device 703 is connected by the 3rd pump 704 with the second import of alkali-melting vessel 702, outlet and the dilution kettle 705 of alkali-melting vessel 702
Import connection, the methanol outlet for diluting kettle 705 is connected with the import of condensate recycling device 706, and condensate recycling device 706 goes out
Mouth is connected with the first import of methanol recovery device 708；The alkali fusion thing outlet for diluting kettle 705 is connected with the entrance of stripper 707,
The methanol outlet of stripper 707 is connected with the second import of methanol recovery device 708, the outlet of methanol recovery device 708 with it is pre-
The import of hot device 703 first is connected；The alkali fusion thing outlet of stripper 707 is connected with the import of alkali fusion thing surge tank 709.
When dilution device 7 works, the liquid caustic soda after concentration is preheated to 180 DEG C through heat exchanger 701, is then fed into alkali-melting vessel
In 702, after then the amino T acid solutions after methyl alcohol and concentration are preheated by preheater 703 respectively, by the pump of the 3rd pump 704
Enter alkali-melting vessel 702, liquid caustic soda, methyl alcohol and amino T acid solutions are reacted under 200 DEG C, 2.8MPa, after reaction terminates, by material
It is diluted with water in press-in dilution kettle 705, obtains the alkali fusion thing after dilute methanol and dilution.Condensed back by condensate recycling device 706
The dilute methanol that receipts are steamed, the alkali fusion thing after dilution reclaims residual methanol through stripper 707.Dilute methanol is delivered into methanol recovery device
In 708, and methanol recovery device 708 is connected with the import of preheater 703 first, the methyl alcohol for that will reclaim is used for next time
Alkali fusion reacts.By in the alkali fusion thing feeding alkali fusion thing surge tank 709 after dilution.
The chemical equation occurred in dilution device 7 is expressed as follows：
In above-described embodiment, the alkali fusion thing after the 8 pairs of dilutions of isolation and filter is isolated and filtration treatment, is obtained
H- acidleach cakes.As shown in figure 1, described isolation and filter 8 include acid preparing device 801, the second dilute sulfuric acid surge tank 802,
Separation kettle 803, the second cooling device 804, cooling reactor 805, filter 806, sulfur dioxide recovery device 807, wash water tank 808,
Wastewater treatment equipment 809.The import of acid preparing device 801 is connected with the outlet of the first dilute sulfuric acid surge tank 404, acid preparing device 801
Outlet be connected with the import of the second dilute sulfuric acid surge tank 802, the outlet of the second dilute sulfuric acid surge tank 802 and separation kettle 803
First import is connected, and the second import of separation kettle 803 and the outlet of alkali fusion thing surge tank 709 are connected, the titanium dioxide of separation kettle 803
Sulphur exports the import connection with the second cooling device 804, the outlet of the second cooling device 804 and sulfur dioxide recovery device 807
Import connection, the material outlet of separation kettle 803 is connected with the import of cooling reactor 805, the outlet of cooling reactor 805 and filter
806 entrance connection, the entrance connection of the first outlet and wash water tank 808 of filter 806, outlet and the isolation of wash water tank 808
The triple feed inlet connection of kettle 803, the import connection of the second outlet and wastewater treatment equipment 809 of filter 806, filter 806
The 3rd outlet and drying device 9 import connect.
When isolation and filter 8 work, carry out first with acid treatment：By the dilute sulphur in the first dilute sulfuric acid surge tank 404
Acid, mixes in acid preparing device 801 with the sulfuric acid that mass concentration is 98%, cools down, and is made into the dilute sulfuric acid of setting concentration, and send into
In second dilute sulfuric acid surge tank 802.Then isolation treatment is carried out：By the alkali fusion thing in alkali fusion thing surge tank 709, H- acid washing waters and
Dilute sulfuric acid in second dilute sulfuric acid surge tank 802, to deliver to and carry out isolation treatment in separation kettle 803, and the sulfur dioxide of generation is through
After two cooling device 804 is cooled down, liquefied by sulfur dioxide recovery device 807 and reclaimed.Finally cooled down and filtration treatment：Will
Material after isolation treatment, through the continuous coo1ing of cooling reactor 805 to 50 DEG C, is filtered with filter 806, washed, and obtains H- acid
Filter cake, wash water and mother liquor, by wash water storage in wash water tank 808, use for the treatment of isolation next time；Mother liquor is delivered at waste water
In reason device 809.
The chemical equation occurred in isolation and filter 8 is expressed as follows：
H2SO4+2NaOH→Na2SO4+2H2O
H2SO4+Na2SO3→Na2SO4+SO2+H2O
As shown in Fig. 2 described device also includes drying device 9.From the H- acidleach cakes that the 3rd outlet of filter 806 is leached
Treatment is dried into drying device 9, H- acid is obtained.H- acidleach cake can use heated-air drying in spin flash dryer,
Dry tail gas and enter air after cyclonic separation, bag-type dust；The H- acid finished products for obtaining, are then fed into subsequent packages operation.
When extraction equipment 4 is extracted to denitration thing, denitration thing is by liquid naphthalene is by xanthator 1, nitrification installation 2 and takes off
Nitre device 3 is made.
Xanthator 1 is used to generate sulfonated bodies.Preferably, as shown in figure 3, described xanthator 1 includes sulphur
Change kettle 101, surge tank 102, indexable sulfonation tower 103,104, three sulfonation towers 105 of sulfonation reactor and sulfonated bodies surge tank 106.
The outlet of sulphonation kettle 101 is connected with the import of surge tank 102, and the outlet of surge tank 102 connects with the import of indexable sulfonation tower 103
Connect, the outlet of indexable sulfonation tower 103 is connected with the import of sulfonation reactor 104, the outlet of sulfonation reactor 104 and three sulfonation
The import connection of tower 105, three outlets of sulfonation tower 105 are connected with the import of sulfonated bodies surge tank 106.
When above-mentioned xanthator 1 works, the sulfuric acid solution that liquid naphthalene and mass concentration are 100% is continuously added to sulphonation kettle
In 101, the temperature in sulphonation kettle 101 is 90 DEG C, carries out first time sulfonation.After the buffered tank of product after first time sulfonation
102 are continuously introduced into indexable sulfonation tower 103, and the temperature in indexable sulfonation tower 103 is 150 DEG C, carries out translocation reaction.Will be indexable anti-
The material that should complete, the sulfuric acid solution that mass concentration is 100% and the oleum that mass concentration is 65% are continuously introduced into sulfonation
In reactor 104, temperature is 65 DEG C in sulfonation reactor 104, carries out second sulfonation.By the material after the completion of second sulfonation
Three sulfonation towers 105 are delivered to oleum, the temperature in three sulfonation towers 105 is 150 DEG C, carries out third time sulfonation, generated
Sulfonated bodies, and will be stored in sulfonated bodies feeding sulfonated bodies surge tank 106.The chemical equation occurred in xanthator 1 is as follows：
Nitrification installation 2 is used to generate itrated compound.Preferably, as shown in figure 3, described nitrification installation 2 includes one
Level 201, two grades of nitrating pots 202 of nitrator and itrated compound surge tank 203, the import and sulfonation of one-level nitrator 201
The outlet connection of thing surge tank 106, the outlet of one-level nitrator 201 is connected with the import of two grades of nitrating pots 202, two grades of nitre
The outlet for changing kettle 202 is connected with the entrance of itrated compound surge tank 203.
During work, the nitric acid that the sulfonated bodies and mass concentration that are stored in sulfonated bodies surge tank 106 are 68% is continuously pumped into
In one-level nitrator 201, and in the case where water cooling is cooled down in 40 DEG C of nitrifications, then in overflow to two grades of nitrating pots 202, complete
Nitration reaction, stores in the itrated compound feeding itrated compound surge tank 203 that will be generated after reaction.
The chemical equation occurred in nitrification installation 2 is as follows：
Denitrification apparatus 3 are used to generate denitration thing.Preferably, as shown in figure 3, denitrification apparatus 3 include the first pump
301st, Benitration reactor 302 and denitration thing surge tank 303, the outlet of the first pump 301 connect with the first import of Benitration reactor 302
Connect, the second import of Benitration reactor 302 is connected with the outlet of itrated compound surge tank 203, the outlet of Benitration reactor 302 with it is de-
The import connection of nitre thing surge tank 303.
During work, water is squeezed into Benitration reactor 302 with pump 301, while the nitre that will be stored in itrated compound surge tank 203
In compound feeding Benitration reactor 302, homogeneous mixture of material generates denitration thing, after cooling, delays through denitration thing feeding denitration thing
Rush in tank 303.The nitrogen oxide gas produced during denitration reaction, it is condensed after use alkali lye, for example NaOH absorbs, and reaches
Air is entered after standard.
The basic principles, principal features and advantages of the present invention have been shown and described above.Those skilled in the art should
Understand, the present invention do not limited by above-mentioned specific embodiment, the description in above-mentioned specific embodiment and specification be intended merely into
One step illustrates principle of the invention, without departing from the spirit and scope of the present invention, the present invention also have various change and
Improve, these changes and improvements all fall within the protetion scope of the claimed invention.The scope of protection of present invention will by right
Ask book and its equivalent thereof.
Claims (2)
1. a kind of H- acid preparation facilities, it is characterised in that the device includes extraction equipment (4), reduction apparatus (5), enrichment facility
(6), dilution device (7), isolation and filter (8), the first outlet of extraction equipment (4) connect with the import of reduction apparatus (5)
Connect, the outlet of reduction apparatus (5) is connected with the import of enrichment facility (6), outlet and the dilution device (7) of enrichment facility (6)
Import is connected, and the outlet of dilution device (7) is connected with the first import of isolation and filter (8), isolates and filter (8)
The second import and extraction equipment (4) second outlet connection；
Described extraction equipment (4) includes the second pump (401), extraction reactor (402), the first cooling and activated carbon adsorption unit
(403), the first dilute sulfuric acid surge tank (404), back extraction reactor (405), second cooling with activated carbon adsorption unit (406),
Nitrobased NPK storage tank (407)；The import of the second pump (401) is connected with the outlet of denitration thing surge tank (303), the second pump (401)
Outlet is connected with the first import of extraction reactor (402), and the first outlet of extraction reactor (402) is cooled down and activity with first
The import connection of carbon adsorption device (403), the first cooling is buffered with the outlet of activated carbon adsorption unit (403) with the first dilute sulfuric acid
The import connection of tank (404)；The second outlet of extraction reactor (402) is connected with the import of back extraction reactor (405), is stripped
The first outlet for taking reactor (405) is connected with the second cooling with the import of activated carbon adsorption unit (406), and second cools down and live
The outlet of property carbon adsorption device (406) is connected with the import of nitrobased NPK storage tank (407)；The second of back extraction reactor (405) goes out
Mouth is connected with the second import of extraction reactor (402)；
Described reduction apparatus (5) include preheating device (501), hydrogenation reactor (502), cooling device (503), gas-liquid separation
Device separates (504), amino T acid storage tanks (505), filter (506), and material inlet and the nitrobased NPK of preheating device (501) are stored up
The outlet connection of tank (407), the outlet of preheating device (501) is connected with the first import of hydrogenation reactor (502), hydrogenation reaction
The outlet of device (502) is connected with the import of cooling device (503), material outlet and the gas-liquid separator point of cooling device (503)
Import from (504) is connected, and the liquid outlet of gas-liquid separator separates (504) is connected with the import of amino T acid storage tanks (505),
The gas vent of gas-liquid separator separates (504) is connected with the import of filter (506), the outlet of filter (506) with
The second import connection of hydrogenation reactor (502)；
Described enrichment facility (6) includes the second preheating device (601), 5 effects adverse current enrichment facility (602), dense T acid bufferings tank
(603), 2 effect adverse current enrichment facility (604), alkali solution surge tank (605), the first import of the second preheating device (601) with it is cold
But the delivery port connection of device (503), the second import of the second preheating device (601) connects with the outlet of amino T acid storage tanks (505)
Connect, the outlet of the second preheating device (601) is connected with the import of 5 effects adverse current enrichment facility (602), 5 effect adverse current enrichment facilities
(602) outlet is connected with the import of dense T acid bufferings tank (603)；The outlet of 2 effects adverse current enrichment facility (604) is delayed with alkali solution
Rush the import connection of tank (605)；
Described dilution device (7) includes heat exchanger (701), alkali-melting vessel (702), preheater (703), the 3rd pump (704), dilution
Kettle (705), condensate recycling device (706), stripper (707), methanol recovery device (708) and alkali fusion thing surge tank (709), institute
The import of the heat exchanger (701) stated is connected with the outlet of alkali solution surge tank (605), the outlet of heat exchanger (701) and alkali-melting vessel
(702) the first import connection, the outlet of dense T acid bufferings tank (603) is connected with the second entrance of preheater (703)；Preheater
(703) outlet is connected by the 3rd pump (704) with the second import of alkali-melting vessel (702), outlet and the dilution of alkali-melting vessel (702)
The import connection of kettle (705), the methanol outlet of dilution kettle (705) is connected with the import of condensate recycling device (706), and condensation is reclaimed
The outlet of device (706) is connected with the first import of methanol recovery device (708)；The alkali fusion thing outlet of dilution kettle (705) and vapour
The entrance connection of stripper (707), the methanol outlet of stripper (707) is connected with the second import of methanol recovery device (708), first
The outlet of alcohol retracting device (708) is connected with the import of preheater (703) first；The alkali fusion thing outlet of stripper (707) and alkali fusion
The import connection of thing surge tank (709)；
Described isolation and filter (8) include acid preparing device (801), the second dilute sulfuric acid surge tank (802), separation kettle
(803), the second cooling device (804), cooling reactor (805), filter (806), sulfur dioxide recovery device (807), wash water tank
(808), wastewater treatment equipment (809)；The import of acid preparing device (801) is connected with the outlet of the first dilute sulfuric acid surge tank (404),
The outlet of acid preparing device (801) is connected with the import of the second dilute sulfuric acid surge tank (802), the second dilute sulfuric acid surge tank (802)
Outlet and the first import of separation kettle (803) connection, the second import of separation kettle (803) and going out for alkali fusion thing surge tank (709)
Mouth connection, the sulfur dioxide outlet and the import of the second cooling device (804) of separation kettle (803) are connected, the second cooling device
(804) outlet and the import connection of sulfur dioxide recovery device (807), the material outlet and cooling reactor of separation kettle (803)
(805) import connection, the outlet of cooling reactor (805) and the entrance connection of filter (806), the first of filter (806) goes out
The entrance of mouth and wash water tank (808) is connected, and the outlet of wash water tank (808) is connected with the triple feed inlet of separation kettle (803), filter
(806) the import connection of second outlet and wastewater treatment equipment (809).
2. according to the H- acid preparation facilities described in claim 1, it is characterised in that also including drying device (9), drying device
(9) import and the 3rd outlet connection of filter (806).
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| CN201610113728.4A CN105753744B (en) | 2016-02-29 | 2016-02-29 | A kind of H acid preparation facilities with energy-saving effect |
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| CN201610113728.4A CN105753744B (en) | 2016-02-29 | 2016-02-29 | A kind of H acid preparation facilities with energy-saving effect |
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| CN105753744B true CN105753744B (en) | 2017-06-16 |
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| CN108191717A (en) * | 2017-11-27 | 2018-06-22 | 江苏力禾颜料有限公司 | H acid isolates preparation process |
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| US1670406A (en) * | 1925-05-09 | 1928-05-22 | Newport Co | Process of preparing h-acid |
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