CN1220256A - Process for reduction of methylaniline from nitro-toluene - Google Patents
Process for reduction of methylaniline from nitro-toluene Download PDFInfo
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- CN1220256A CN1220256A CN 97107142 CN97107142A CN1220256A CN 1220256 A CN1220256 A CN 1220256A CN 97107142 CN97107142 CN 97107142 CN 97107142 A CN97107142 A CN 97107142A CN 1220256 A CN1220256 A CN 1220256A
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- monomethylaniline
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Abstract
The production process of methylphenylamine by reduction of methyl nitrobenzene, including charging reduction and pressure-relieving separation procedures, is characterized by that in the procedure of charging reduction, only adding methyl nitrobenzene,Raney's nickel catalyst and hydrogen gas in the reactor, and under the non-solvent condition, adopting liquid-phase catalytic reduction process to obtain the invented methylphenylamine. By adopting non-solvent method to make production the solvent recovering procedure is saved, investment is economized, technological process is simple, product quality is good and yield is high, and the catalyst also can be recovered for reuse. Said invention can be used for reduction of 0-, m- and p-nitrotoluene to produce 0-, m- and p- methyl aniline.
Description
The present invention relates to a kind of technology of producing monomethylaniline, particularly relate to a kind of technology of reduction of methylaniline from nitro-toluene.
The technology of reduction of methylaniline from nitro-toluene is to adopt iron powder reducing in the prior art, this technology comparative maturity, but it contains amine iron mud and can't handle in a large number in can producing in process of production.Another kind method is the method for the present hydrogenating reduction of using always, and this method is to be solvent with methyl alcohol, adds required catalyzer, under certain temperature and pressure, and hydrogen and nitrotoluene reaction.After reaction was finished, mixed solution filtered, leaves standstill or dynamic separation, the catalyzer of taking off mourning clothes.Solvent is ruined and is received the deaf again usefulness of circulation.Vinegar product monomethylaniline just can obtain finished product through separating.This side's enamel has solvent owing to deposit screening, makes the throughput of FU volume less, reclaims solvent simultaneously and has also brought cost height, problems such as environmental pollution.
By above-mentioned finding, have in the prior art that iron powder reducing produces that monomethylaniline brought can't handle in a large number contain that the equipment that amine iron mud and hydrogenating reduction brought is huge, the solvent recuperation solvent easily produces many disadvantages such as harm to workers ' health, and the utmost point is necessary to be improved.
The object of the invention is: overcome above-mentioned defective of the prior art, and provide a kind of under solvent-free condition, liquid phase catalytic hydrogenation makes the technology of reduction of methylaniline from nitro-toluene.
The objective of the invention is to reach by following technical scheme:
A kind of technology of reduction of methylaniline from nitro-toluene, it includes reinforced reduction operation and separation circuit, it is characterized in that only adding nitrotoluene, Raney's nickel catalyst and hydrogen in the reactor in reinforced reduction operation, under condition of no solvent, liquid phase catalytic reduction becomes monomethylaniline.
Purpose of the present invention can also further reach by following technical measures:
The technology of aforesaid reduction of methylaniline from nitro-toluene, it adds nitrotoluene in reactor in reinforced reduction operation, simultaneously with nitrotoluene with launch after Raney's nickel catalyst in 400: in the ratio adding reactor (1-3), and with H
2Pressure with 1.8-3.0Mpa feeds in the reactor, and the air displacement in the reactor is complete; Start agitator motor, its rotating speed is controlled at 500-750r.p.m,, make its interior temperature be controlled at 170 ± 10 ℃, begin reaction in the reactor and finish until reaction simultaneously to the reactor heating; In the release separation circuit, the temperature of reactor is reduced to 100 ± 5 ℃, release then, when pressure only has 0.3-0.4Mpa, after analysis nitro thing content is qualified, open the binder valve, thick monomethylaniline is depressed into the crude product groove, leave standstill; Make thick monomethylaniline and catalyst separating, with thick monomethylaniline through dehydration tower dehydration, rectifying tower rectifying get final product finished product.
The present invention compared with prior art has following advantage:
Solventless method is produced, and has deducted the solvent recuperation operation, has saved investment, and technical process is simple, good product quality, yield height.Catalyzer is recyclable to be utilized again.The generation wastewater flow rate is few, and tar is few.Environmental benefit is good, and running cost is low, and safety and sanitation are good, and adaptability is strong, can be used for the neighbour,, the reduction of para-nitrotoluene, produce adjacent,, to monomethylaniline.
Concrete technology of the present invention is provided in detail by the following drawings and embodiment.
Fig. 1 is a production technique block diagram of the present invention.
Describe in detail as the back below in conjunction with structure, feature and the effect thereof of accompanying drawing the preferred embodiment of invention:
The present invention is periodical operation.
Embodiment 1:
Is 0.5m by pipeline to volume
3The 400Kg purity of adding through being up to the standards is not less than 99% meta-nitrotoluene in the reactor, adds the about 2.0Kg of unfolded nickel catalyzator by pipeline simultaneously.The back is complete with the air displacement in the reactor by pipeline feeding hydrogen.Starting the agitator motor rotating speed is that 500r.p.m heats up, and hydrogen pressure machine top hole pressure is reconciled to 1.8Mpa, rises comparatively fast when temperature of reaction kettle is heated to 140 temperature when spending, and shows that reaction begins.Close heating steam, open cooling water valve, temperature is controlled at the 160-180 degree.React after 3-4 hour,, when temperature no longer rises, show that reaction finishes substantially when reactor pressure rises.At this moment close H
2Intake valve pressurize for some time so that a small amount of unreacted nitro thing continues reaction.When find reactor pressure descend when very slow (15 minutes do not see variation) show that reaction finishes.Open cooling water temperature to 100 ± 10 ℃, release, when pressure only has 0.3-0.4Mpa, analyze nitro thing content qualified after, open the binder valve, will be thick between monomethylaniline be depressed into the crude product groove, leave standstill.Make it and catalyst separating.Catalyst recovery is utilized again.Reactor suction again, intensification, driving.Monomethylaniline can get finished product through dehydration tower dehydration, rectifying tower rectifying between thick.
Embodiment 2:
Is 0.5m by pipeline to volume
3The 400Kg purity of adding through being up to the standards is not less than 99% para-nitrotoluene in the reactor, adds the about 2.0Kg of unfolded nickel catalyzator by pipeline simultaneously.The back is complete with the air displacement in the reactor by pipeline feeding hydrogen.Starting the agitator motor rotating speed is that 600r.p.m heats up, and hydrogen pressure machine top hole pressure is reconciled to 2.2Mpa, rises comparatively fast when temperature of reaction kettle is heated to 140 temperature when spending, and shows that reaction begins.Close heating steam, open cooling water valve, temperature is controlled at the 160-180 degree.React after 3-4 hour,, when temperature no longer rises, show that reaction finishes substantially when reactor pressure rises.At this moment close H
2Intake valve pressurize for some time so that a small amount of unreacted nitro thing continues reaction.When find reactor pressure descend when very slow (15 minutes do not see variation) show that reaction finishes.Open cooling water temperature to 100 ± 5 ℃, release, when pressure only has 0.3-0.4Mpa, analyze nitro thing content qualified after, open the binder valve, will slightly be depressed into the crude product groove to monomethylaniline, leave standstill.Make it and catalyst separating.Catalyst recovery is utilized again.Reactor suction again, intensification, driving.Slightly can get finished product through dehydration tower dehydration, rectifying tower rectifying to monomethylaniline.
Embodiment 3:
Is 0.5m by pipeline to volume
3The 400Kg purity of adding through being up to the standards is not less than 99% Ortho Nitro Toluene in the reactor, adds the about 2.0Kg of unfolded nickel catalyzator by pipeline simultaneously.The back is complete with the air displacement in the reactor by pipeline feeding hydrogen.Starting the agitator motor rotating speed is that 750r.p.m heats up, and hydrogen pressure machine top hole pressure is reconciled to 3.0Mpa, when temperature of reaction kettle is heated to 140 rising of temperature when spending broads, shows that reaction wiped formula.Close heating steam-open cooling water valve greatly, temperature is controlled at 160-180 crosses.React after 3-4 hour,, when temperature no longer rises, show that reaction finishes substantially when reactor pressure rises.At this moment close H
2Intake valve pressurize for some time so that a small amount of unreacted nitro thing continues reaction.When find reactor pressure descend when very slow (15 minutes do not see variation) show that reaction finishes.Open cooling water temperature to 100 ± 5 ℃, release, when pressure only has 0.3-0.4Mpa, analyze nitro thing content qualified after, open the binder valve, thick o-toluidine is depressed into the crude product groove, leave standstill.Make it and catalyst separating.Catalyst recovery is utilized again.Reactor suction again, intensification, driving.Thick o-toluidine can get finished product through dehydration tower dehydration, rectifying tower rectifying.
Claims (2)
1. the technology of a reduction of methylaniline from nitro-toluene, it includes reinforced reduction operation and discharging separation circuit, it is characterized in that only adding nitrotoluene, Raney's nickel catalyst and hydrogen in the reactor in reinforced reduction operation, under condition of no solvent, liquid phase catalytic reduction becomes monomethylaniline.
2. the technology of reduction of methylaniline from nitro-toluene according to claim 1, it is characterized in that in reinforced reduction operation, in reactor, add nitrotoluene, simultaneously with nitrotoluene with launch after Raney's nickel catalyst in 400:(1-3) ratio adding reactor in, and with H
2Pressure with 1.8-3.0Mpa feeds in the reactor, and the air displacement in the reactor is complete; Start agitator motor, its rotating speed is controlled at 500-750r.p.m,, make its interior temperature be controlled at 170 ± 10 ℃, begin reaction in the reactor and finish until reaction simultaneously to the reactor heating; In the release separation circuit, the temperature of reactor is reduced to 100 ± 5 ℃, release then, when pressure only has 0.3-0.4Mpa, after analysis nitro thing content is qualified, open the binder valve, thick monomethylaniline is depressed into the crude product groove, leave standstill; Make thick monomethylaniline and catalyst separating, with thick monomethylaniline through dehydration tower dehydration, rectifying tower rectifying get final product finished product.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 97107142 CN1220256A (en) | 1997-10-07 | 1997-10-07 | Process for reduction of methylaniline from nitro-toluene |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 97107142 CN1220256A (en) | 1997-10-07 | 1997-10-07 | Process for reduction of methylaniline from nitro-toluene |
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| Publication Number | Publication Date |
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| CN1220256A true CN1220256A (en) | 1999-06-23 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN 97107142 Pending CN1220256A (en) | 1997-10-07 | 1997-10-07 | Process for reduction of methylaniline from nitro-toluene |
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Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101838206A (en) * | 2010-04-14 | 2010-09-22 | 江苏淮河化工有限公司 | Purification method of o-toluidine |
| CN102399154A (en) * | 2011-08-08 | 2012-04-04 | 江苏福斯特化工制造有限公司 | Method for producing methylaniline from nitrotoluene through liquid-phase hydrogenation reduction |
| CN102718666A (en) * | 2012-05-29 | 2012-10-10 | 吴江市屯村颜料厂 | Method for preparing paratoluidine |
| CN104098474A (en) * | 2014-07-28 | 2014-10-15 | 淮安嘉诚高新化工股份有限公司 | Device and method for producing methyl aniline through performing continuous liquid-phase catalytic hydrogenation reduction on nitrotoluene |
| CN105968018A (en) * | 2016-07-15 | 2016-09-28 | 江苏大华化学工业有限公司 | Solvent-free catalysis hydrogenation and reduction method of substituted nitrobenzene |
| CN109721499A (en) * | 2018-12-19 | 2019-05-07 | 南京杰科丰环保技术装备研究院有限公司 | A kind of nitrotoleune adds hydrogen to prepare the preparation method of methylaniline |
| CN114890901A (en) * | 2022-06-17 | 2022-08-12 | 老河口华辰化学有限公司 | Synthesis method for synthesizing m-toluidine by 2-chloro-3-nitrotoluene one-step method |
| CN115232012A (en) * | 2022-08-02 | 2022-10-25 | 福建康峰新材料有限公司 | Method for producing m-amino benzotrifluoride by solvent-free hydrogenation process |
-
1997
- 1997-10-07 CN CN 97107142 patent/CN1220256A/en active Pending
Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101838206A (en) * | 2010-04-14 | 2010-09-22 | 江苏淮河化工有限公司 | Purification method of o-toluidine |
| CN101838206B (en) * | 2010-04-14 | 2013-04-24 | 江苏淮河化工有限公司 | Purification method of o-toluidine |
| CN102399154A (en) * | 2011-08-08 | 2012-04-04 | 江苏福斯特化工制造有限公司 | Method for producing methylaniline from nitrotoluene through liquid-phase hydrogenation reduction |
| CN102718666A (en) * | 2012-05-29 | 2012-10-10 | 吴江市屯村颜料厂 | Method for preparing paratoluidine |
| CN104098474A (en) * | 2014-07-28 | 2014-10-15 | 淮安嘉诚高新化工股份有限公司 | Device and method for producing methyl aniline through performing continuous liquid-phase catalytic hydrogenation reduction on nitrotoluene |
| CN104098474B (en) * | 2014-07-28 | 2016-01-20 | 淮安嘉诚高新化工股份有限公司 | Nitrotoluene Continuous Liquid Phase catalytic hydrogenating reduction produces the device and method of monomethylaniline |
| CN105968018A (en) * | 2016-07-15 | 2016-09-28 | 江苏大华化学工业有限公司 | Solvent-free catalysis hydrogenation and reduction method of substituted nitrobenzene |
| CN105968018B (en) * | 2016-07-15 | 2017-06-16 | 江苏大华化学工业有限公司 | A kind of method of solvent-free catalysis substituted-nitrobenzene hydrogenating reduction |
| CN109721499A (en) * | 2018-12-19 | 2019-05-07 | 南京杰科丰环保技术装备研究院有限公司 | A kind of nitrotoleune adds hydrogen to prepare the preparation method of methylaniline |
| CN114890901A (en) * | 2022-06-17 | 2022-08-12 | 老河口华辰化学有限公司 | Synthesis method for synthesizing m-toluidine by 2-chloro-3-nitrotoluene one-step method |
| CN115232012A (en) * | 2022-08-02 | 2022-10-25 | 福建康峰新材料有限公司 | Method for producing m-amino benzotrifluoride by solvent-free hydrogenation process |
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