CN104478738A - Reaction method for continuously synthesizing diphenylamine from aniline - Google Patents
Reaction method for continuously synthesizing diphenylamine from aniline Download PDFInfo
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- CN104478738A CN104478738A CN201410661655.3A CN201410661655A CN104478738A CN 104478738 A CN104478738 A CN 104478738A CN 201410661655 A CN201410661655 A CN 201410661655A CN 104478738 A CN104478738 A CN 104478738A
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Abstract
The invention discloses a reaction method for continuously synthesizing diphenylamine from aniline. The reaction flow is as follows: firstly introducing an aniline raw material into an aniline high-level slot, and then introducing the aniline raw material into a metering slot and a two-stage series heat exchanger which is used for enabling reactants and raw materials to exchange heat, thereby enabling the raw materials to exchange heat and heat up; heating the raw materials; sequentially introducing the raw materials to a reactor A, a relay heater B, a reactor B, a relay heater C, a reactor C, a relay heater D and a reactor D which are connected in series to perform material reaction, and finally discharging the reacted materials from the reactor D; enabling the reaction materials to exchange heat and cool in the two-stage series heat exchanger; and introducing the cooled reaction materials into an ammonia and reaction liquor separator, and finally introducing the cooled reaction materials to a follow-up separating system, and returning the aniline raw materials to the aniline high-level slot for recycling. The reaction method for continuously synthesizing diphenylamine from aniline disclosed by the invention can be used for improving the heat exchange efficiency, comprehensively utilizing heat energy, saving energy resources, enabling the un-reacted aniline to pass through the follow-up separating system, and returning the recycled aniline to the aniline high-level slot of the reaction system for recycling.
Description
Technical field
The present invention relates to a kind of reaction method utilizing aniline continuous synthesizing diphenylamine, belong to chemical production field.
Background technology
China Patent No. is CN87107052.9, contacts to prepare pentanoic with aluminium oxide catalyst at about 380-475 DEG C of chien shih aniline; China Patent No. is CN95103700.5, discloses a kind of method by aniline syntehsizing diphenylamine.The present invention take aniline as raw material, at hydrogen and β zeolite/Al
2o
3there is the method for lower syntehsizing diphenylamine in catalyzer, adopt lower feeding manner, temperature of reaction is 250 ~ 400 DEG C, reaction pressure 1.5 ~ 4.5MPa, aniline Feed space velocities 0.05 ~ 1.0h
-1, the volume ratio 20 ~ 600 of hydrogen and aniline, with this understanding, in product, diphenylamine content is more than 22%, by product <0.5%.Liquid reacting product, reaction generation ammonia and hydrogen are separated from each other by vapor-liquid separation under reaction pressure, water absorption dehydrogenating and hydrogen desiccation, hydrogen recycle uses.
China Patent No. is CN02112535.X, disclose a kind of aniline syntehsizing diphenylamine method adding nitrogen in reactor, its processing step is followed successively by: aniline measures, and is measured and is sent into aniline well heater by aniline raw material by aniline scale tank, volume pump, nitrogen buffers packet; Aniline heats, and the aniline raw material after metering carries out heating to 330-370 DEG C; Reaction, raw material aniline after heating is located at and is equipped with in the reactor of catalyzer, nitrogen is added in reactor, pressure in reactor is 1.6-2.5MPa, aniline is 0.15-0.2/h with the air speed ratio of catalyzer, temperature is 320-360 DEG C, is then lowered the temperature by raw produce interchanger, makes temperature reach the phase less than 150 DEG C.
China Patent No. is CN201110058065.8, disclose a kind of method be by amino benzenes compounds and phenol compound under high-temperature and high-pressure conditions, under the pimelinketone and metal catalyst existence of catalytic amount, by system internal condensation-dehydrogenation-hydrogenation process, direct syntehsizing diphenylamine compounds.
China Patent No. is CN201110313288.4, disclose a kind of method by aniline continuous synthesizing diphenylamine, contacted with hydrogen before aniline raw material enters reactor, hydrogen is made to be dissolved in aniline raw material, the aniline raw material having dissolved hydrogen enters in aniline continuous synthesizing diphenylamine reactor, the aniline raw material having dissolved hydrogen, by beds, carries out the reaction of aniline syntehsizing diphenylamine, there is not the hydrogen of gas phase in beds.
China Patent No. is CN201210552308.8, disclose the diphenylamine reaction device of a kind of biphenyl heating, comprise biphenyl heat conducting oil boiler, described biphenyl heat conducting oil boiler is connected with biphenyl well heater by pipeline, described biphenyl well heater is connected to reactor and raw produce interchanger, described raw produce interchanger is connected with flash tank, and described flash tank is also connected with flash condenser, and described biphenyl heat conducting oil boiler is connected with water dust scrubber by pipeline.
In sum, above in technology disclosed in these patents, some temperature of reaction height 380-475 DEG C; Needing of having adds hydrogen; Some needs add nitrogen in reaction process, and need the follow-up Ammonia recovery operation needs constantly not solidifying tail gas of discharge, the not solidifying tail gas of continuous blow-down must carry ammonia emission secretly, is unfavorable for the protection of environmental resources, and waste resource, operating process becomes loaded down with trivial details.
Summary of the invention
The object of the invention is to for deficiency of the prior art, a kind of reaction method utilizing aniline continuous synthesizing diphenylamine is provided, do not have at the beginning to need during material to replace with nitrogen in reactor, reactive system is made to be in anaerobic state, do not need to add nitrogen in reaction process, do not need hydrogen.
For solving the problems of the technologies described above, the technical solution used in the present invention is: a kind of reaction method utilizing aniline continuous synthesizing diphenylamine, its innovative point is: reaction process is: (1) aniline raw material is introduced into aniline header tank, then scale tank is entered, what enter two-stage tandem again carries out in the interchanger of heat exchange for reactant and raw material, carries out raw material heat exchange intensification;
(2) raw material after heat exchange is entered well heater and carry out heating raw materials intensification;
(3) raw material after heating up in step (2) is entered successively the reactor A of series connection, relaying well heater B, reactor B, relaying well heater C, reactor C, relaying well heater D, reactor D carries out material reaction, finally in reactor D out, become reaction mass;
(4) reaction mass in step (3) is carried out in the interchanger of heat exchange through two-stage tandem for reactant and raw material, carry out reaction mass heat exchange cooling;
(5) reaction mass after step (4) being lowered the temperature, by the reducing valve of the automatic control in heat exchanger tube, enters ammonia and reaction solution separator, finally enters subsequent separation system, isolates aniline raw material and returns aniline header tank and reuse.
Further, the concrete steps of described reaction process are as follows:
(1) from aniline material storaging tank, by raw material with pump pump to aniline header tank, enter scale tank, volume pump is again with the input speed of 3500kg/H, raw material is pumped into two-stage tandem be used for reactant and raw material carries out in the interchanger of heat exchange, by feeding temperature heat exchange to 260 ~ 265 DEG C;
(2) raw material after heat exchange is entered well heater and carry out heating raw materials intensification, the feeding temperature of raw material is risen to 295 ~ 330 DEG C, and heating mode is set to gradient increased temperature, and temperature rise rate is 0.106 DEG C/day;
(3) raw material being warming up to 295 ~ 330 DEG C in step (2) is entered successively the reactor A of series connection, relaying well heater B, reactor B, relaying well heater C, reactor C, relaying well heater D, reactor D, arrange the pressure of reactor A to D all between 2.2 MPa ~ 1.8MPa, and according to reactor A to the order of D, force value reduces successively, finally in reactor D out, become reaction mass;
(4) reaction mass in step (3) is carried out in the interchanger of heat exchange through two-stage tandem for reactant and raw material, carry out reaction mass heat exchange cooling, reaction mass temperature is down to less than 110 DEG C;
(5) reaction mass after step (4) being lowered the temperature, by the reducing valve of the automatic control in heat exchanger tube, enters ammonia and reaction solution separator, finally enters subsequent separation system, isolates aniline raw material and returns aniline header tank and reuse.
Further, in four reactors in described step (3), commercially available porous solid-supported catalyst is all installed.
Further, described four relaying well heaters, in step (3) whole reaction process, to the continuous additional heat of reactor, maintain reactor reaction temperature-resistant.
Main reaction chemical principle of the present invention is as follows:
2C
6H
5NH
2= C
6H
5NHC
6H
5+ NH
3
Beneficial effect of the present invention is as follows:
(1) reaction method utilizing aniline continuous synthesizing diphenylamine of the present invention, by the cascade reaction technology that multiple reactors in series is reacted, the reaction conversion ratio improving syntehsizing diphenylamine is 16 ~ 32%, the interchanger carried out for reactant and raw material of two-stage tandem, improve heat exchange efficiency, by heat integration, save energy, unreacted aniline can be made by separation system below, and the aniline header tank that the aniline of recovery is back to reactive system is reused simultaneously.
(2) reaction method utilizing aniline continuous synthesizing diphenylamine of the present invention, solve conventional in reactor when there is no material at the beginning, need to replace with nitrogen, with the problem making reactive system be in anaerobic state, do not need to add nitrogen in reaction process, do not need hydrogen.
(3) the specific material selected in aniline conversion and production method of the present invention in main reaction of the present invention enters these conditions of sequencing, temperature, pressure, catalyzer duration of service etc. and changes closely related, the aniline remaining 65 ~ 85% in reaction solution does not react, return aniline header tank after being separated with subsequent separation system to reuse, higher by 5 ~ 8% than the utilization ratio of aniline raw material in the past.
(4) side reaction that the present invention produces can generate 2-picoline, 4-ethylaniline, acridine, indoles, 4-(1-methylethyl-N-phenyl) aniline, side reaction product total amount only accounts for 0.5 ~ 1% of product pentanoic amount.
Embodiment
Below in conjunction with specific embodiment, technical scheme of the present invention is elaborated.
Embodiment 1
A kind of reaction process concrete steps of the reaction method of aniline continuous synthesizing diphenylamine that utilize of the present invention are as follows:
(1) from aniline material storaging tank, by raw material with pump pump to aniline header tank, enter scale tank, volume pump is again with the input speed of 3500kg/H, raw material is pumped into two-stage tandem be used for reactant and raw material carries out in the interchanger of heat exchange, by feeding temperature heat exchange to 260 DEG C;
(2) raw material after heat exchange is entered well heater and carry out heating raw materials intensification, the feeding temperature of raw material is risen to 295 DEG C, and heating mode is set to gradient increased temperature, and temperature rise rate is 0.106 DEG C/day; (pass with catalyzer duration of service, temperature of reaction from 295 DEG C slowly gradual change be increased to 330 DEG C).
(3) raw material being warming up to 295 DEG C in step (2) is entered successively the reactor A of series connection, relaying well heater B, reactor B, relaying well heater C, reactor C, relaying well heater D, reactor D, the porous solid-supported catalyst of purchase is all housed in four reactors, pressure is followed successively by 2.2 MPa, 2.1MPa, 2.0MPa, 1.9MPa from reactor A to D, and relaying well heater gives reactor additional heat in reaction process, maintains temperature of reaction, last material out, becomes reaction mass in reactor D;
(4) reaction mass in step (3) is carried out in the interchanger of heat exchange through two-stage tandem for reactant and raw material, carry out reaction mass heat exchange cooling, reaction mass temperature is down to 110 DEG C;
(5) reaction mass after step (4) being lowered the temperature, by the reducing valve of the automatic control in heat exchanger tube, enters ammonia and reaction solution separator, finally enters subsequent separation system, and the aniline raw material isolating 65% returns aniline header tank and reuses.
In the present embodiment, solve conventional in reactor when there is no material at the beginning, need to replace with nitrogen, with the problem making reactive system be in anaerobic state, do not need to add nitrogen in reaction process, do not need hydrogen.The reaction conversion ratio of syntehsizing diphenylamine is 32%, and residue aniline raw material is 65%, and exceed 8% than the utilization ratio of conventional production process, side reaction product total amount only accounts for 1% of product pentanoic amount.
Embodiment 2
On the basis of embodiment 1, change each step reaction parameter in reaction method, be specially: feeding temperature heat exchange to 265 DEG C, feeding temperature rise to 330 DEG C, pressure is followed successively by 2.1MPa, 2.0MPa from reactor A to D, 1.9MPa, 1.8MPa, reaction mass temperature are down to 100 DEG C; After final reaction thing enters subsequent separation system, the aniline raw material isolating 75% returns aniline header tank and reuses.
In the present embodiment, the reaction conversion ratio of syntehsizing diphenylamine is 26%, and residue aniline raw material is 75%, and exceed 6% than the utilization ratio of conventional production process, side reaction product total amount only accounts for 0.8% of product pentanoic amount.
Embodiment 3
On the basis of embodiment 1 or 2, change each step reaction parameter in reaction method, be specially: feeding temperature heat exchange to 263 DEG C, feeding temperature rise to 300 DEG C, pressure is followed successively by 2.2 MPa, 2.0MPa from reactor A to D, 1.9MPa, 1.8MPa, reaction mass temperature are down to 110 DEG C; After final reaction thing enters subsequent separation system, the aniline raw material isolating 85% returns aniline header tank and reuses.
In the present embodiment, the reaction conversion ratio of syntehsizing diphenylamine is 18%, and residue aniline raw material is 85%, and exceed 5% than the utilization ratio of conventional production process, side reaction product total amount only accounts for 0.5% of product pentanoic amount.
More than show and describe ultimate principle of the present invention and principal character and advantage of the present invention.The technician of the industry should understand; the present invention is not restricted to the described embodiments; what describe in above-described embodiment and specification sheets just illustrates principle of the present invention; without departing from the spirit and scope of the present invention; the present invention also has various changes and modifications, and these changes and improvements all fall in the claimed scope of the invention.Application claims protection domain is defined by appending claims and equivalent thereof.
Claims (4)
1. one kind utilizes the reaction method of aniline continuous synthesizing diphenylamine, it is characterized in that: reaction process is: (1) aniline raw material is introduced into aniline header tank, then enter scale tank, then enter two-stage tandem carry out in the interchanger of heat exchange for reactant and raw material, carry out raw material heat exchange intensification;
(2) raw material after heat exchange is entered well heater and carry out heating raw materials intensification;
(3) raw material after heating up in step (2) is entered successively the reactor A of series connection, relaying well heater B, reactor B, relaying well heater C, reactor C, relaying well heater D, reactor D carries out material reaction, finally in reactor D out, become reaction mass;
(4) reaction mass in step (3) is carried out in the interchanger of heat exchange through two-stage tandem for reactant and raw material, carry out reaction mass heat exchange cooling;
(5) reaction mass after step (4) being lowered the temperature, by the reducing valve of the automatic control in heat exchanger tube, enters ammonia and reaction solution separator, finally enters subsequent separation system, isolates aniline raw material and returns aniline header tank and reuse.
2. the reaction method utilizing aniline continuous synthesizing diphenylamine according to claim 1, is characterized in that: the concrete steps of described reaction process are as follows:
(1) from aniline material storaging tank, by raw material with pump pump to aniline header tank, enter scale tank, volume pump is again with the input speed of 3500kg/H, raw material is pumped into two-stage tandem be used for reactant and raw material carries out in the interchanger of heat exchange, by feeding temperature heat exchange to 260 ~ 265 DEG C;
(2) raw material after heat exchange is entered well heater and carry out heating raw materials intensification, the feeding temperature of raw material is risen to 295 ~ 330 DEG C, and heating mode is set to gradient increased temperature, and temperature rise rate is 0.106 DEG C/day;
(3) raw material being warming up to 295 ~ 330 DEG C in step (2) is entered successively the reactor A of series connection, relaying well heater B, reactor B, relaying well heater C, reactor C, relaying well heater D, reactor D, arrange the pressure of reactor A to D all between 2.2 MPa ~ 1.8MPa, and according to reactor A to the order of D, force value reduces successively, finally in reactor D out, become reaction mass;
(4) reaction mass in step (3) is carried out in the interchanger of heat exchange through two-stage tandem for reactant and raw material, carry out reaction mass heat exchange cooling, reaction mass temperature is down to less than 110 DEG C;
(5) reaction mass after step (4) being lowered the temperature, by the reducing valve of the automatic control in heat exchanger tube, enters ammonia and reaction solution separator, finally enters subsequent separation system, isolates aniline raw material and returns aniline header tank and reuse.
3. the reaction method utilizing aniline continuous synthesizing diphenylamine according to claim 1 and 2, is characterized in that: be all provided with commercially available porous solid-supported catalyst in four reactors in described step (3).
4. the reaction method utilizing aniline continuous synthesizing diphenylamine according to claim 2, is characterized in that: described four relaying well heaters, in step (3) whole reaction process, to the continuous additional heat of reactor, maintain reactor reaction temperature-resistant.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105384683A (en) * | 2015-12-17 | 2016-03-09 | 南通新邦化工科技有限公司 | 2-Methyl-pyridine and 4-methylpyridine production method |
| CN107935862A (en) * | 2017-11-27 | 2018-04-20 | 南通新邦化工科技有限公司 | A kind of method of aniline continuous synthesizing diphenylamine |
| CN114805086A (en) * | 2022-05-16 | 2022-07-29 | 杰超橡塑南通有限公司 | Process and system for producing diphenylamine by adopting aniline continuous condensation method |
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| JPS6051152A (en) * | 1983-08-31 | 1985-03-22 | Mitsui Petrochem Ind Ltd | Production of diphenylamine compound |
| EP0560157A1 (en) * | 1992-03-12 | 1993-09-15 | Bayer Ag | Fixed bed reactors with short catalyst bed in the direction of flow |
| US5648538A (en) * | 1994-06-29 | 1997-07-15 | Fushun Research Institute Of Petroleum And Petrochemicals | Process for preparing diarylamines from arylamines |
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| CN2892853Y (en) * | 2006-02-13 | 2007-04-25 | 南通新邦化工有限公司 | Apparatus for whole continuous producing diphenylamine from aniline |
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2014
- 2014-11-19 CN CN201410661655.3A patent/CN104478738B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS6051152A (en) * | 1983-08-31 | 1985-03-22 | Mitsui Petrochem Ind Ltd | Production of diphenylamine compound |
| EP0560157A1 (en) * | 1992-03-12 | 1993-09-15 | Bayer Ag | Fixed bed reactors with short catalyst bed in the direction of flow |
| US5648538A (en) * | 1994-06-29 | 1997-07-15 | Fushun Research Institute Of Petroleum And Petrochemicals | Process for preparing diarylamines from arylamines |
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Non-Patent Citations (2)
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105384683A (en) * | 2015-12-17 | 2016-03-09 | 南通新邦化工科技有限公司 | 2-Methyl-pyridine and 4-methylpyridine production method |
| CN105384683B (en) * | 2015-12-17 | 2018-04-10 | 南通新邦化工科技有限公司 | A kind of 2 picoline, the production method of 4 picolines |
| CN107935862A (en) * | 2017-11-27 | 2018-04-20 | 南通新邦化工科技有限公司 | A kind of method of aniline continuous synthesizing diphenylamine |
| CN114805086A (en) * | 2022-05-16 | 2022-07-29 | 杰超橡塑南通有限公司 | Process and system for producing diphenylamine by adopting aniline continuous condensation method |
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