CN1122320A - Method and apparatus for extracting alpha-methyl naphthalene and beta-methylnaphthalene - Google Patents
Method and apparatus for extracting alpha-methyl naphthalene and beta-methylnaphthalene Download PDFInfo
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- CN1122320A CN1122320A CN 94113628 CN94113628A CN1122320A CN 1122320 A CN1122320 A CN 1122320A CN 94113628 CN94113628 CN 94113628 CN 94113628 A CN94113628 A CN 94113628A CN 1122320 A CN1122320 A CN 1122320A
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Abstract
Industrial methylnaphthalene fraction is first H2SO4 pickled and KOH alkaline washed to remove impurity quinoline and indole and then rectified to produce alpha- and beta- methylnaphthalene product with a purity over 90%. The extraction equipment consists of raw material tank, back material tank for the material after removing impurity, rectifying tower, crystallizer, suction filter, filtrate tank, vacuum pump, condensator and other parts, and it features its pickling tank, static separator, alkaline washing tank and filter successively connected between the two material tanks.
Description
The present invention relates to the method and the device of a kind of extraction α-methylnaphthalene and β-methylnaphthalene, be specially adapted to from the technical methylnaphthalene fraction, extract the method and apparatus of α-methylnaphthalene, β methylnaphthalene.
Before the present invention, extracting α-methylnaphthalene and β-methylnaphthalene from the technical methylnaphthalene fraction mainly is the processing method that adopts distillation, crystallization, suction filtration, be that the technical methylnaphthalene fraction directly enters rectifying tower and carries out rectifying, for improving product purity, ctystallizing point difference according to α-methylnaphthalene and β methylnaphthalene, in crystallizer, purify, utilize the purity product of aforesaid method extraction more than 90%, the one, enough stage number be arranged, rectifying tower will increase like this, tower height all bring difficulty for manufacturing, installation etc., and to waste starting material; The 2nd, product concentration is that the product extraction yield more than 90% only accounts for about 40%, and extraction yield is very low, is unfavorable for comprehensive utilization.
Order of the present invention is that the product purity that improves α-methylnaphthalene and β-methylnaphthalene reaches 90%.β-methylnaphthalene product extraction yield height, processing method is simple, and production cost is lower.
In order to reach goal of the invention, existing details are as follows with technology contents:
A kind of method of from the technical methylnaphthalene fraction, extracting α-methylnaphthalene and β-methylnaphthalene, its extraction process is as follows:
(1) with technical methylnaphthalene fraction concentration is H2SO4 solution pickling in pickling tank of 15～25%, the per kilogram quinoline adds 3.5～4.0 liters of H2SO4 solution, this groove is heated, and be controlled at 60～65 ℃, constantly stir in the groove, then, enter in the standing separation device and separate, the moisture content that contains the impurity quinoline in the standing separation device is extracted out;
(2) the technical methylnaphthalene fraction of removing quinoline after pickling enters into alkaline bath, and the KOH solution with 10～20% carries out alkali cleaning, and the per kilogram indoles adds 13.0～17.0 liters of KOH solution, this groove is heated, keep boiling state, also will constantly stir, and extract the isolating moisture content of evaporation out;
(3) the technical methylnaphthalene fraction after the alkali cleaning enters into strainer, and the impurity that contains indoles on the strainer Inner filter net is extracted out;
(4) rectifying is carried out at the middle part that enters into rectifying tower of the technical methylnaphthalene fraction hopper after the removal of impurity after the alkali cleaning, extracts α-methylnaphthalene product in the rectifying tower middle and upper part, is extracting β-methylnaphthalene product near place, rectifying tower top.
The method of extracting α-methylnaphthalene and β-methylnaphthalene from the technical methylnaphthalene fraction relies on isolated plant to finish.This device is mainly by raw material tank, hopper behind the decon, rectifying tower, crystallizer tank, suction filter, filtrate receiver, the vacuum pump feed heater, pump, the naphtalene oil groove, make condenser, β-methyl is the product groove how, α-methylnaphthalene groove is formed, for implementing to remove quinoline and the indoles in the technical methylnaphthalene fraction, so behind raw material tank by the pipe connection pickling tank, in pickling tank inside agitator and well heater are housed, high-order acid solution case uses pipe connection in pickling tank, the standing separation device by pipe connection between pickling tank and alkaline bath, high-order lye tank uses pipe connection in alkaline bath, agitator and well heater are housed in alkaline bath, are using the pipe connection strainer after alkaline bath and the impurity elimination between the hopper.
In order to regulate, control the flow and the concentration of the KOH solution that will enter pickling tank H2SO4 solution and will enter alkaline bath according to the amount of contained quinoline, indoles in the technical methylnaphthalene fraction, so between high-order acid solution case and the pickling tank, high-order lye tank and and alkaline bath between, with pipe connection under meter is arranged respectively.
Adopt present method and device to extract α-methylnaphthalene and β-first naphthalene product from the technical methylnaphthalene fraction, the product purity of extraction reaches more than 90%, and β-first naphthalene product extraction rate reached is more than 60%, and general rectifying tower gets final product, and technology is simple, and is easy to operate.
Description of drawings is as follows:
Accompanying drawing 1 is for extracting the device synoptic diagram of α-methylnaphthalene and β-methylnaphthalene.
Further describe as follows below in conjunction with accompanying drawing:
Mainly contain α-methylnaphthalene and β-methylnaphthalene and be 78.6%, quinoline is 8.4%, to be 3.9% technical methylnaphthalene fraction enter into pickling tank 8 and concentration from raw material tank 1 to indoles is that 20% H2SO4 solution carries out chemical reaction, its H2SO4 solution add-on is that 30ml adds by the per kilogram quinoline, by steam well heater 10 is heated, be heated more than 60 ℃, and be controlled within 65 ℃, agitator 9 constantly stirs, so that evenly, and sufficient reacting.Entering standing separation device 12 middle parts then separates, following liquid is the moisture content that contains quinoline, and for removing the technical methylnaphthalene fraction of quinoline, containing quinoline in the technical methylnaphthalene fraction after pickling is 0.1% above, the moisture that will contain quinoline is extracted out, can be used as the raw material of producing quinoline.
The technical methylnaphthalene fraction of removing behind the impurity quinoline enters into alkaline bath 13, mixes with 12% KOH solution from high-order lye tank 14.By steam well heater 10 is heated, make the technical methylnaphthalenes in the alkaline bath 13 be the boiling shape, promptly more than 241 ℃, and constantly stir, will evaporate isolating moisture and extract out from alkaline bath 13 tops with agitator 9.
Technical methylnaphthalene fraction after alkali cleaning enters in the strainer 15 by pipeline, the impurity that contains indoles on strainer 15 Inner filter nets is extracted out, as the raw material of producing indoles.Indoles content is 0.3% in the technical methylnaphthalene fraction after alkali cleaning is filtered.
After hopper behind the decon 2 and feed heater 17 heating, enter into rectifying tower 3 through the technical methylnaphthalene fraction after KOH alkali liquid washing, the filtration, its reflux in tower is than being normal value, promptly 10～15, the district is promptly gathered at α-methylnaphthalene in middle and upper part at rectifying tower 3, dna purity is α-methylnaphthalene product of 90%, at rectifying tower 3 tops is β-methylnaphthalene product that β-methylnaphthalene gathers district's dna purity＞90%, and the light component of cat head is after the condensation cooling, and part is returned the stream part and entered the front-end volatiles groove.
When since in the technical methylnaphthalene fraction α-methylnaphthalene and β-methylnaphthalene content less than 70%, impurity is higher, or owing to the operation reason, cause β-methylnaphthalene product purity after rectifying less than 90%, greater than 80% o'clock, perhaps require its product purity to reach 95% when above, then β-methylnaphthalene the product that extracts from cat head can pass through crystallizer 4, crystallization is carried out in cooling through water coolant, enters into suction filter 5 then and carries out the suction filtration separation, extracts β-methylnaphthalene product from suction filter 5 napexes, purity is not high enters filtrate receiver 6 from the bottom, separate through vacuum tank 22, top air is extracted out by vacuum pump 7, following fraction then behind the decon hopper 2 participate in rectifying once more.
When H2SO4 concentration greater than 25% the time, the technical methylnaphthalene fraction is lost in more than 5%, its concentration was less than 15% o'clock, then the quinoline poor removal effect promptly also has 0.3% above quinoline to be present in the technical methylnaphthalene, influences product purity.
Fig. 1 is for being exclusively used in the device that extracts α-methylnaphthalene and β-methylnaphthalene from the technical methylnaphthalene fraction: raw material tank 1 by pipe connection in pickling tank 8, its entrance is at the middle part of pickling tank 8, the connecting tube of pickling tank 8 bottoms is connected standing separation device 12 middle parts, be connected in the middle part of alkaline bath 13 from standing separation device 12 top introduction pipes, the pipeline of drawing from alkali cleaning 13 inside is connected to strainer 15 tops, on strainer 15 filter screens, for containing the impurity of indoles.The pipeline of drawing from strainer 15 bottoms is connected to hopper 2 tops after the impurity elimination, with pump this raw material is squeezed into the middle part of rectifying tower 3, gathers district's introduction pipe from the middle and upper part α-methylnaphthalene of rectifying tower 3 and extracts α-methylnaphthalene product out.Gather district's introduction pipe from the β-methylnaphthalene of rectifying tower 3, extract β-methylnaphthalene product.For ease of further purification, use pipe connection crystallizer 4 suction filters 5, filtrate receiver 6, vacuum pump 7 at extraction β-methylnaphthalene product conduit place in addition, promptly work as the β-methylnaphthalene product purity of extraction less than 90%, or the β of customer requirements-methylnaphthalene product reaches 95% when above, and doing further purifies uses.
Use pipe connection under meter 16 between high-order acid solution case 11 and the pickling tank 8, the agitator 9 by driven by motor is housed on pickling tank 8 tops, coil heater 10 is contained in bottoms in the pickling tank 8.Use pipe connection under meter 16 between high-order lye tank 14 and the alkaline bath 13, the agitator 9 by driven by motor is arranged on the top of alkaline bath 13, alkaline bath 13 inner bottom parts have coil heater 10, at the top of alkaline bath 13 introduction pipe, to extract isolated water out.
Claims (3)
1, a kind of method of extracting α-methylnaphthalene and β-methylnaphthalene from the technical methylnaphthalene fraction is characterized in that extraction process is:
(1) be that 15～25% H2SO4 solution carries out pickling with technical methylnaphthalene fraction concentration in pickling tank 8, the per kilogram quinoline adds 3.5～4.0 liters of H2SO4 solution, this groove internal heating temperature is controlled at 60～65 ℃, and constantly stir, enter then in the standing separation device 12 and separate, extract the moisture content that contains quinoline out;
(2) the technical methylnaphthalene fraction after pickling enters into alkaline bath 13, KOH solution with 10～20% carries out alkali cleaning, and the per kilogram indoles adds 13.0～17.0 liters of KOH solution, and the groove internal heating also keeps boiling state, constantly stir, and extract the isolated moisture content of evaporation out;
(3) the technical methylnaphthalene fraction after the alkali cleaning enters into strainer 15, and the impurity that contains indoles on the filter screen is extracted out;
(4) the technical methylnaphthalene fraction after the alkali cleaning carries out rectifying by the middle part that strainer 15 hopper 2 after the removal of impurity enters into rectifying tower 3, extracts α-methylnaphthalene product in the middle and upper part of rectifying tower 3, extracts β-methylnaphthalene product at the place, top near rectifying tower 3.
2, a kind of device that from the technical methylnaphthalene fraction, extracts α-methylnaphthalene and β-methylnaphthalene, mainly by raw material tank 1, hopper 2 behind the decon, rectifying tower 3, crystallizer 4, suction filter 5, filtrate receiver 6, vacuum pump 7 raw materials heating 17, pump 18, naphtalene oil groove 19, condenser 20, β-methylnaphthalene product groove 21, vacuum tank 22, evaporation tank 23, α-methylnaphthalene groove is formed, it is characterized in that raw material tank 1 back is by pipe connection pickling tank 8, agitator 9 and well heater 10 are housed in the pickling tank 8, high moor tank-washer 11 usefulness pipe connection are in pickling tank 8, standing separation device 12 by pipe connection between pickling tank 8 and alkaline bath 13, high-order lye tank 14 usefulness pipe connection are in alkaline bath 13, well heater 10 is housed in alkaline bath 13, agitator 9 is being used pipe connection strainer 15 between the hopper 2 behind alkaline bath 13 and the decon.
3, the device that extracts α-methylnaphthalene and β-methylnaphthalene from the technical methylnaphthalene fraction according to claim 2, its feature is equipped with under meter 16 between high-order acid solution case 11 and pickling tank 8 respectively between high-order lye tank 14 and alkaline bath 13.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN94113628A CN1044703C (en) | 1994-11-02 | 1994-11-02 | Method and apparatus for extracting alpha-methyl naphthalene and beta-methylnaphthalene |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN94113628A CN1044703C (en) | 1994-11-02 | 1994-11-02 | Method and apparatus for extracting alpha-methyl naphthalene and beta-methylnaphthalene |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1122320A true CN1122320A (en) | 1996-05-15 |
| CN1044703C CN1044703C (en) | 1999-08-18 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN94113628A Expired - Fee Related CN1044703C (en) | 1994-11-02 | 1994-11-02 | Method and apparatus for extracting alpha-methyl naphthalene and beta-methylnaphthalene |
Country Status (1)
| Country | Link |
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| CN (1) | CN1044703C (en) |
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100393677C (en) * | 2005-06-30 | 2008-06-11 | 天津大学 | Process for extracting 1-methylnaphthalene and 2-methylnaphthalene from tar |
| CN101898932A (en) * | 2010-07-21 | 2010-12-01 | 莱芜雅鲁生化有限公司 | Purifying process of beta-methylnaphthalene |
| CN102114396A (en) * | 2010-12-10 | 2011-07-06 | 江阴市盛通化工有限公司 | Non-quinoline dispersant MF and production process |
| CN101270028B (en) * | 2007-03-23 | 2012-01-11 | 宝山钢铁股份有限公司 | purification process of alpha-methylnaphthalene |
| CN103212214A (en) * | 2012-01-20 | 2013-07-24 | 鞍钢集团工程技术有限公司 | Method for producing beta-methylnaphthalene by using coal tar washing oil for continuously distilling |
| CN106336338A (en) * | 2015-07-09 | 2017-01-18 | 上海宝钢化工有限公司 | Method for removing quinoline in DMNO-3 |
| CN106966850A (en) * | 2017-04-20 | 2017-07-21 | 鹏辰新材料科技股份有限公司 | A kind of preparation method of the methyl naphthalene of high-purity 1 |
| CN115073257A (en) * | 2022-08-03 | 2022-09-20 | 连云港鹏辰特种新材料有限公司 | Method for separating and purifying 1-methylnaphthalene from methylnaphthalene enrichment mother liquor |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3270074A (en) * | 1963-02-05 | 1966-08-30 | Ashland Oil Inc | Process for the production of pure methylnaphthalene |
| CN1040576A (en) * | 1989-09-19 | 1990-03-21 | 马红龙 | Technology for production of refined naphthalene by crystalization in solvents |
-
1994
- 1994-11-02 CN CN94113628A patent/CN1044703C/en not_active Expired - Fee Related
Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100393677C (en) * | 2005-06-30 | 2008-06-11 | 天津大学 | Process for extracting 1-methylnaphthalene and 2-methylnaphthalene from tar |
| CN101270028B (en) * | 2007-03-23 | 2012-01-11 | 宝山钢铁股份有限公司 | purification process of alpha-methylnaphthalene |
| CN101898932A (en) * | 2010-07-21 | 2010-12-01 | 莱芜雅鲁生化有限公司 | Purifying process of beta-methylnaphthalene |
| CN102114396A (en) * | 2010-12-10 | 2011-07-06 | 江阴市盛通化工有限公司 | Non-quinoline dispersant MF and production process |
| CN103212214A (en) * | 2012-01-20 | 2013-07-24 | 鞍钢集团工程技术有限公司 | Method for producing beta-methylnaphthalene by using coal tar washing oil for continuously distilling |
| CN103212214B (en) * | 2012-01-20 | 2016-02-03 | 鞍钢集团工程技术有限公司 | A kind of method of being produced beta-methylnaphthalene by coal tar wash oil continuous still |
| CN106336338A (en) * | 2015-07-09 | 2017-01-18 | 上海宝钢化工有限公司 | Method for removing quinoline in DMNO-3 |
| CN106966850A (en) * | 2017-04-20 | 2017-07-21 | 鹏辰新材料科技股份有限公司 | A kind of preparation method of the methyl naphthalene of high-purity 1 |
| CN106966850B (en) * | 2017-04-20 | 2020-05-05 | 鹏辰新材料科技股份有限公司 | Preparation method of high-purity 1-methylnaphthalene |
| CN115073257A (en) * | 2022-08-03 | 2022-09-20 | 连云港鹏辰特种新材料有限公司 | Method for separating and purifying 1-methylnaphthalene from methylnaphthalene enrichment mother liquor |
| CN115073257B (en) * | 2022-08-03 | 2023-10-27 | 连云港鹏辰特种新材料有限公司 | Method for separating and purifying 1-methylnaphthalene from methylnaphthalene enrichment mother liquor |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1044703C (en) | 1999-08-18 |
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