CN1472184A - Continuous preparation of m-toluidine - Google Patents
Continuous preparation of m-toluidine Download PDFInfo
- Publication number
- CN1472184A CN1472184A CNA031282725A CN03128272A CN1472184A CN 1472184 A CN1472184 A CN 1472184A CN A031282725 A CNA031282725 A CN A031282725A CN 03128272 A CN03128272 A CN 03128272A CN 1472184 A CN1472184 A CN 1472184A
- Authority
- CN
- China
- Prior art keywords
- cresol
- reaction
- crude product
- meta
- aminotoluene
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Solid-Sorbent Or Filter-Aiding Compositions (AREA)
Abstract
A process for continuously preparing meta-tolylphenol includes such steps as continuously adding the diazonium salt of meta-tolylamine to diluted sulfuric acid, and reacting at 106-150 deg.C while controlling the concentration of sulfuric acid to 25-64 wt.%. Its advantages are low cost, high output rate, small reactor volume, and cyclic use of sulfuric acid after treated by macroreticular resin.
Description
Technical field
The present invention relates to the method that a kind of serialization prepares m-cresol, belong to field of fine chemical.
Background technology
Be converted into the general at present production method of being interrupted that adopts of m-cresol from meta-aminotoluene by diazotization, hydrolysis reaction.This method is carried out the diazonium salt solution that diazotization reaction generates meta-aminotoluene at low temperatures with Sodium Nitrite, sulfuric acid, meta-aminotoluene, again the meta-aminotoluene diazonium salt solution is joined the reaction that is hydrolyzed in the ebullient dilute sulphuric acid, the m-cresol that reaction generates steams with water vapour by distillation, stays the m-cresol in the reactor and the m-cresol that steams steams solvent again and obtains after solvent extraction.This method be discontinuously, batch production, need very large equipment volume, use a large amount of solvents, yield is generally lower, only about 70%.Because the viscous tar shape material that side reaction forms floats over the reaction solution surface, has hindered m-cresol and has taken reaction system out of with distillation, makes reaction time long.In addition, the sulfuric acid amount of using in the above-mentioned reaction is big, and three wastes treatment capacity is also big.
Summary of the invention
Problem to be solved by this invention provides the method that a kind of serialization prepares m-cresol, this method not only reaction time shorter, and reaction yield is higher, the equipment used volume is less.
Technical scheme provided by the invention is: a kind of serialization prepares the method for m-cresol, add the meta-aminotoluene diazonium salt in the dilute sulphuric acid of 25～64wt% continuously, adding speed by control meta-aminotoluene diazonium salt, steam the speed of water and overflowing liquid take-off rate from overflow port, make that vitriolic concentration remains on 25～64wt% in the reactor, temperature of reaction remains on 106～150 ℃, the m-cresol that reaction generates steams with wet distillation continuously, and the byproduct of reaction tarry matters and the sulfur waste acid that contain m-cresol overflow from the overflow port of reactor continuously; The m-cresol crude product that separates, purifies and steam and overflow promptly gets required m-cresol.
Above-mentioned water that steams and m-cresol mixture are isolated the m-cresol crude product after layering, the water after the separation discharges behind absorption with macroporous adsorbent resin; With the aqueous sodium hydroxide solution of 2～10wt% or the m-cresol crude product in steam or the methanol-eluted fractions recovery macroporous adsorbent resin.
Acid separates after layering the above-mentioned byproduct of reaction tarry matters that contains m-cresol that overflows from the reactor overflow port with sulfur waste, and the sulfur waste acid after the separation recycles as the raw material of preparation meta-aminotoluene diazonium salt behind the absorption with macroporous adsorbent resin organic substance; Tarry matters discharges after the m-cresol crude product is reclaimed in underpressure distillation.
The fine chemical product m-cresol that the present invention makes extensively uses as the raw material of medicine, agricultural chemicals, dyestuff, spices.
The present invention compared with prior art has the following advantages:
1. the present invention not only can under normal circumstances continuously produce m-cresol, and production cost is lower, and the m-cresol product yield of content 〉=99.5% has improved about 10% than discontinuous preparation method more than 84%.2/5 of disconnected production.Not only reduce investment, and saved energy consumption, lowered running expense.
3. after heavy-gravity tarry by product overflowed from overflow port, the m-cresol solution that reaction is generated was taken out of with wet distillation easily, has improved the feed rate of diazonium salt, has shortened reaction time.
4. reaction can be carried out under solvent-free, has saved the trouble of separating solvent and reclaiming solvent, and has lowered material consumption greatly.
5. the sulfur waste acid that hydrolysis reaction produced can be used as preparation meta-aminotoluene diazonium salt after macroporous adsorbent resin is handled raw material recycles, and has solved a difficult problem of being interrupted a large amount of spent acid dischargings of hydrolysis reaction.
Description of drawings
Accompanying drawing is a process flow diagram of the present invention.
Embodiment
Below in conjunction with accompanying drawing the present invention is further described;
Embodiment 1: with plural reactor at 0～10 ℃ of diazonium salt solution that alternately prepares meta-aminotoluene according to a conventional method.Referring to accompanying drawing, in the reactor of 500L, add the sulfuric acid 281kg of 20wt%, add the 25kg meta-aminotoluene again, under agitation keep 0～10 ℃ of temperature of reaction, the solution that adding 17.5kg Sodium Nitrite is dissolved in 35kg water prepares the meta-aminotoluene diazonium salt solution by diazotization reaction.
In the 500L hydrolytic reaction pot, add the sulfuric acid 300L of 30wt%, under 105～110 ℃, continuously join the above-mentioned meta-aminotoluene diazonium salt solution that makes in the hydrolytic reaction pot; The m-cresol that reaction generates is taken out of continuously with wet distillation, overflows dilute sulphuric acid continuously and has the tarry by product of m-cresol from the survey overflow port of reactor simultaneously.
Behind standing demix, isolate sulfur waste acid and the tarry matters (containing pyrogaelol) that contains m-cresol from the overflowing liquid that overflow port overflows.Isolated useless dilute sulphuric acid is used to prepare the meta-aminotoluene diazonium salt solution as raw material after macroporous adsorbent resin (as commercially available XDA-1 type resin) adsorb organic compound; Isolating carbonizing matter discharges after the m-cresol crude product is reclaimed in distillation.
Water that wet distillation is taken out of and m-cresol (water, phenol) are isolated the m-cresol crude product behind standing demix; The water of telling discharges (containing m-cresol＜0.02 grams per liter in the waste water up to standard of discharging) behind absorption with macroporous adsorbent resin.Aqueous sodium hydroxide solution or steam wash-out with 2～10wt% reclaims the m-cresol crude product that is adsorbed on the resin again.
It is 23.68kg that all m-cresol crude products (crude phenols) merge the back, and content is 95～97wt%.Getting the m-cresol finished product after the rectifying is 21.37kg, and content 〉=99.5%, yield are 84.7%.
Embodiment 2: meta-aminotoluene diazotization is with embodiment 1; Adopt the reaction that is hydrolyzed of the sulfuric acid of 50wt%, hydrolysising reacting temperature is 110～150 ℃; The water that is steamed discharges (containing m-cresol＜0.02 grams per liter in the water) after macroporous resin adsorption.Reclaim the m-cresol crude product with methanol-eluted fractions.Sulfur waste acid is used to prepare the meta-aminotoluene diazonium salt solution as raw material after resin absorption.With adsorbed organic matter matter on the water vapour wash-out resin.Obtaining content is the thick m-cresol 24.04kg of 95～97wt%.Thick m-cresol obtains the m-cresol finished product 21.69kg of content 〉=99.5% after rectifying, yield is 85.96%.
Claims (3)
1. a serialization prepares the method for m-cresol, it is characterized in that: add the meta-aminotoluene diazonium salt in the dilute sulphuric acid of 25～64wt% continuously, adding speed, the speed that steams water and overflowing liquid by control meta-aminotoluene diazonium salt is from the take-off rate of overflow port, make that vitriolic concentration remains on 25～64wt% in the reactor, temperature of reaction remains on 106～150 ℃, the m-cresol that reaction generates steams with wet distillation continuously, and the byproduct of reaction tarry matters and the sulfur waste acid that contain m-cresol overflow from the overflow port of reactor continuously; The m-cresol crude product that separates, purifies and steam and overflow promptly gets required m-cresol.
2. method according to claim 1 is characterized in that: above-mentioned water that steams and m-cresol mixture are isolated the m-cresol crude product after layering, the water after the separation discharges behind absorption with macroporous adsorbent resin; With the aqueous sodium hydroxide solution of 2～10wt% or the m-cresol crude product in steam or the methanol-eluted fractions recovery macroporous adsorbent resin.
3. method according to claim 1 and 2, it is characterized in that: the m-cresol crude product is isolated in above-mentioned byproduct of reaction tarry matters that contains m-cresol and the sulfur waste acid that overflows from the reactor overflow port after layering, and the sulfur waste acid after the separation recycles as the raw material of preparation meta-aminotoluene diazonium salt behind the absorption with macroporous adsorbent resin organic substance; Tarry matters discharges after the m-cresol crude product is reclaimed in underpressure distillation.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 03128272 CN1202057C (en) | 2003-07-03 | 2003-07-03 | Continuous preparation of m-toluidine |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 03128272 CN1202057C (en) | 2003-07-03 | 2003-07-03 | Continuous preparation of m-toluidine |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1472184A true CN1472184A (en) | 2004-02-04 |
| CN1202057C CN1202057C (en) | 2005-05-18 |
Family
ID=34153309
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 03128272 Expired - Fee Related CN1202057C (en) | 2003-07-03 | 2003-07-03 | Continuous preparation of m-toluidine |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1202057C (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101774893B (en) * | 2010-02-05 | 2012-12-05 | 江苏淮河化工有限公司 | Process for preparing m-cresol by nitrogen oxide gas |
-
2003
- 2003-07-03 CN CN 03128272 patent/CN1202057C/en not_active Expired - Fee Related
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101774893B (en) * | 2010-02-05 | 2012-12-05 | 江苏淮河化工有限公司 | Process for preparing m-cresol by nitrogen oxide gas |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1202057C (en) | 2005-05-18 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN1276929C (en) | Method for producing chitin, astaxanthin, protein, calcium powder and biological fertilizer from shrimp shell | |
| CN1799996A (en) | Wet method phosphoric acid purification method | |
| CN102241606B (en) | Clean production method of N-cyanoethylaniline | |
| US10562874B2 (en) | Process for the recovery of furfural | |
| JP5582812B2 (en) | Layer separation method | |
| CN102206196B (en) | Method for recovering morpholine from acidic waste water containing morpholine | |
| CN101343135A (en) | Method for treatment of low-concentration organic acid wastewater | |
| JP2013208108A (en) | Method for recovering acid, method for manufacturing sugar liquid and method of fermentation | |
| JP5581069B2 (en) | Acid recovery method, sugar solution production method, and fermentation method | |
| CN1202057C (en) | Continuous preparation of m-toluidine | |
| CN218778875U (en) | Device for separating and recovering alcohol and aldehyde from glyphosate mother liquor | |
| CN111576070B (en) | Method for removing poplar lignin by recycling acetic acid-hydrogen peroxide pretreatment liquid | |
| CN110270582B (en) | Treatment device and process for solid waste residues in nitromethane production | |
| CN103641793A (en) | Treatment method of AE (Active Ester) residual liquid | |
| CN112500268A (en) | Preparation process of 1, 3-propylene glycol methyl ether | |
| CN114409574A (en) | Preparation method of allyl benzenesulfonate | |
| CN1348947A (en) | Prepn process of vitamin A intermediate | |
| CN111848359A (en) | Method for separating phenolic substances in medium and low temperature coal tar | |
| KR100349038B1 (en) | Manufacturing method for a cohesive material of Poly aluminum Chloride | |
| CN109680296B (en) | Method for preparing eugenol by reacting ortho-methoxyphenol group decomposed from lignin with additional allyl | |
| CN103420882A (en) | Method for preparing L-methionine | |
| CN112876438B (en) | Separation and purification method of high-purity 3-acetamido-5-acetylfuran | |
| CN110105313B (en) | Double-circulation furfural production system and technology | |
| JP5657915B2 (en) | Methane fermentation method | |
| CN114736103B (en) | Method for separating propyl guaiacol and propyl syringol from lignin oil |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C19 | Lapse of patent right due to non-payment of the annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |