CN103242902A

CN103242902A - Processing method of coal tar

Info

Publication number: CN103242902A
Application number: CN2013101644035A
Authority: CN
Inventors: 陈义涛
Original assignee: XINJIANG XINLIAN COAL CHEMICAL INDUSTRY Co Ltd
Current assignee: XINJIANG XINLIAN COAL CHEMICAL INDUSTRY Co Ltd
Priority date: 2013-04-25
Filing date: 2013-04-25
Publication date: 2013-08-14

Abstract

The invention relates to a processing method of coal tar. The processing method is characterized by comprising the following steps of: dewatering tar; distilling the tar; sequentially distilling the dewatered tar by adopting continuous type distillation devices, namely a first-stage evaporator and a second-stage evaporator, to respectively obtain light oil, asphalt, anthracene oil II, anthracene oil I, mixed oil III; washing and decomposing: alkalizing the mixed oil III to generate water-soluble phenoxide which can be separated from water-insoluble naphthalene washing distillates so as to provide a raw material for industrial naphthalene; evaporating the separated neutral phenoxide to obtain pure sodium phenolate; decomposing by using sulphuric acid to finally obtain crude phenol of which phenol content is more than or equal to 83%; and distilling industrial naphthalene: dewatering washed mixed distillates, carrying out heat exchange with industrial naphthalene steam to 190-210 DEG C, cutting phenol oil distillates in a primary distillation tower, and cutting the industrial naphthalene and wash oil distillates in a rectifying tower. The process method disclosed by the invention is simple and reasonable in process, reduces the energy consumption and plays an energy conservation role by sufficiently utilizing the afterheat of products in the distillation process of the tar and prevents the flue gas from polluting the environment by arrangement of an exhaust cleaning tower in a washing and decomposing procedure.

Description

A kind of working method of coal tar

Technical field

The invention belongs to technical field of coal chemical industry, be specifically related to a kind of working method of coal tar.

Background technology

Tar claims coal tar or coal cream again, is the liquid product that obtains in the dry distillation of coal process, according to the difference of pyrolysis temperature, coal tar can be divided into semi coking tar, middle temperature tar and high temperature tar three classes.Coal-tar heavy oil is one of product in the raw gas that generates of process of coking pyrolysis of coal, the 3%-4% that its output accounts for the shove charge coal its product at normal temperatures and pressures is black viscous fluid shape, composition mainly is made up of polycyclc aromatic compound, alkylaromatic hydrocarbon content is less, high boiling component is more, Heat stability is good.Its component naphthalene, main component has: 1-methylnaphthalene, 2-methylnaphthalene, acenaphthene, fluorenes, dibenzofuran, anthracene, phenanthrene, carbazole, fluoranthene, quinoline, pyrene etc.

Coal tar is one of staple product of coking industry, it forms very complicated, in most cases be to be used after separating specially, purify by coal-tar industry, generally be by distillation it to be divided into several narrow fractions and tar-bitumens such as light oil, carbolic oil, naphtalene oil, carbolineum, from different cuts, isolate thick chemicals or smart chemicals then.

The purposes of the chemicals that coal tar processing obtains is very extensive, much be the important source material of plastics, synthon, dyestuff, synthetic rubber, agricultural chemicals, material of construction, high temperature material and national defense industry, can be used for producing industrial chemicals, pharmacy, dyestuff oil such as coumarone, phenylformic acid as light oil, naphthols oil; Crude phenols are mainly for the production of synthon, agricultural chemicals, engineering plastics, dyestuff intermediate; NAPTHALENE FLAKES. (INDUSTRIAL GRADE, naphthalene and naphthalene are that product is widely used in industries such as synthetic resins, coating, medicine, agricultural chemicals, light industry, plastics, auxiliary agent, can be used for producing products such as phthalic anhydride, 2-Naphthol, methyl naphthylamine, H acid, paracril, softening agent, diffusant, antithrombotics, also should be utilized fully, be made the bigger economic benefit of its performance; Washing oil is a kind of mixture of complexity, is rich in valuable Organic Chemicals such as quinoline, isoquinoline 99.9, indoles, alpha-methyl-naphthalene, the Beta-methyl bitter edible plant, biphenyl, the dimethyl bitter edible plant, acenaphthene, dibenzofuran and fluorenes, is mainly used in pharmacy, dyestuff; Carbolineum is mainly used in disposing carbon black raw material oil, road asphalt or fuel wet goods, also can be used for wood preservation and produces anthraquinone etc.; Mid-temperature pitch is used for malthoid processed, building waterproof layer, senior bituminous varnish etc., also is the raw material of producing pitch coke or delay coke and modified pitch; Modified pitch is then stuck with paste the superpower electrode bar for the manufacture of pre-training carbon anode.

The development coal tar deep processing can improve resource utilization and economic benefit greatly, and existing coal tar processing means is more single, and has problems such as energy consumption height, quality are stablized inadequately, the Working environment pollution is big.

Summary of the invention

It is simple, easy to operate that technical problem to be solved by this invention provides a kind of technology, and the working method of the coal tar of less energy consumption, has constant product quality, advantage such as low in the pollution of the environment simultaneously.

The present invention solves the problems of the technologies described above the technical scheme that adopts: a kind of working method of coal tar is characterized in that may further comprise the steps:

1) dehydration of tar;

2) tar distillation: adopt the continous way water distilling apparatus, the tar after the dehydration is handled through one section vaporizer, flash evaporator distillation successively, distill out light oil, pitch, anthracene oil, a carbolineum, mixed triolein respectively;

3) washing is decomposed: the phenol in the mixed triolein is generated water-soluble phenates by adding alkali, thereby washing fraction with water-fast naphthalene separates, for NAPTHALENE FLAKES. (INDUSTRIAL GRADE is supplied raw materials, isolated neutral phenates, remove wherein to mix oil through steaming to blow down, obtain clean sodium phenolate, decomposing by sulfuric acid, finally obtain containing the crude phenols of phenol 〉=83%;

4) NAPTHALENE FLAKES. (INDUSTRIAL GRADE distillation: will wash and mix part through dehydration, and with 190～210 ℃ of NAPTHALENE FLAKES. (INDUSTRIAL GRADE steam heat-exchangings, enter primary tower, and in primary tower, cut the carbolic oil fraction, and in rectifying tower, cut NAPTHALENE FLAKES. (INDUSTRIAL GRADE and washing oil fraction.

As improvement, described tar is coal-tar heavy oil, and dehydration of tar is to adopt to leave standstill dehydration, tar is delivered in the dehydration of tar groove left standstill 22～26h, makes water content be not more than 4%.

As improvement, the concrete steps of described tar distillation are: the tar after will dewatering is after one section pump pressurization, through the tar steam preheater, after tar and a carbolineum interchanger are heated to 125-135 ℃, go into one section vaporizer, the light oil that distillation obtains steams from the cat head of one section vaporizer, and the anhydrous tar that comes out at the bottom of the tower is forced into the tube furnace radiation section through two sections pumps, after being heated to 380-400 ℃, go into flash evaporator; Anhydrous tar distills in flash evaporator, and flash evaporator cuts and obtains anthracene oil, and the mixing oil vapour that obtains of distillation steams from the cat head of flash evaporator and enters the fraction tower, and the remaining pitch in distillation back goes out to enter follow-up workshop section from the tower bottom flow of flash evaporator; Mixing oil vapour distills in the fraction tower, the mixed triolein that cuts in the fraction tower is cooled to 80-90 ℃ through the mixed triolein water cooler, cooled mixed triolein is sent to washing and decomposes workshop section, the secondary light oil that obtains of distillation steams to enter from the cat head of fraction tower and mixes the light oil receiving tank, and the remaining carbolineum in distillation back is gone into a carbolineum interchanger and raw tar carries out heat exchange from the tower bottom flow of fraction tower, and the carbolineum after the heat exchange enters a carbolineum medial launder; Secondary light oil part in the described mixing light oil receiving tank is through the light oil reflux pump, be back to the fraction tower and regulate 110-130 ℃ of control tower top temperature, remainder enters the light oil groove, a part one carbolineum of a described carbolineum medial launder is back to flash evaporator through a carbolineum reflux pump and regulates 330-345 ℃ of control tower top temperature, and remainder enters a carbolineum groove.

Improve, the concrete steps that described washing is decomposed are again: washed pump and extract out by once connecting by the contaminated product of not giving a baby a bath on the third day after its birth that tar distillation comes, the alkaline phenol sodium that comes with alkaline phenol sodium header tank is mixed into once to connect washes knockout tower; By static layering, isolated neutral phenol sodium enters neutral phenol sodium groove from once connecting the bottom discharge of washing knockout tower, mixes oil content and enters the dephenolize dashpot one time from once connecting the top discharge of washing knockout tower; Above-mentioned mixing oil content connects by secondary washes the pump extraction, enter secondary after alkali fully mixes and connect and to wash knockout tower by adding, pass through static layering, alkalescence phenol sodium connects the bottom discharge of washing knockout tower from secondary and enters alkaline phenol sodium groove, send in the alkaline phenol sodium header tank by alkaline phenol sodium pump, giving a baby a bath on the third day after its birth to mix connects the top of washing knockout tower from secondary and discharges and flow into the NAPTHALENE FLAKES. (INDUSTRIAL GRADE water distilling apparatus and further process again; Carbolic oil in the carbolic oil groove is extracted out by washing pump, and wash in the device between alkaline phenol sodium is mixed into and react, isolated neutral phenol sodium is discharged from the bottom of washing device and is entered neutral phenol sodium groove, and isolated removal phenol carbolic oil is discharged from the top of washing device and entered the removal phenol carbolic oil groove; Neutral phenol sodium in the neutral phenol sodium groove removes wherein to mix oil through steaming to blow down, and obtains clean sodium phenolate, decomposes by sulfuric acid again, finally obtains crude phenols.

Improve, described mass ratio of not giving a baby a bath on the third day after its birth contaminated product and alkaline phenol sodium is 5.5～6.5: 1 again; The described alkali lye that adds alkali is that mass concentration is 13～15% sodium hydroxide, and the mass ratio of described mixing oil content and alkali lye is 6～7: 1; It is to adopt vitriol oil interval type to decompose that described sulfuric acid decomposes, detailed process is: clean sodium phenolate is put into splitter, be under 55～60Kpa condition at pressure, stir the vitriol oil of adding 90～92%, the control temperature of reaction is 80～85 ℃, till subacidity, static 5～7h, the upper strata is crude phenols, and at separator gas barrier is installed, and the flue gas of discharge enters in the clean tower of exhaust and handles.

At last, the concrete steps of the distillation of described NAPTHALENE FLAKES. (INDUSTRIAL GRADE are: washed to mix and part be heated to 85-90 ℃ in raw material tank, leave standstill dehydration after, deliver to feed preheater by feedstock pump, with NAPTHALENE FLAKES. (INDUSTRIAL GRADE steam heat-exchanging to 190～210 ℃, enter the primary tower middle part, top adopts carbolic oil through condensate cooler, enters water-and-oil separator, the carbolic oil backflash, a part is returned the primary tower top through the carbolic oil reflux pump and is used as backflow, the control tower top temperature, and remainder is then gone into pan tank as product.The washing oil of naphthalene at the bottom of the primary tower is pumped into the fore-running tube furnace with the fore-running hot oiling and is heated to 270～290 ℃, returns primary tower bottom, is the primary tower circulation heating in the mode of hot oiling;

Tell a part of naphthalene from fore-running hot oil pump outlet pipe, wash contaminated product, send into the rectifying tower middle part, cat head extraction content is gone into NAPTHALENE FLAKES. (INDUSTRIAL GRADE vaporization and condensation water cooler to 110 ± 10 ℃ of NAPTHALENE FLAKES. (INDUSTRIAL GRADE backflashes after mixing the raw material heat exchange greater than 95% NAPTHALENE FLAKES. (INDUSTRIAL GRADE steam and three, a part is delivered to the rectifying tower top through the NAPTHALENE FLAKES. (INDUSTRIAL GRADE reflux pump and is used as backflow, the control tower top temperature, overflow portion is gone into the NAPTHALENE FLAKES. (INDUSTRIAL GRADE receiver, behind rotary drum crystallizer crystallisation by cooling, the packing warehouse-in, the washing oil of rectifier bottoms is delivered to the rectifying tube furnace by the rectified heat oil pump and is heated to 295～320 ℃ and passes back into rectifier bottoms, is the rectifying tower heat supply in the mode of hot oiling.Separate a part of washing oil from the outlet of rectified heat oil pump, as low naphthalene washing oil, after the condensation cooling, go into the washing oil groove.

Compared with prior art, the invention has the advantages that: take full advantage of the waste heat of each product of tar distillation process, thereby reduce energy consumption, play the effect of save energy; Washing arranges exhaust in the decomposition process and cleans tower, stops the smoke pollution environment, complete processing advantages of simple of the present invention, easy to operate, and safe and reliable, the constant product quality of production process, environmental pollution, energy consumption are lower simultaneously.

Description of drawings

Fig. 1 is the process flow sheet of coal tar processing of the present invention;

Fig. 2 is the process flow sheet of tar distillation;

Fig. 3 is the process flow sheet that washing is decomposed;

Fig. 4 is the process flow sheet of NAPTHALENE FLAKES. (INDUSTRIAL GRADE distillation.

Embodiment

Describe in further detail below in conjunction with the present invention of accompanying drawing embodiment.

A kind of working method of coal tar is characterized in that may further comprise the steps:

1) dehydration of tar: tar must be removed moisture before distillation, and the tar of dehydration can reduce the heat exhaustion of still-process, increases the throughput of equipment, reduces the systemic resistance of continuous still battery heating.After general tar was evenly finished, a part of water was mixed in tar inside, need heat to leave standstill to make the profit layering in 24 hours, dewatered to satisfy production requirement again.

------delivering to the dehydration of tar groove---delivers to the production raw material tank to operational path: the incoming test of raw material to put into the underground recessing that unloads.

2) tar distillation: adopt the continous way water distilling apparatus, after raw tar left standstill dehydration, the water content of dehydrated raw material tar was less than or equal to 4%., through one section pump pressurization, send into the tar steam preheater, be heated to 125-135 ℃ with carbolineum exchanger heat exchange, the tar after the heating is delivered to one section vaporizer; Tar distills in one section vaporizer, the light oil that distillation obtains steams from the cat head of one section vaporizer, through a light oil condensate cooler but to 30-40 ℃, a cooled light oil through a light oil water-and-oil separator with water sepn, a light oil after the separation enters backflash, and the waste water of separating enters wastewater trough; And the remaining anhydrous tar in distillation back pressurizes through two sections tar pumps at the bottom of the tower of one section vaporizer, and the radiation section that is delivered to tube furnace after the pressurization is heated to 380-400 ℃, and the anhydrous tar after the heating is delivered to flash evaporator; Anhydrous tar distills in flash evaporator, and the mixing oil vapour that obtains of distillation steams from the cat head of flash evaporator and enters the fraction tower; The anthracene oil that cuts in the flash evaporator is cooled to 80-90 ℃ through the anthracene oil water cooler, and cooled anthracene oil enters the anthracene oil groove; And the remaining pitch in distillation back is cooled to 200-260 ℃ through pitch cooler at the bottom of tower, and cooled pitch enters follow-up workshop section; Need test earlier to pitch, the product that is up to the standards enters asphalt moulding workshop section, and substandard product switches into the tar medial launder; Mixing oil vapour distills in the fraction tower, the secondary light oil that obtains of distillation steams through secondary light oil water cooler from the cat head of fraction tower and is cooled to 50-60 ℃, cooled secondary light oil enters secondary light oil water-and-oil separator with water sepn, secondary light oil after the separation enters and mixes the light oil receiving tank, and the phenolic wastewater of separating enters the phenol tank; The mixed triolein that cuts in the fraction tower is cooled to 80-90 ℃ through the mixed triolein water cooler, and cooled mixed triolein is sent to washing and decomposes workshop section; And the remaining carbolineum in distillation back is gone into a carbolineum interchanger and raw tar carries out heat exchange from the tower bottom flow of fraction tower, carbolineum after the heat exchange is drawn to a carbolineum water cooler by carbolineum extractor pump pressurization and is cooled to 80-90 ℃, and a cooled carbolineum enters a carbolineum medial launder.Secondary light oil part in the described mixing light oil receiving tank is back to the fraction tower and regulates its tower top temperature of control through the light oil reflux pump, and top tower control is controlled at 110-130 ℃, and remainder enters the light oil groove; A part one carbolineum of a described carbolineum medial launder is back to flash evaporator through a carbolineum reflux pump and regulates its tower top temperature of control, and its top tower control control is at 330-345 ℃, and remainder enters a carbolineum groove.

Wherein the origin of heat of flash evaporator and fraction column distillation comes from steam; steam is heated to more than 360 ℃ through the tube furnace convection zone; for flash evaporator; the fraction column distillation uses; the ammonium salt corrosion that is not produced in the production process for protection equipment; be connected with the yellow soda ash groove in the equipment pipeline, remove ammonium salt, protection equipment by the neutralization reaction of sodium carbonate solution and ammonium salt.

3) washing is decomposed: comprise three shuffle wash dephenolize, phenol sodium decomposes and carbolic oil between wash-out phenol, detailed process is: wash the pump extraction by the contaminated product of not giving a baby a bath on the third day after its birth that tar distillation comes by once connecting, to wash in the pump with mass ratio be to mix at 5.5～65: 1 to the alkaline phenol sodium that comes with alkaline phenol sodium header tank once connecting, and enters once to connect and wash knockout tower; Mixed solution mixes oil content and neutral phenol sodium once connecting to wash in the knockout tower to be separated into by static layering, wherein neutral phenol sodium enters neutral phenol sodium groove from once connecting the bottom of washing knockout tower, mixes oil content and enters the dephenolize dashpot one time from once connecting the top discharge of washing knockout tower; In order further to take off the phenols that mixes oil content, carry out the secondary dephenolize, above-mentioned mixing oil content is even washed pump by secondary extracts out, be 13～15% sodium hydroxide according to mass ratio 6～7 with mass concentration: 1 enters secondary after fully mixing connects and washes knockout tower, connect to wash in the knockout tower to be separated into by static layering at secondary and wash and alkaline phenol sodium, alkalescence phenol sodium connects the bottom discharge of washing knockout tower from secondary and enters alkaline phenol sodium groove, send in the alkaline phenol sodium header tank by alkaline phenol sodium pump again, give a baby a bath on the third day after its birth and further process as the raw material of NAPTHALENE FLAKES. (INDUSTRIAL GRADE mixed the company the top discharge inflow NAPTHALENE FLAKES. (INDUSTRIAL GRADE water distilling apparatus of washing knockout tower from secondary, so just isolated residual alkaline phenol sodium, be of great importance to stablizing the NAPTHALENE FLAKES. (INDUSTRIAL GRADE water distilling apparatus; Carbolic oil in the carbolic oil groove is extracted out by washing pump, and wash in the device between alkaline phenol sodium is mixed into and react, isolate neutral phenol sodium and removal phenol carbolic oil, wherein neutral phenol sodium is discharged from the bottom of washing device and is entered neutral phenol sodium groove, and removal phenol carbolic oil is discharged from the top of washing device and entered the removal phenol carbolic oil groove; And the neutral phenol sodium in the neutral phenol sodium groove removes wherein to mix oil through steaming to blow down, and obtains clean sodium phenolate, decomposes by sulfuric acid again, finally obtains containing the crude phenols of phenol 〉=83%; Steaming is blown in the phenolate distilling still and is carried out, the phenolate distilling still adopts the steam indirect heating and blows with direct steaming of steam, isolated clean sodium phenolate enters the clean phenates groove at the bottom of still, blow out carbolic oil and phenol water enter to steam and blow in the water-and-oil separator, isolated carbolic oil carries out in the removal phenol carbolic oil groove, and isolated phenol water enters sewage disposal device; It is to adopt vitriol oil interval type to decompose that sulfuric acid decomposes, detailed process is: clean sodium phenolate is put into splitter, be under 55～60Kpa condition at pressure, stir the vitriol oil of adding 90～92%, the control temperature of reaction is 80～85 ℃, till subacidity, static 5～7h, the upper strata is crude phenols, in order to control the add-on of the vitriol oil, the adding of the vitriol oil is to control by spinner-type flowmeter, reaction times is 2～2.5h, and at separator gas barrier is installed, and the flue gas of discharge enters in the clean tower of exhaust and handles, so just guaranteed that Working environment is pollution-free, ensured operator's health.

4) NAPTHALENE FLAKES. (INDUSTRIAL GRADE distillation: washed mixing part and be heated to 85～90 ℃ in raw material tank, after leaving standstill dehydration, deliver to feed preheater by feedstock pump, with about NAPTHALENE FLAKES. (INDUSTRIAL GRADE steam heat-exchanging to 200 ℃, enter the primary tower middle part, top adopts carbolic oil through condensate cooler, enter water-and-oil separator, the carbolic oil backflash, a part is returned the primary tower top through the carbolic oil reflux pump and is used as backflow, the control tower top temperature, remainder is then gone into pan tank as product.The washing oil of naphthalene at the bottom of the primary tower is pumped into the fore-running tube furnace with the fore-running hot oiling and is heated to about 270～290 ℃, returns primary tower bottom, is the primary tower circulation heating in the mode of hot oiling;

Claims

1. the working method of a coal tar is characterized in that may further comprise the steps:

1) dehydration of tar;

4) NAPTHALENE FLAKES. (INDUSTRIAL GRADE distillation: will wash and mix part through dehydration, and with NAPTHALENE FLAKES. (INDUSTRIAL GRADE steam heat-exchanging to 190～210 ℃, enter primary tower, and in primary tower, cut the carbolic oil fraction, and in rectifying tower, cut NAPTHALENE FLAKES. (INDUSTRIAL GRADE and washing oil fraction.

2. working method according to claim 1, it is characterized in that: described tar is coal-tar heavy oil, dehydration of tar is to adopt to leave standstill dehydration, tar is delivered in the dehydration of tar groove left standstill 22～26h, makes water content be not more than 4%.

3. working method according to claim 1, it is characterized in that: the concrete steps of described tar distillation are: the tar after will dewatering is after one section pump pressurization, through the tar steam preheater, after tar and a carbolineum interchanger are heated to 125～135 ℃, go into one section vaporizer, the light oil that distillation obtains steams from the cat head of one section vaporizer, and the anhydrous tar that comes out at the bottom of the tower is forced into the tube furnace radiation section through two sections pumps, after being heated to 380～400 ℃, go into flash evaporator; Anhydrous tar distills in flash evaporator, and flash evaporator cuts and obtains anthracene oil, and the mixing oil vapour that obtains of distillation steams from the cat head of flash evaporator and enters the fraction tower, and the remaining pitch in distillation back goes out to enter follow-up workshop section from the tower bottom flow of flash evaporator; Mixing oil vapour distills in the fraction tower, the mixed triolein that cuts in the fraction tower is cooled to 80～90 ℃ through the mixed triolein water cooler, cooled mixed triolein is sent to washing and decomposes workshop section, the secondary light oil that obtains of distillation steams to enter from the cat head of fraction tower and mixes the light oil receiving tank, and the remaining carbolineum in distillation back is gone into a carbolineum interchanger and raw tar carries out heat exchange from the tower bottom flow of fraction tower, and the carbolineum after the heat exchange enters a carbolineum medial launder; Secondary light oil part in the described mixing light oil receiving tank is through the light oil reflux pump, be back to the fraction tower and regulate 110～130 ℃ of control tower top temperatures, remainder enters the light oil groove, a part one carbolineum of a described carbolineum medial launder is back to flash evaporator through a carbolineum reflux pump and regulates 330～345 ℃ of control tower top temperatures, and remainder enters a carbolineum groove.

4. working method according to claim 1, it is characterized in that: the concrete steps that described washing is decomposed are: the contaminated product of not giving a baby a bath on the third day after its birth by tar distillation is washed the pump extraction by once connecting, and the alkaline phenol sodium with alkaline phenol sodium header tank is mixed into once to connect washes knockout tower; By static layering, isolated neutral phenol sodium enters neutral phenol sodium groove from once connecting the bottom discharge of washing knockout tower, mixes oil content and enters the dephenolize dashpot one time from once connecting the top discharge of washing knockout tower; Above-mentioned mixing oil content connects by secondary washes the pump extraction, enter secondary after alkali fully mixes and connect and to wash knockout tower by adding, pass through static layering, alkalescence phenol sodium connects the bottom discharge of washing knockout tower from secondary and enters alkaline phenol sodium groove, send in the alkaline phenol sodium header tank by alkaline phenol sodium pump, giving a baby a bath on the third day after its birth to mix connects the top of washing knockout tower from secondary and discharges and flow into the NAPTHALENE FLAKES. (INDUSTRIAL GRADE water distilling apparatus and further process again; Carbolic oil in the carbolic oil groove is extracted out by washing pump, and wash in the device between alkaline phenol sodium is mixed into and react, isolated neutral phenol sodium is discharged from the bottom of washing device and is entered neutral phenol sodium groove, and isolated removal phenol carbolic oil is discharged from the top of washing device and entered the removal phenol carbolic oil groove; Neutral phenol sodium in the neutral phenol sodium groove removes wherein to mix oil through steaming to blow down, and obtains clean sodium phenolate, decomposes by sulfuric acid again, finally obtains crude phenols.

5. working method according to claim 4 is characterized in that: the give a baby a bath on the third day after its birth mass ratio of contaminated product and alkaline phenol sodium of described end is 5.5～6.5: 1; The described alkali lye that adds alkali is that mass concentration is 13～15% sodium hydroxide, and the mass ratio of described mixing oil content and alkali lye is 6～7: 1; It is to adopt vitriol oil interval type to decompose that described sulfuric acid decomposes, detailed process is: clean sodium phenolate is put into splitter, be under 55～60Kpa condition at pressure, stir the vitriol oil of adding 90～92%, the control temperature of reaction is 80～85 ℃, till subacidity, static 5～7h, the upper strata is crude phenols, and at separator gas barrier is installed, and the flue gas of discharge enters in the clean tower of exhaust and handles.

6. working method according to claim 1, it is characterized in that: the concrete steps of the distillation of described NAPTHALENE FLAKES. (INDUSTRIAL GRADE are: washed mixing part and be heated to 85-90 ℃ in raw material tank, after leaving standstill dehydration, deliver to feed preheater by feedstock pump, with NAPTHALENE FLAKES. (INDUSTRIAL GRADE steam heat-exchanging to 190～210 ℃, enter the primary tower middle part, top adopts carbolic oil through condensate cooler, enter water-and-oil separator, the carbolic oil backflash, a part is returned the primary tower top through the carbolic oil reflux pump and is used as backflow, the control tower top temperature, and remainder is then gone into pan tank as product.The washing oil of naphthalene at the bottom of the primary tower is pumped into the fore-running tube furnace with the fore-running hot oiling and is heated to 270～290 ℃, returns primary tower bottom, is the primary tower circulation heating in the mode of hot oiling;