CN207362101U - A kind of crude naphthalene fine-processing production line - Google Patents

Abstract

The utility model belongs to crude naphthalene finishing technology field, propose a kind of crude naphthalene fine-processing production line, including crude naphthalene groove, the lasting feed inlet being connected with pipeline and the steam inlet for keeping internal temperature to stablize for being passed through steam are provided with the crude naphthalene groove, waste gas spreading mouth is provided with the crude naphthalene groove, the waste gas spreading mouth successively with thin-walled condenser, sack cleaner connects, the dust collection mouth of the sack cleaner is connected with the feed inlet that continues, the crude naphthalene groove is connected with the first crystallization case, the first crystallization case is connected with the first cut groove, second cut groove, first semi-finished product tank.The utility model solves existing crude naphthalene finishing technology, the problem of having much room for improvement in production process in terms of resource utilization and environmental pollution.

Description

A kind of crude naphthalene fine-processing production line

Technical field

The utility model belongs to crude naphthalene finishing technology field, is related to a kind of crude naphthalene fine-processing production line.

Background technology

Naphthalene content in coal tar is about 8%~12%, in crude naphthalene in addition to containing naphthalene, also containing thia indenes, phenols, Quinolines and other unsaturated compounds.To obtain refined naphthalene, it is necessary to which crude naphthalene is further refined.Traditional crude naphthalene essence Technology method processed is pickling rectification method, and the process gradually to grow up has solvent method, catalytic hydrogenation method, zone-melting Crystallisation and Steppecd crystallization.In the various technology sides that crude naphthalene refines, pickling rectification method is traditional old technique, it is special Point is that product purity is not high, seriously corroded, and investment is big, waste water is difficult to handle.Due to these shortcomings, the traditional handicraft at present by Eliminate；Solvent process shortcoming is that solvent for use has certain toxicity, and equipment is more numerous and more jumbled, and refining effect is bad.At present, it is external very This method is used less, though domestic have this method production of the small station-service in several small towns, because of solvent price, solvent loss is big, product cost Height, is not also promoted；For catalytic hydrogenation method since technique is more complicated, capital construction and operating cost are higher, promote and apply more difficult. And have the generation of accessory substance naphthane, limit the scope of this naphthalene products application；Zone melting method produces refined naphthalene production technology Continuous flow procedure, product quality are stablized.But because its capital expenditure and operating cost are high, operating condition requirement is tighter, so It is not widely used also at home.Existing crude naphthalene finishing technology, resource utilization and environment in production process Have much room for improvement in terms of pollution.

Utility model content

The utility model proposes a kind of crude naphthalene fine-processing production line, solves the above problem of the prior art.

What the technical solution of the utility model was realized in：

A kind of crude naphthalene fine-processing production line, including

Crude naphthalene groove, the lasting feed inlet being connected with pipeline is provided with the crude naphthalene groove and is kept for being passed through steam The steam inlet that internal temperature is stablized, is provided with waste gas spreading mouth on the crude naphthalene groove, the waste gas spreading mouth successively with it is thin Wall condenser, sack cleaner connection, the dust collection mouth of the sack cleaner are connected with the feed inlet that continues,

The crude naphthalene groove is connected with the first crystallization case, and the first crystallization case is connected with the first cut groove, the second cut Groove, the first semi-finished product tank, the first cut groove are connected with building materials naphthalene transfer pipeline, the second cut groove and first knot The connection of brilliant case, first semi-finished product tank crystallize case with semi-finished product first and be connecteds, the crystallization case of semi-finished product first and described the Two cut grooves, first semi-finished product tank, the first pan tank connection, first pan tank be connected with beta naphthal production system and First slicer, first slicer are connected with the connection of the first packing machine, and the beta naphthal production system is connected with K acid productions System, the building materials naphthalene transfer pipeline are connected with water-reducing agent production system.

As further technical solution, the water-reducing agent production system includes what is be connected with the building materials naphthalene transfer pipeline Liquid naphthalene measuring tank, the liquid naphthalene measuring tank are connected with the first sulfonating reaction kettle, and the first sulfonating reaction kettle is connected with the first sulphur Sour measuring tank, the first hydrolytic reaction pot, first hydrolytic reaction pot are connected with the first condensation reaction kettle, and first condensation is anti- Kettle is answered to be connected with the second sulfuric acid gauge tank, the first formaldehyde measuring tank, the first neutralization reaction kettle, the first neutralization reaction kettle connection There are the first liquid caustic soda measuring tank, liquid water-reducing agent transfer pipeline, the first atomizer, the liquid water-reducing agent transfer pipeline and first are answered Connected with kettle, first atomizer is connected with the first drying tower, first drying tower and the first hot-blast stove, the first whirlwind point Connected from device, the first spiral discharging device, first cyclone separator and the first water dust scrubber, first spiral discharging device Connection, first spiral discharging device are connected with the first packing machine.

As further technical solution, first hydrolytic reaction pot is connected with the first metering sink, first meter Flume is connected with the condensation mouth of a river of the first triple effect evaporator, first triple effect evaporator and beta naphthal mother liquor conveying water lines Connection.

As further technical solution, the beta naphthal production system includes the refined naphthalene being connected with first pan tank Melting channel, the refined naphthalene melting channel are connected with sulfidation pan, and the sulfidation pan blows naphthalene pot and connect with the first sulfuric acid high position tank, hydrolysis Connect, first sulfuric acid high position tank is connected with the first sulfuric acid storage tank, and naphthalene pot and the first water measuring tank, the second liquid caustic soda are blown in the hydrolysis Measuring tank, steam pipework, the first naphthalene steam condenser, neutralization pot are all connected with, and the first naphthalene steam condenser and the first naphthalene return Receipts tower, the first drier are sequentially connected, and the recycling naphthalene mouth of first drier is connected with the sulfidation pan, and first naphthalene returns The separation mouth of a river of receipts tower is blown naphthalene pot with the hydrolysis and is connected,

The neutralization pot is boiled with the first cooling tank, the first suction filtration tank, alkal melting pan, dilution pot, the first acidifying pot, first Pot, the second boiling pot, the 3rd boiling pot, the first dry pot, the first distillation still are sequentially connected,

First suction filtration tank is connected with the first whizzer, first suction filtration tank also with naphthalene water trap, the 3rd Neutralization reaction kettle, the second triple effect evaporator are sequentially connected, concentrated solution outlet and the cooling nutsch filter of second triple effect evaporator Connection, the mother liquor outlet for cooling down nutsch filter is connected with the first equipment of crystallisation by cooling, precipitate exports and the first centrifugal device Connection, the sodium naphthalene sulfonate outlet of first centrifugal device are connected with alkali fusion device, the condensate liquid of second triple effect evaporator Outlet be connected with the alkali fusion device, the alkali fusion device with it is described dilute pot be connected, first equipment of crystallisation by cooling it is upper Purified liquor outlet is connected with second triple effect evaporator, crystallizes outlet is connected with the second centrifugal device, second centrifugal device Centrifugate outlet be connected with second triple effect evaporator,

The dilution pot is also connected by the second acidifying pot with first boiling pot, and the sulfur dioxide for neutralizing pot goes out Mouth is connected with the described second acidifying pot, the first acidifying pot successively.

As further technical solution, the outlet of the sodium sulfite solution of first boiling pot successively with sub- sodium cooling Groove, the connection of the first filter press, the first cake of filter-press outlet are connected with the dilution pot, the filter of first filter press Liquid outlet is sequentially connected with dnockout pumps, the 3rd triple effect evaporator, the second equipment of crystallisation by cooling, the 3rd whizzer, and described the Three whizzers are all connected with the 3rd triple effect evaporator, second equipment of crystallisation by cooling, the dnockout pumps also with Asia Sodium head tank connects.

New water is both provided with as further technical solution, on first boiling pot and the 3rd boiling pot to enter Mouthful, it is both provided with washing water outlet, the washing water outlet of second boiling pot on second boiling pot and the 3rd boiling pot It is connected with the dilution pot, the washing water outlet of the 3rd boiling pot is connected with second boiling pot.

As further technical solution, the steam outlet of first dry pot is connected with dry trap, described The condensation-water drain of dry trap is connected with condensation liquid storage tank, and first distillation still is connected with distillation trap, the steaming The condensation-water drain for evaporating trap is connected with the condensation liquid storage tank, and the condensation liquid storage tank is connected with the dilution pot.

As further technical solution, the first fraction outlets of first distillation still, the second fraction outlets, the 3rd evaporate Sub-export is connected with the 3rd cut groove, the second pan tank, the 4th cut groove respectively, the 3rd cut groove, the 4th cut Groove is connected with the 3rd boiling pot, and second pan tank is connected with section head tank, the section head tank and second Slicer, second package machine are sequentially connected.

As further technical solution, the K acid production system includes two be connected with the beta naphthal production system Secondary sulfonating reaction kettle, the kettle of sulfonating reaction twice are connected with kettle of saltouing, and the kettle of saltouing also connects with potassium sulfate solution measuring tank Connecing, the kettle of saltouing is connected with the second filter press,

The mother liquor outlet of second filter press is connected with the 4th neutralization reaction kettle, the 4th neutralization reaction kettle and the 4th Triple effect evaporator connects, and the condensate outlet of the 4th triple effect evaporator is connected with waste water processing station, and the 4th triple effect steams The concentrated solution outlet of hair device is connected by the 3rd equipment of crystallisation by cooling with the 4th centrifugal device, the centrifugation of the 4th centrifugal device Liquid outlet is connected with the 4th triple effect evaporator,

The second cake of filter-press outlet is connected with aminating reaction kettle, and sulfurous acid is provided with the aminating reaction kettle Hydrogen ammonium entrance and ammonia inlet, the aminating reaction kettle successively with deamination kettle, the 3rd acidifying kettle be connected, it is described 3rd acidifying kettle and Cooling separates out kettle, the 3rd filter press is sequentially connected, and the 3rd cake of filter-press outlet is connected with the 5th triple effect evaporator, filters Liquid outlet is connected with the 4th sulphonation kettle, and the concentrated solution outlet of the 5th triple effect evaporator connection is connected with the kettle of saltouing,

4th sulphonation kettle is connected by dilution trap with the 4th filter press, the K of the 4th filter press acid outlet and the Four packing machines connect.

The utility model use principle and have the beneficial effect that：

Above scheme improves resource utilization well, improve material balance while reduce caused by environment it is dirty Dye.

Brief description of the drawings

The utility model is described in further detail with reference to the accompanying drawings and detailed description.

Fig. 1 is the utility model process schematic representation；

Fig. 2 is water-reducing agent production system process schematic representation in the utility model；

Fig. 3 is a part of process schematic representation of beta naphthal production system in the utility model；

Fig. 4 is the another some processes schematic diagram of beta naphthal production system in the utility model；

Fig. 5 is beta naphthal production system another part process schematic representation in the utility model；

Fig. 6 is the another some processes schematic diagram of beta naphthal production system in the utility model；

Fig. 7 is K acid production system process schematic representations in the utility model；

In figure：1- crude naphthalene grooves, 2- water-reducing agent production systems, 3-2- naphthols production systems, 4-K acid production systems, 5- are thin Wall condenser, 6- sack cleaners, the crystallization casees of 7- first, 8- the first cut grooves, 9- the second cut grooves, the first semi-finished product tanks of 10-, 11- building materials naphthalene transfer pipelines, the first pan tanks of 12-, 13- continue feed inlet, 14- steam inlets, 15- waste gas spreading mouths, 16- One slicer, the first packing machines of 17-, 18- semi-finished product crystallization case, 201- liquid naphthalene measuring tanks, 202- the first sulfonating reaction kettles, 203- First sulfuric acid gauge tank, the first hydrolytic reaction pots of 204-, 205- the first condensation reaction kettles, the second sulfuric acid gauge tanks of 206-, 207- First formaldehyde measuring tank, 208- the first neutralization reaction kettles, 209- the first liquid caustic soda measuring tanks, 210- liquid water-reducing agent transfer pipelines, The first atomizers of 211-, 212- first compound kettle, the first drying towers of 213-, the first hot-blast stoves of 214-, the first cyclonic separations of 215- Device, the first spiral discharging devices of 216-, the first water dust scrubbers of 217-, the first packing machines of 218-, 219- first measure sink, 220- First triple effect evaporator, 221-2- naphthols mother liquor conveying water lines, 301- refined naphthalene melting channels, 302- sulfidation pans, the first sulphur of 303- Sour head tank, 304-, which is hydrolyzed, blows naphthalene pot, 305- the first sulfuric acid storage tanks, 306- the first water measuring tanks, 307- the second liquid caustic soda measuring tanks, 308- steam pipeworks, 309- the first naphthalene steam condensers, in 310- and pot, 311- the first naphthalene recovery towers, the first driers of 312-, The first cooling tanks of 313-, the first suction filtration tanks of 314-, 315- alkal melting pans, 316- dilution pots, 317- first are acidified pot, and 318- first is boiled Boiling pot, the second boiling pots of 319-, the 3rd boiling pots of 320-, the first dry pots of 321-, the first distillation stills of 322-, 323- first are centrifuged Separator, 324- naphthalene water traps, the 3rd neutralization reaction kettles of 325-, the second triple effect evaporators of 326-, 327- cooling nutsch filters, The first equipment of crystallisation by cooling of 328-, the first centrifugal devices of 329-, 330- alkali fusion devices, the second centrifugal devices of 331-, 332- second Acidifying pot, 333- Asias sodium cooling groove, the first filter presses of 334-, 335- dnockout pumpss, the 3rd triple effect evaporators of 336-, 337- second are cold But crystallization apparatus, the 3rd whizzers of 338-, 339- Asias sodium head tank, the new water inlets of 340-, 341- washing water outlets, 342- are done Dry trap, 343- condensation liquid storage tanks, 344- distillation traps, the 3rd cut grooves of 345-, the second pan tanks of 346-, 347- the 4th Cut groove, 348- section head tanks, the second slicers of 349-, 350- second package machines, 401- sulfonating reaction kettles twice, 402- salt Analyse kettle, 403- potassium sulfate solution measuring tanks, the second filter presses of 404-, the 4th neutralization reaction kettles of 405-, the 4th triple effect evaporations of 406- Device, 407- waste water processing stations, the 3rd equipment of crystallisation by cooling of 408-, the 4th centrifugal devices of 409-, 410- aminating reaction kettles, 411- are sub- Ammonium hydrogen sulfate entrance, 412- ammonia inlets, 413- the 3rd are acidified kettle, and 414- coolings separate out kettle, the 3rd filter presses of 415-, 416- the Five triple effect evaporators, the 4th sulphonation kettles of 417-, 418- dilution traps, the 4th filter presses of 419-, the 4th packing machines of 420-, 421- deaminations Kettle.

Embodiment

The following is a combination of the drawings in the embodiments of the present utility model, and the technical scheme in the embodiment of the utility model is carried out Clearly and completely describe, it is clear that the described embodiments are only a part of the embodiments of the utility model, rather than whole Embodiment.Based on the embodiment in the utility model, those of ordinary skill in the art are without creative efforts All other embodiments obtained, shall fall within the protection scope of the present invention.

As shown in Fig. 1~Fig. 7, the utility model proposes a kind of crude naphthalene fine-processing production line, including crude naphthalene groove 1, The lasting feed inlet 13 being connected with pipeline and the steam for keeping internal temperature to stablize for being passed through steam are provided with crude naphthalene groove 1 Entrance 14, is provided with waste gas spreading mouth 15 on crude naphthalene groove 1, waste gas spreading mouth 15 successively with thin-walled condenser 5, sack cleaner 6 connections, the dust collection mouth of sack cleaner 6 are connected with continuing feed inlet 13,

Crude naphthalene groove 1 with first crystallization case 7 be connected, first crystallization case 7 be connected with the first cut groove 8, the second cut groove 9, First semi-finished product tank 10, the first cut groove 8 are connected with building materials naphthalene transfer pipeline 11, and the second cut groove 9 connects with the first crystallization case 7 Connect, the first semi-finished product tank 10 is connected with semi-finished product crystallization case 18,18 and second cut groove 9 of semi-finished product crystallization case, the first semi-finished product Groove 10, the first pan tank 12 connect, and the first pan tank 12 is connected with 3 and first slicer 16 of beta naphthal production system, and first cuts Piece machine 16 is connected with the first packing machine 17 and connects, and beta naphthal production system 3 is connected with K acid production system 4, building materials naphthalene transfer pipeline 11 are connected with water-reducing agent production system 2.

In the utility model, the refined naphthalene of production is melted crude naphthalene again using the physical characteristic of naphthalene using crude naphthalene as raw material Cooling restructuring, re-melting fractionation, and repeat multistage fractionation and obtain product refined naphthalene, crude naphthalene is directly by carbon black company in pipeline Conveying is continuously delivered into crude naphthalene groove 1 by lasting feed inlet 13, therefore can continue uninterruptedly to produce, without a collection of Carry out, be closed type in groove, be provided with heating coil, being passed through saturated vapor by the steam inlet 14 on crude naphthalene groove 1 protects Temperature is held more than 80 DEG C, holding crude naphthalene is liquid phase state, while the exhaust gas containing naphthalene of crude naphthalene groove 1 is drawn by waste gas spreading mouth 15 Go out, first pass through thin-walled condenser 5 and be condensed into naphthalene powder, purified treatment then is carried out to exhaust gas by sack cleaner 6, and pocket type removes The dust collection mouth of dirt device 6 is connected with continuing feed inlet 13, and the naphthalene dirt of mobile phone is back to crude naphthalene groove 1 is recycled, Therefore it can realize that good material utilizes, and the pollution to environment has been also reduced to minimum, realizes clean raw well Production.Afterwards, crude naphthalene is pumped to the first crystallization case 7 (80 DEG C of ＞) by crude naphthalene groove 1 by submerged pump and carries out primary crystal fractionation, Recirculated cooling water is passed through in the crystallization case tubulation of first crystallization case 7, liquid industrial naphthalene is cooled to 70 with the rate of temperature fall of 2 DEG C/h DEG C, make its crystallization, be then passed through hot water again in the crystallization case tubulation of the first crystallization case 7, crystal is heated with the heating rate of 4 DEG C/h Naphthalene, while the fractionation into the first cut groove 8 (75~80 DEG C of cuts) by naphthalene liquid, when naphthalene liquid is warming up to 80 DEG C, naphthalene liquid is turned to Second cut groove 9 (80 DEG C of cuts of ＞) strains material, and final naphthalene liquid temperature degree is maintained at 81~82 DEG C, to first crystallization 7 lower floor's material of case Crystalline temperature is 79 DEG C, and naphthalene liquid is gone to the first semi-finished product tank 10, and it is cold that circulation is passed through in the crystallization case tubulation of the first semi-finished product tank 10 But semi-finished product naphthalene liquid is down to 72 DEG C by water with the rate of temperature fall of 2 DEG C/h, makes its crystallization, then is passed through hot water with the heating speed of 2 DEG C/h Rate heats up crystal naphthalene, while strains material to the second cut groove 9 (80 DEG C of cuts of ＞), to 80 DEG C when first semi-finished product tank 10 that alters course strain Material, final naphthalene liquid temperature degree are maintained at 82 DEG C or so, take orlop material assay, and crystalline temperature turns to naphthalene liquid when being 79.3 DEG C First pan tank, 12 blowing, after roller crystallisation by cooling, sheet is cut into by the first slicer 16, then by the first packing machine 17 into Row is packed as far as possible, while the cut of the first cut groove 8 is delivered to water-reducing agent production system 2 by building materials naphthalene transfer pipeline 11 and is subtracted The production of aqua, the cut of the first pan tank 12 send to beta naphthal production system 3 production for carrying out beta naphthal, beta naphthal production system System 3 is also associated with the production of progress K acid after K acid production system 4, and good Matter Transfer is realized by this process, improves The utilization rate of material, and pollution sources masters will be that naphthalene heats fusing in crystallization case, diversion channel, semi-finished product tank, pan tank a bit The steam containing naphthalene that process produces, and the naphthalene dirt that slicer and packing machine produce, pump making an uproar for the generations such as class, slicer, packing machine Sound, after the naphthalene steam produced in production process is collected by pipeline, is condensed into naphthalene dirt through thin-walled condenser, is then sent to pocket type and removes Dirt device purified treatment so that purified treatment can also be carried out by condensing the solid naphthalene of recycling, therefore improve material utilization well, and Reduce pollution, while production equipment of making an uproar is distributed on progress noise reduction isolation in workshop, it is overall so that production environment has obtained greatly Improvement, realize good effect.

As further technical solution, water-reducing agent production system 2 includes the liquid naphthalene being connected with building materials naphthalene transfer pipeline 11 Measuring tank 201, liquid naphthalene measuring tank 201 are connected with the first sulfonating reaction kettle 202, and the first sulfonating reaction kettle 202 is connected with the first sulphur Sour measuring tank 203, the first hydrolytic reaction pot 204, the first hydrolytic reaction pot 204 are connected with the first condensation reaction kettle 205, the first contracting Close reaction kettle 205 and be connected with the second sulfuric acid gauge tank 206, the first formaldehyde measuring tank 207, the first neutralization reaction kettle 208, in first The first liquid caustic soda measuring tank 209, liquid water-reducing agent transfer pipeline 210, the first atomizer 211 are connected with reaction kettle 208, liquid subtracts Aqua transfer pipeline 210 is connected with the first compounding kettle 212, and the first atomizer 211 is connected with the first drying tower 213, the first drying Tower 213 is connected with the first hot-blast stove 214, the first cyclone separator 215, the first spiral discharging device 216, the first cyclone separator 215 are connected with the first water dust scrubber 217, the first spiral discharging device 216, the first spiral discharging device 216 and the first packing machine 218 Connection.

As further technical solution, the first hydrolytic reaction pot 204 is connected with the first metering sink 219, the first metering Sink 219 is connected with the condensation mouth of a river of the first triple effect evaporator 220, the first triple effect evaporator 220 and beta naphthal mother liquor conveying water Pipeline 221, which connects, (by the water conservancy that production process in beta naphthal production line produces hydrolysis here, to be realized well Water resource utilization).

In the utility model, for water-reducing agent production system 2 using building materials naphthalene as primary raw material, system passes through sulfonation, hydrolysis, contracting The target product that process is produced well such as close, neutralize, is dry, and the yield of the system production can improve to 86.5% with On, building materials naphthalene is delivered to liquid naphthalene measuring tank 201 located underground by building materials naphthalene transfer pipeline 11, and when production is sent by submerged pump Enter the first sulfonating reaction kettle 202, while according to naphthalene after 98% concentrated sulfuric acid is measured by the first sulfuric acid gauge tank 203：Sulfuric acid ≈ 1:The ratio of 1.3 (molar ratios), is slowly added to after metering to the first sulfonating reaction kettle 202, while the first sulfonating reaction kettle 202 Chuck in be passed through steam, temperature of reaction kettle is risen to 160~165 DEG C of closed normal pressure sulfonation, by accurate temperature control and Material is added than making the completion of sulfonating reaction in high yield, and the exhaust gas containing naphthalene, sulfuric acid discharged during simultaneous reactions passes through closed Pipeline is sent to scrubbing tower purified treatment, and the noise that product pump produces also is isolated so that whole system can keep preferable Production status.After sulfonating reaction, the accessory substance (α-naphthalenesulfonicacid) contained in reaction mixture is as far as possible by the first water The hydrolysis of solution reaction kettle 204 removes, and the characteristic of hydrolysis is easier to using side reaction thing and realizes purity and yield well Raising, sulfonating reaction product by react carry steam press-in condensation kettle, carried out in the environment of 120 DEG C, due to a upper process In temperature it is higher (165 DEG C), therefore realize the progress of hydrolysis well, 204 temperature of the first hydrolytic reaction pot is cold by circulating But after water cooling, the condensed water being sent at the condensation mouth of a river of the first triple effect evaporator 220 is added by the first metering sink 219, because To mainly contain naphthalene sulfonic acids (sodium) in condensed water, be before hydrolysis in material i.e. existing for material, therefore hydrolysis will not be produced It is raw to influence, therefore this partial condensation water has been subjected to good utilization, the utilization rate for improving water improves production efficiency at the same time, In addition, sulfonating reaction occurs again in high temperature environments for part naphthalene and the sulfuric acid of hydrolysis generation, and based on can part naphthalene be converted Product (beta-naphthalenesulfonic-acid), by the adjustment of hydrolysis, can cause the overall reaction yield of beta-naphthalenesulfonic-acid to reach more than 88%.It Condensation reaction afterwards carries out in the first condensation reaction kettle 205, before reaction, is measured first in hydrolysate by the second sulfuric acid Groove 206 adds a certain amount of 98% sulfuric acid, and acidity is brought up to 30% or so, makes condensation reaction be easier to carry out, and reaction is more Completely, the quality of product is finally improved, hydrolyzate is warming up to 120 DEG C with steam with the speed of 1 DEG C/min, while formaldehyde is through defeated Send and be pumped to the first formaldehyde measuring tank 207, according to formaldehyde：Building materials naphthalene=1：Condensation kettle is added after 7 ratio (mass ratio) metering In, formaldehyde is converted into the stronger carbonyl ion of reactivity under the catalytic action of acid, and electrophilic contracting then occurs with beta-naphthalenesulfonic-acid again Reaction is closed, ultimately generates beta-naphthalenesulfonic-acid formaldehyde condensation compound, a small amount of formaldehyde of pollutant and sulfuric acid mist which produces, by closed Pipeline is sent to scrubbing tower so as to fulfill purification, while the equipment for producing noise is carried out sound insulation, can reach cleanliness without any pollution production Purpose.Neutralization reaction is carried out in the first neutralization reaction kettle 208 afterwards, is added in right amount by the first liquid caustic soda measuring tank 209 thoroughly NaOH solution neutralization reaction occurs therewith, naphthalene sulfonic acids is converted into sodium salt, while the sulfuric acid of neutralization reaction, final neutralization production 7~9 or so, neutralization reaction is crossed by controlling amount of water for thing pH controls, material concentration is maintained at 50%, while by material temperature Degree is down to less than 80 DEG C so that the part naphthalene solidification produced in hydrolyzing process, after the completion of neutralization, part neutralizer subtracts by liquid Aqua transfer pipeline 210 is delivered to the first compounding kettle 212, while is diluted with water to concentration 40% or so, obtains liquid concrete Water-reducing agent, remainder neutralizer are pumped into head tank after filtering, send for producing solid water-reducing agent, filter consolidating for generation State naphthalene, send naphthalene groove to re-use.Solid water-reducing agent is sent into the first drying tower 213 and is dried afterwards, because finished product feed liquid moisture Higher, 50% or so, therefore drying is essential, and feed liquid is sent into the first drying tower 213 by feed pump first, into tower it The first atomizer 211 of preceding increase further improves efficiency, while the heat smoke blasted by the first hot-blast stove 214 is through hot-air distributor Be sent into the first atomizer 211, atomization feed liquid hot wind effect under (350 DEG C) be dried, dried material have 90% from First drying tower, 213 the first spiral discharging device of lower part 216 and Pneumatic conveyer send to the first packing machine 218 and carry out sacker Sequence, remainder enter the first cyclone separator 215 with dry waste gas, product are further recycled through the first cyclone separator 215, Liquid is sent out by the first spiral discharging device 216 and is packed, and dried moisture content of finished products is about 5%, so as to meet product quality The requirement of middle solid content >=90%, the production process of whole water-reducing agent is scientific and reasonable, realizes the good utilization of resources, reaches Good effect.

As further technical solution, beta naphthal production system 3 includes the refined naphthalene fusing being connected with the first pan tank 12 Groove 301, refined naphthalene melting channel 301 are connected with sulfidation pan 302, and naphthalene pot 304 is blown in 302 and first sulfuric acid high position tank 303 of sulfidation pan, hydrolysis Be all connected with, the first sulfuric acid high position tank 303 is connected with the first sulfuric acid storage tank 305, hydrolysis blow 304 and first water measuring tank 306 of naphthalene pot, Second liquid caustic soda measuring tank 307, steam pipework 308, the first naphthalene steam condenser 309, neutralization pot 310 are all connected with, the first naphthalene steam Condenser 309 is sequentially connected with the first naphthalene recovery tower 311, the first drier 312, the recycling naphthalene mouth and sulphur of the first drier 312 To change pot 302 to connect, the separation mouth of a river and the hydrolysis of the first naphthalene recovery tower 311 are blown naphthalene pot 304 and are connected,

Neutralize 310 and first cooling tank 313 of pot, the first suction filtration tank 314, alkal melting pan 315, dilution pot 316, first and be acidified pot 317th, the first boiling pot 318, the second boiling pot 319, the 3rd boiling pot 320, the first dry pot 321, the first distillation still 322 be successively Connection,

First suction filtration tank 314 is connected with the first whizzer 323, the first suction filtration tank 314 also with naphthalene water trap 324, 3rd neutralization reaction kettle 325, the second triple effect evaporator 326 are sequentially connected, the concentrated solution outlet of the second triple effect evaporator 326 with it is cold But nutsch filter 327 connects, cooling nutsch filter 327 mother liquor outlet be connected with the first equipment of crystallisation by cooling 328, precipitate outlet and First centrifugal device 329 connects, and the sodium naphthalene sulfonate outlet of the first centrifugal device 329 is connected with alkali fusion device 330, and the second triple effect steams The condensate outlet of hair device 326 is connected with alkali fusion device 330, and alkali fusion device 330 is connected with dilution pot 316, the first crystallisation by cooling The supernatant outlet of device 328 is connected with the second triple effect evaporator 326, crystallizes outlet is connected with the second centrifugal device 331, and second The centrifugate outlet of centrifugal device 331 is connected with the second triple effect evaporator 326,

Dilution pot 316 is also connected by the second acidifying pot 332 with the first boiling pot 318, and the sulfur dioxide for neutralizing pot 310 goes out Mouth is acidified pot 317 with the second acidifying pot 332, first successively and is connected,

As further technical solution, the outlet of the sodium sulfite solution of the first boiling pot 318 successively with sub- sodium cooling groove 333rd, the first filter press 334 connects, and the filtered solid outlet of the first filter press 334 is connected with dilution pot 316, the first filter press 334 Filtrate (liquid and dnockout pumps 335, the 3rd triple effect evaporator 336, the second equipment of crystallisation by cooling 337, the 3rd whizzer 338 according to Secondary connection, the 3rd whizzer 338 are all connected with the 3rd triple effect evaporator 336, the second equipment of crystallisation by cooling 337, dnockout pumps 335 are also connected with sub- sodium head tank 339.

As further technical solution, new water inlet is both provided with the first boiling pot 318 and the 3rd boiling pot 320 340, washing water outlet 341, the washing water outlet of the second boiling pot 319 are both provided with the second boiling pot 319 and the 3rd boiling pot 320 341 are connected with dilution pot 316, and the washing water outlet 341 of the 3rd boiling pot 320 is connected with the second boiling pot 319.

As further technical solution, the steam outlet of the first dry pot 321 is connected with dry trap 342, is done The condensation-water drain of dry trap 342 is connected with condensation liquid storage tank 343, and the first distillation still 322 is connected with distillation trap 344, The condensation-water drain for distilling trap 344 is connected with condensation liquid storage tank 343, and condensation liquid storage tank 343 is connected with dilution pot 316.

As further technical solution, the first fraction outlets of the first distillation still 322, the second fraction outlets, the 3rd evaporate Sub-export is connected with the 3rd cut groove 345, the second pan tank 346, the 4th cut groove 347 respectively, the 3rd cut groove the 345, the 4th Cut groove 347 is connected with the 3rd boiling pot 320, and the second pan tank 346 is connected with section head tank 348, head tank 348 of cutting into slices It is sequentially connected with the second slicer 349, second package machine 350.

In the utility model, beta naphthal production system 3 uses naphthalene sulfonated alkali fusion method, is original with refined naphthalene, sulfuric acid, caustic soda etc. Material, it is sulfonated, hydrolyze, blow naphthalene, neutralization, suction filtration, alkali fusion, be acidified, boil, press filtration, drying, distillation, the process such as section, pass through The improvement of system, can improve total yield of products to the production of more than 78.8%, 2- naphthalene powder with the essence in the first pan tank 12 Naphthalene is primary raw material, and through pipeline to refined naphthalene melting channel 301, using steam heating and thermal insulation, liquid naphthalene is sent to sulphur by head tank again Change pot 302, it is heated using the steam jacket of sulfidation pan 302, liquid naphthalene temperature is risen to 120 DEG C, subsequent first sulfuric acid is high-order 98% concentrated sulfuric acid in groove 303 is according to naphthalene：Sulfuric acid=1:1.4 ratio (molar ratio) is slowly added dropwise to sulfidation pan 302, then Stir and slowly heat up, 302 temperature of sulfidation pan is maintained 160~165 DEG C, naphthalene and sulfuric acid occur sulfonating reaction generate β- Naphthalene sulfonic acids, separately there is the side reaction of part generation α-naphthalenesulfonicacid, while also has time side reaction β-dinaphthyl sulfone, naphthalenedisulfonic acid and its indexing The generation of body, it is mainly exhaust gas containing naphthalene, the sulfuric acid mist escaped in refined naphthalene melting channel 301, sulfidation pan 302 which, which produces pollutant, Exhaust gas, molten naphthalene exhaust gas is subjected to purified treatment using bag filter, sulphonation waste gas sent to scrubbing tower water by closed conduit Good clear production can be reached by washing purified treatment.After sulfonating reaction, by hydrolysis except the larger α of deactivation- Naphthalene sulfonic acids, has reached good production effect, eliminates influence of the production line to lower procedure well, sulfonating reaction thing is by pressing Naphthalene pot 304 is blown in the press-in hydrolysis of contracting air, is opened agitating device and is blown naphthalene pot 304 to hydrolysis and adds water 306 by the first water measuring tank Water is added, and appropriate steam direct heating is passed through by steam pipework 308,160 DEG C is maintained, α-naphthalenesulfonicacid is hydrolyzed to naphthalene, By the improvement of hydrolysis, beta-naphthalenesulfonic-acid overall reaction yield can be improved to 90%, be restarted after hydrolysis Agitating device, and a small amount of liquid caustic soda is added by the second liquid caustic soda measuring tank 307, liquid caustic soda and part beta-naphthalenesulfonic-acid generation β-naphthalene sulphur can be made Acid sodium-salt crystallizing seeds, while the sulfuric acid generation that liquid caustic soda can not also complete the sulfuric acid of reaction with sulfonating reaction and hydrolysis produces Neutralize, steam is then passed through by steam pipework 308 in material is hydrolyzed and carries out blowing naphthalene, that is, being passed through high-temperature steam produces hydrolysis The distillation of free state naphthalene, and naphthalene steam is sent to the first naphthalene steam condenser 309 by closed conduit, then to the first naphthalene recovery tower 311, blow naphthalene exhaust gas and enter the first naphthalene recovery tower 311 after the secondary coil condensation of the first naphthalene steam condenser 309 first, with β Spray liquid of the salt mother liquor as the first naphthalene of fountain recovery tower 311, while the naphthalene in tail gas is recycled, after blowing naphthalene, stop successively Only steam supply, stirring and spray, when in hydrolyzer without overbottom pressure, 100 are warming up to 311 indirectly heat of the first naphthalene recovery tower DEG C, the solid naphthalene of recycling is all melted, be then turned on tower top and put naphthalene valve and bottom of towe into mother liquor valve, when 311 tower of the first naphthalene recovery tower Interior liquid level rises to liquid naphthalene when putting naphthalene pipe height and all flow in the first drier 312, is closed after putting naphthalene into mother liquor valve, due to Naphthalene is immiscible from β salt mother liquors and density is different, into the first drier 312 liquid naphthalene it is warm it is static after be layered, open Bottom water valve releases β salt mother liquor, so that the simple separation for efficiently realizing naphthalene and β salt mother liquors, naphthalene are back to as raw material 302 process of sulfidation pan utilizes, therefore improves the rate of recovery of naphthalene well, its rate of recovery has been reached 98%, naphthalene is blown in generation Exhaust gas can realize good CR production using two-stage coil condensation combination naphthalene water trap spray cleaning, improve production Cleanliness.Neutralization step is carried out afterwards, and naphthalene sulfonic acids is changed into sodium naphthalene sulfonate by main purpose, and unnecessary sulfuric acid is neutralized, blowout The hydrolysis material of free naphthalene blows naphthalene pot 304 from hydrolysis and is gone to through air compressor in neutralization pot 310, is passed through steam by mixed material Directly heat to boiling, to neutralize added in pot 310 18% preheated sodium sulfite solution (come whisper it is follow-up boil work Sequence), and it be in micro-vacuum state to keep in pot, and starting stirring makes material fully react, and is passed through steam and will neutralize the two of generation Sulfur oxide is taken out of, and sulfur dioxide is all sent after pipeline is collected to 317 and second acid of the first acidifying pot in follow-up acidizing process Change pot 318 as acidulant and uses (neutralization reaction and acidification reaction be with open with stopping), when no longer producing foam in neutralization pot 310 When, that is, stop adding sub- sodium, but still blast steam and all drive sulfur dioxide out of, neutralize material and go to first through air compressor Crystallisation by cooling is carried out in cooling tank 313, and opens stirring, is cooled to 35 DEG C indirectly by recirculated cooling water, sodiumβ-naphthalenesulfonate is opened Begin to produce crystallization precipitation, then crystallized stock is gradually put into the first suction filtration tank 314 and is filtered with reciprocating pump, obtained Wet beta-naphthalenesulfonic-acid sodium salt, then material is hung to alkal melting pan 315 with electric block, due to neutralization reaction in a heated condition into OK, reaction solution is in alkalescence, and still blasts steam after reacting, so that the sulfur dioxide of reaction generation all escapes, therefore, is taken out Filter process is arranged in vitro without sulfur dioxide gas, realizes harmless production well, sodiumβ-naphthalenesulfonate can be realized by this process Reaction yield be 90%, and the major pollutants of the process are also handled well, are filtered mother liquor, are neutralized exhaust gas, take out The exhaust gas to volatilize during filter is rationally handled, and suction filtration mother liquor is sent to naphthalene water trap 324 and is used as shower water, is jacked up more After changing first through lye in the 3rd neutralization reaction kettles of 325- in and naphthalene sulfonic acids therein, be then sent to the second triple effect evaporator 326 Desalination is carried out, exhaust gas sulfur dioxide is neutralized and is all sent after pipeline to the first acidifying acidifying pot 318 of pot 317 and second as acidifying Agent efficiently utilizes, and filters exhaust gas and blows naphthalene exhaust gas in the lump through naphthalene water trap naphthalene water trap with condensed after gas gathering mask is collected 324 carry out spray cleaning processing, it is achieved that non-pollutant discharge production well, and realize efficiently production well. Alkali fusion procedure afterwards is mainly to be reacted by the alkali of molten state with sodium naphthalene sulfonate, generates naphthalene powder sodium, solid caustic soda is added choline pot It is sent into by metering after stove heat melts Huawei's liquid can be heated in alkal melting pan 315, alkal melting pan 315 is also risen using heating furnace Temperature, then according to molar ratio 1:2 ratio slowly adds sodiumβ-naphthalenesulfonate filter cake to alkal melting pan 315, and warming while stirring, reaches Stop heating to imposing a condition, sodiumβ-naphthalenesulfonate has reached 95% with sodium hydroxide reaction generation β-naphthalene powder sodium, reaction yield, alkali The molten outlet valve for opening alkal melting pan 315 after completion of the reaction, material is sent into dilution pot 316, and dilution pot 316 first adds before feeding Alkali fusion material, is then slowly added to by the secondary boiled water of subsequent handling, and material closes inlet valve after shifting, and continuously adds Secondary boiled water adjusts diluted material volume, and the pollutant of generation is choline exhaust gas and alkali fusion exhaust gas through cyclone dust removal and two level water Outer row after spray-absorption purification, so as to fulfill good purification production.It is acidified afterwards, material is pressed into the after alkali fusion dilution One acidifying pot 317, when keeping temperature in the kettle to be 260~270 DEG C, into kettle, negative pressure introduces sulfur dioxide gas (neutralization step production Raw sulfur dioxide), wherein material guiding tube insertion feed liquid bottom, gas fairlead are located at kettle top, open stirring, steam bubble dress Put, carry out material acidifying, the two-stage that pot 332 is acidified by the first acidifying pot 317, second is acidified, and neutralizes the sulfur dioxide of generation After appendix all send and it is fully acidified to the second acidifying pot 332, through pipe after unabsorbed sulfur dioxide effusion liquid level Road all send to the next first acidifying pot 317 and participates in acidification reaction, and the design of two-stage acidifying has obtained efficiency is acidified greatly Improve, while reduce sulfur dioxide well and lose outer discharge capacity, the thick finished product of 2- naphthalene powder can be obtained after the completion of acidifying, generation A small amount of sulfur dioxide that pollutant vacuumizes generation for acidification reaction can reach non-pollution discharge production after alkali cleaning absorbs.Acid Contain thick naphthalene powder and sodium sulfite in compound material, using the difference of its solubility, by washing repeatedly, isolated purer crude phenols Naphthalene, after acidifying material enters the first boiling pot 318, clear water is added by new water inlet 340, and is passed through steam indirectly heat to boiling Rise, be then shut off steam and stood, thick naphthalene powder and sodium sulfite solution open bottom valve by Asia after there is good layering Metabisulfite solution makes a small amount of naphthols in solution by further cooling by being sent after plate-type condenser to sub- sodium cooling groove 333 334 press filtration of the first filter press is sent in crystallization after separating out, crystallisation by cooling uses obturator, and it is temporary that sub- sodium filtrate is sent into sub- sodium geosyncline Deposit, press filtration filter cake is a small amount of crude phenols naphthalene, is sent to utilization in dilution pot 316, the compressed sky of upper strata crude phenols naphthalene of the first boiling pot 318 Air pressure enters to the second boiling pot 329, before the product crude phenols naphthalene of the first boiling pot 318 is received, first by the 3rd boiling pot 320 The ejected wash water that the second boiling pot 329 is depressed into by washing water outlet thereon is heated to seething with excitement, then a crude phenols naphthalene boiled is injected, And stood after stirring, after mixed material is fully layered, crude phenols naphthalene is pressed into by the 3rd boiling pot 320, wash water by compressed air As dilution kettle moisturizing, quantitative clear water is filled into it by the new water inlet 340 on the 3rd boiling pot 320 and is heated to boiling Rise, add the crude phenols naphthalene boiled through the second boiling pot 329, stood again after opening stirring, after material layering, by crude phenols naphthalene press-in the One dry pot 321, the second boiling pot 329 is pressed into by washing water outlet 341 thereon, therefore realizes production well Water resource utilizes, and has reached good balance, and the exhaust gas that the volatilization of pressure-filtering process naphthalene powder produces is sent into spray cleaning after collection, is pressed Filter produce sub- sodium filtrate send to sub- sodium head tank as neutralization step raw material utilization, partly send to the 3rd triple effect evaporator 336, Second equipment of crystallisation by cooling 337, the 3rd whizzer 338 are utilized, and integrally realize good material balance.3rd boils Moisture content, 1- naphthols, beta naphthal etc. in the thick naphthalene powder of 320 product of pot are boiled, the beta naphthal for not obtaining degree of purity is dehydrated and is separated 1- naphthols, will boil product three times and be sent by the 3rd boiling pot 320 to the first dry pot 321, be heated up and be dehydrated as heat source using steam, Vacuum pump is opened to being vacuumized in the first dry pot 321 at the same time, and the vapor that drying process produces enters in vacuum Dry trap 342, is gathered in condensation liquid storage tank 343 after condensation, is recycled sending to the 3rd boiling pot 320, first is dry Temperature rises to 110 DEG C or so in dry pot 321, and stopping is vacuumized and dried, and dried material is sent to first by compressed air and is steamed Kettle 322 is evaporated, the first distillation still 322 is vacuumized using vacuum pump while thick naphthols is pressed into distillation still, charging finishes The first distillation still 322 is heated afterwards, heating stove heat initial stage, the heating draining of distilling material normal pressure, discharge moisture is through distillation Trap 344 send to the 3rd boiling pot 320 through subcooling condensate basin 343 utilize again, when the jacket temperature of the first distillation still 322 reaches To 220~250 DEG C, liquidus temperature at 185~205 DEG C, a cut (predominantly moisture and a small amount of 1- naphthols, beta naphthal are steamed Deng), into the 3rd cut groove 345, continue to heat up, when jacket temperature reach 250~275 DEG C, liquid temperature reach 195~220 DEG C, gas Temperature reach 190~220 DEG C, vacuum >=0.09MPa when, steam all two cuts (i.e. refined beta naphthal), be sent into the second finished product Groove 346 is temporary, when in pot temperature of charge be raised to 330~360 DEG C, vapor phase temperature 300~330 DEG C, jacket temperature 380~ 420 DEG C, steam three cuts (predominantly salinity, byproduct of reaction and a small amount of beta naphthal etc.) and send out three cuts to the 4th cut groove 347, finally distillation slag (predominantly resin, carbonizing matter etc.) discharge, distillation are terminated with steam, a cut and three cuts are sent to the Three boiling pots 320 produce beta naphthal, impurity etc. and enter dilution pot 316 with wash water again after boiling, eventually enter into sub- sodium salt mother liquor, The naphthols distillation vacuum system exhaust gas of generation, which is sent after secondary coil condenses to water spray system, to be purified, and plant area is sent in vacuum pump drainage Waste water processing station processing, so as to fulfill hamlessizing technology.Finally, the beta naphthal for being temporarily stored into the second pan tank 346 is pumped through feed To section head tank 348, section head tank 348 is kept the temperature by heat source of steam, and liquid beta naphthal is by blowing in head tank To the second slicer 349, by adjusting rotary drum cooling water, control chip rate, cut into slices to beta naphthal, obtained sheet production Product are packed through second package machine 350, finally realize efficient and rational production, have good actual production value.Slightly Naphthalene powder boiling washing water contains about 18% sodium sulfite, and boil water set in part is used for neutralization step, remaining boiling washing water Handled using evaporating and concentrating process, realize good material balance and water resource and utilize.

As further technical solution, K acid production system 4 includes the sulfonation twice being connected with beta naphthal production system 3 Reaction kettle 401, twice sulfonating reaction kettle 401 be connected with kettle 402 of saltouing, kettle 402 of saltouing also connects with potassium sulfate solution measuring tank 403 Connecing, kettle 402 of saltouing is connected with the second filter press 404,

The mother liquor outlet of second filter press 404 is connected with the 4th neutralization reaction kettle 405, the 4th neutralization reaction kettle 405 and Four triple effect evaporators 406 connect, and the condensate outlet of the 4th triple effect evaporator 406 is connected with waste water processing station 407, the 4th triple effect The concentrated solution outlet of evaporator 406 is connected by the 3rd equipment of crystallisation by cooling 408 with the 4th centrifugal device 409, the 4th centrifugation dress Put 409 centrifugate outlet be connected with the 4th triple effect evaporator 406,

The filtered solid outlet of second filter press 404 is connected with aminating reaction kettle 410, and sulfurous is provided with aminating reaction kettle 410 Sour hydrogen ammonium entrance 411 and ammonia inlet 412, aminating reaction kettle 410 are acidified kettle 413 with deamination kettle the 421, the 3rd successively and are connected, the Three acidifying kettles 413 are sequentially connected with cooling precipitation kettle 414, the 3rd filter press 415, the filtered solid outlet of the 3rd filter press 415 and the Five triple effect evaporators 416 connect, filtrate (liquid is connected with the 4th sulphonation kettle 417, the concentrate of the 5th triple effect evaporator 416 connection The kettle 402 that exports and saltout connects,

4th sulphonation kettle 417 is connected by dilution trap 418 with the 4th filter press 419, the K acid outlet of the 4th filter press 419 It is connected with the 4th packing machine 420.

In the utility model, by K acid production system 4 produce K it is sour when first by sour measuring tank by 98% concentrated sulfuric acid It is fed through sulfonating reaction kettle 401 twice, and using steam as heat source indirectly heat sulfonating reaction kettle 401 twice, when temperature reaches 40 DEG C when, beta naphthal that beta naphthal production system 3 is produced is sent to G salt sulfidation pans after metering, is completed a sulfonating reaction, is controlled Acidity and temperature just can realize good sulfonation, and 20% oleum is slowly added dropwise into sulphur twice after acid measures again afterwards Change reaction kettle 401, so as to realize the process of secondary sulfonation well.Then a certain amount of potassium sulfate is added to configuration pot again, And Amino-G Acid, K acid mother liquors after being concentrated by evaporation are added thereto, it is configured to the potassium sulfate solution that concentration is about 30%, so After be passed to kettle 402 of saltouing, heated up and stirred with steam, then cooling and standings, thus realize well G salt crystallization analysis Go out, the crystal salt and mother liquor in kettle 402 of saltouing are put into the second filter press 404 and carry out good press filtration, and press filtration filtrate is taken out Handled to the 4th neutralization reaction kettle 405 and carry out certain recycling, so as to fulfill the good utilization of resources, obtained filter cake is G Salt, and the reaction yield of G salt can be brought up to 76%, at the same sulfonation, saltout, escaped in press filtration containing beta naphthal, sulfuric acid mist Gas sampling after by closed conduit send to secondary condenser condense, be then sent to spray column spray cleaning processing so that very The good discharge for reducing pollution.Afterwards, G salt, ammonium bisulfite and the concentration the second filter press 404 isolated are 20% Ammonium hydroxide is pressed into aminating reaction kettle 410 by being passed through compressed air by ammonium bisulfite entrance 411, ammonia inlet 412 after metering, close The aminating reaction kettle 410 closed can be very good temperature being promoted to 140 DEG C, and keep certain pressure, be opened after the completion of reaction Feed liquid and the ammonia of releasing are pressed into deamination kettle 421 and carry out deamination by the valve of aminating reaction kettle 410 well, until pressure is put down Weigh, the agitating device in deamination kettle 421 can be very good to ensure the efficient progress of reaction, while the ammonia that will escape out is recycled Utilize, be passed through spray equipment it is achieved thereby that ammonium hydroxide it is spare, the reasonable utilization of resource is realized well, so that will production effect Rate and product yield further improve, and the feed liquid in deamination kettle 421 is subsequently re-fed into the 3rd acidifying kettle 413 plus the 4th filter press The K acid mother liquors and 100% sulfuric acid that 419 K acid outlet is produced are acidified, and Amino-G Acid, the dioxy of generation are obtained after reaction Ammonium hydroxide made from changing the ammonia that sulphur is generated using the pressure of its own by pipeline with deamination kettle 421 is reacted, and is generated Bisulfite ammonia can also continue on for 410 aminating reaction of aminating reaction kettle, so as to realize the efficient profit of resource well With, therefore whole system design is very scientific and reasonable.After acidification reaction in 3rd acidifying kettle 413, by reaction mass Send to cooling precipitation kettle 414 and carry out crystallization precipitation, it is closed structure that cooling, which separates out kettle 414, so as to improve precipitation effect, Zhi Houjie Brilliant thing send to the 3rd filter press 415 and carries out press filtration separation, and obtained filter cake is amino G crystal, and filtrate, which is sent to the 5th triple effect, steams Hair device 416 is concentrated, and concentrate send to kettle 402 of saltouing and recycled, and condensed water is handled, therefore is improved well Product yield and process rationality, improve production efficiency, and reduce the pollution that production is brought.Afterwards by 65% smoke Sulfuric acid is pumped into sour measuring tank by acid, and the 4th sulphonation kettle 417 is added after metering, agitating device stirring cooling is opened, when temperature reaches During to 60 DEG C, G acid crystals are sent to the 4th sulphonation kettle 417, with steam indirectly heat, temperature is risen to 140 DEG C, keep certain Duration, after completion of the reaction, is diluted with water adjustment acidity by reaction mass addition dilution trap 418 and is separated out so as to improve crystal well Effect, is then pumped into the 4th filter press 419 by reaction product and carries out press filtration, obtains K acid crystals, carry out after pulverizer crushing by It is finished product after 4th packing machine packaging, mother liquor, which is equally sent, to carry out concentration concentrate to the 5th triple effect evaporator 416 and send to saltouing Kettle 402 is recycled, so as to improve production efficiency and resource utilization well.It is female that K acid production mother liquors include G salt Liquid, Amino-G Acid mother liquor and K acid mother liquors have obtained good utilization, therefore global design is practical rationally, have actual production effect The extraordinary advantage of fruit.

The above is only the preferred embodiment of the utility model only, is not intended to limit the utility model, all at this Within the spirit and principle of utility model, any modification, equivalent replacement, improvement and so on, should be included in the utility model Protection domain within.

Claims (9)

1. a kind of crude naphthalene fine-processing production line, it is characterised in that including crude naphthalene groove (1), set on the crude naphthalene groove (1) There are the lasting feed inlet (13) being connected with pipeline and the steam inlet (14) for keeping internal temperature to stablize for being passed through steam, it is described Be provided with waste gas spreading mouth (15) on crude naphthalene groove (1), the waste gas spreading mouth (15) successively with thin-walled condenser (5), pocket type Deduster (6) connects, and the dust collection mouth of the sack cleaner (6) is connected with the feed inlet (13) that continues,

The crude naphthalene groove (1) with first crystallization case (7) be connected, it is described first crystallize case (7) be connected with the first cut groove (8), Second cut groove (9), the first semi-finished product tank (10), the first cut groove (8) is connected with building materials naphthalene transfer pipeline (11), described Second cut groove (9) is connected with the described first crystallization case (7), and first semi-finished product tank (10) connects with semi-finished product crystallization case (18) Connect, the semi-finished product crystallization case (18) and the second cut groove (9), first semi-finished product tank (10), the first pan tank (12) connect, first pan tank (12) is connected with beta naphthal production system (3) and the first slicer (16), and described first cuts Piece machine (16) is connected with the first packing machine (17) connection, and the beta naphthal production system (3) is connected with K acid production system (4), institute State building materials naphthalene transfer pipeline (11) and be connected with water-reducing agent production system (2).

A kind of 2. crude naphthalene fine-processing production line according to claim 1, it is characterised in that the water-reducing agent production system (2) the liquid naphthalene measuring tank (201) that be connected with the building materials naphthalene transfer pipeline (11) is included, the liquid naphthalene measuring tank (201) and the One sulfonating reaction kettle (202) connects, and the first sulfonating reaction kettle (202) is connected with the first sulfuric acid gauge tank (203), the first water Solution reaction kettle (204), first hydrolytic reaction pot (204) are connected with the first condensation reaction kettle (205), and first condensation is anti- Kettle (205) is answered to be connected with the second sulfuric acid gauge tank (206), the first formaldehyde measuring tank (207), the first neutralization reaction kettle (208), institute State the first neutralization reaction kettle (208) and be connected with the first liquid caustic soda measuring tank (209), liquid water-reducing agent transfer pipeline (210), the first mist Change device (211), the liquid water-reducing agent transfer pipeline (210) is connected with the first compounding kettle (212), first atomizer (211) it is connected with the first drying tower (213), first drying tower (213) and the first hot-blast stove (214), the first cyclonic separation Device (215), the first spiral discharging device (216) connection, first cyclone separator (215) and the first water dust scrubber (217), First spiral discharging device (216) connection, first spiral discharging device (216) are connected with the first packing machine (218).

A kind of 3. crude naphthalene fine-processing production line according to claim 2, it is characterised in that first hydrolytic reaction pot (204) the first metering sink (219), the condensation of the first metering sink (219) and the first triple effect evaporator (220) are connected with The mouth of a river connects, and first triple effect evaporator (220) is connected with beta naphthal mother liquor conveying water lines (221).

A kind of 4. crude naphthalene fine-processing production line according to claim 1, it is characterised in that the beta naphthal production system (3) the refined naphthalene melting channel (301) being connected with first pan tank (12), the refined naphthalene melting channel (301) and sulfidation pan are included (302) connecting, the sulfidation pan (302) is blown naphthalene pot (304) and is all connected with the first sulfuric acid high position tank (303), hydrolysis, and described first Sulfuric acid high position tank (303) is connected with the first sulfuric acid storage tank (305), and naphthalene pot (304) and the first water measuring tank are blown in the hydrolysis (306), the second liquid caustic soda measuring tank (307), steam pipework (308), the first naphthalene steam condenser (309), neutralization pot (310) connect Connect, the first naphthalene steam condenser (309) is sequentially connected with the first naphthalene recovery tower (311), the first drier (312), described The recycling naphthalene mouth of first drier (312) is connected with the sulfidation pan (302), the separation water of the first naphthalene recovery tower (311) Mouth blows naphthalene pot (304) with the hydrolysis and is connected,

It is described neutralization pot (310) with the first cooling tank (313), the first suction filtration tank (314), alkal melting pan (315), dilution pot (316), First acidifying pot (317), the first boiling pot (318), the second boiling pot (319), the 3rd boiling pot (320), the first dry pot (321), the first distillation still (322) is sequentially connected,

First suction filtration tank (314) is connected with the first whizzer (323), first suction filtration tank (314) also with naphthalene water Trap (324), the 3rd neutralization reaction kettle (325), the second triple effect evaporator (326) are sequentially connected, second triple effect evaporation The concentrated solution outlet of device (326) is connected with cooling nutsch filter (327), the mother liquor outlet and first of the cooling nutsch filter (327) Equipment of crystallisation by cooling (328) connection, precipitate outlet are connected with the first centrifugal device (329), first centrifugal device (329) Sodium naphthalene sulfonate outlet be connected with alkali fusion device (330), the condensate outlet of second triple effect evaporator (326) and the alkali Fusing device (330) connects, and the alkali fusion device (330) is connected with the dilution pot (316), first equipment of crystallisation by cooling (328) supernatant outlet is connected with second triple effect evaporator (326), crystallizes outlet and the second centrifugal device (331) even Connecing, the centrifugate outlet of second centrifugal device (331) is connected with second triple effect evaporator (326),

The dilution pot (316) is also connected by the second acidifying pot (332) with first boiling pot (318), the neutralization pot (310) sulfur dioxide outlet is connected with the described second acidifying pot (332), the first acidifying pot (317) successively.

A kind of 5. crude naphthalene fine-processing production line according to claim 4, it is characterised in that first boiling pot (318) sodium sulfite solution outlet is connected with sub- sodium cooling groove (333), the first filter press (334) successively, first press filtration The filtered solid outlet of machine (334) is connected with the dilution pot (316), the filtrate (liquid and dnockout pumps of first filter press (334) (335), the 3rd triple effect evaporator (336), the second equipment of crystallisation by cooling (337), the 3rd whizzer (338) are sequentially connected, 3rd whizzer (338) and the 3rd triple effect evaporator (336), second equipment of crystallisation by cooling (337) are equal Connection, the dnockout pumps (335) are also connected with sub- sodium head tank (339).

A kind of 6. crude naphthalene fine-processing production line according to claim 4, it is characterised in that first boiling pot (318) and on the 3rd boiling pot (320) new water inlet (340), second boiling pot (319) and described are both provided with Be both provided with washing water outlet (341) on three boiling pots (320), the washing water outlet (341) of second boiling pot (319) with it is described Pot (316) connection is diluted, the washing water outlet (341) of the 3rd boiling pot (320) is connected with second boiling pot (319).

A kind of 7. crude naphthalene fine-processing production line according to claim 4, it is characterised in that first dry pot (321) steam outlet is connected with dry trap (342), the condensation-water drain of the dry trap (342) and condensation Liquid storage tank (343) connects, and first distillation still (322) is connected with distillation trap (344), the distillation trap (344) Condensation-water drain with it is described condensation liquid storage tank (343) be connected, it is described condensation liquid storage tank (343) with it is described dilution pot (316) connect Connect.

A kind of 8. crude naphthalene fine-processing production line according to claim 4, it is characterised in that first distillation still (322) the first fraction outlets, the second fraction outlets, the 3rd fraction outlets respectively with the 3rd cut groove (345), the second pan tank (346), the 4th cut groove (347) connects, and the 3rd cut groove (345), the 4th cut groove (347) are with the described 3rd Boiling pot (320) connects, and second pan tank (346) is connected with section head tank (348), the section head tank (348) It is sequentially connected with the second slicer (349), second package machine (350).

A kind of 9. crude naphthalene fine-processing production line according to claim 4, it is characterised in that the K acid production system (4) Including the kettle of sulfonating reaction twice (401) being connected with the beta naphthal production system (3), the kettle of sulfonating reaction twice (401) It is connected with kettle of saltouing (402), the kettle of saltouing (402) is also connected with potassium sulfate solution measuring tank (403), the kettle of saltouing (402) it is connected with the second filter press (404), the mother liquor outlet and the 4th neutralization reaction kettle (405) of second filter press (404) Connection, the 4th neutralization reaction kettle (405) are connected with the 4th triple effect evaporator (406), the 4th triple effect evaporator (406) Condensate outlet be connected with waste water processing station (407), the concentrated solution outlet of the 4th triple effect evaporator (406) passes through the 3rd Equipment of crystallisation by cooling (408) is connected with the 4th centrifugal device (409), the outlet of the centrifugate of the 4th centrifugal device (409) with 4th triple effect evaporator (406) connection,

The filtered solid outlet of second filter press (404) is connected with aminating reaction kettle (410), on the aminating reaction kettle (410) Be provided with ammonium bisulfite entrance (411) and ammonia inlet (412), the aminating reaction kettle (410) successively with deamination kettle (421), the 3rd acidifying kettle (413) connection, the 3rd acidifying kettle (413) separate out kettle (414), the 3rd filter press with cooling (415) it is sequentially connected, the filtered solid outlet of the 3rd filter press (415) is connected with the 5th triple effect evaporator (416), filtrate (liquid It is connected with the 4th sulphonation kettle (417), the concentrated solution outlet and the kettle of saltouing of the 5th triple effect evaporator (416) connection (402) connect,

4th sulphonation kettle (417) is connected by dilution trap (418) with the 4th filter press (419), the 4th filter press (419) K acid outlet is connected with the 4th packing machine (420).