CN1363550A - Process for synthesizing biphenylamine from phenylamine by adding nitrogen gas to reactor - Google Patents
Process for synthesizing biphenylamine from phenylamine by adding nitrogen gas to reactor Download PDFInfo
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- CN1363550A CN1363550A CN 02112535 CN02112535A CN1363550A CN 1363550 A CN1363550 A CN 1363550A CN 02112535 CN02112535 CN 02112535 CN 02112535 A CN02112535 A CN 02112535A CN 1363550 A CN1363550 A CN 1363550A
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- aniline
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Abstract
A process for synthesizing biphenylamine from phenylamine includes such steps as metering phenylamine, heating it so 330-370 deg.C, reacting with catalyst and nitrogen gas at 320-360 deg.C, 1.6-2.5 MPa and 0.15-0.2 /h of space speed, cooling by heat exchange with raw material, gas-liquid separation to obtain intermediate liquid, heating, feeding in phenylamine rectifying tower, and purifying in biphenylamine rectifying tower. Its advantages include simple equipment, low cost, and high safety.
Description
Technical field:
The present invention relates to be a kind of with aniline as raw material synthetic pentanoic method, prepared product is used for synthetic rubber anti-aging agent, dyestuff intermediate and important stablizer etc.Belong to the fine chemical technology field.
Background technology:
Prior art such as CN1186802A, denomination of invention is a continous diphenylemine synthesizing industrial system by using phenylamine as material.Its structure includes reactor and outlet is connected in series gas-liquid separator successively, the absorption device, inhale the nitrogen device, air water separator, dry cleaner was set before reactor, this dry cleaner inlet connects from syngas for synthetic ammonia (being refinery gas), the clean gas outlet of clean cleaner is connected to reactor, the gas phase import, the 1 grade of import that is connected to synthetic ammonia installation high-pressure unit operation is returned in the stripping gas outlet, Detoxicating device is set after air water separator, this Detoxicating device inlet connects from air water separator works off one's feeling vent one's spleen, V level (or the IV level) import that is connected to synthetic ammonia installation high-pressure unit operation is returned in the Detoxicating device air outlet, it designs by synthetic ammonia installation, that is to say, it is the hydrogen consumption that utilizes in the technical process of synthetic ammonia installation minimizing syntehsizing diphenylamine, reaches the purpose that reduces cost.Yet because it needs synthetic ammonia installation, and not thorough to reducing hydrogen consumption yet, so its cost is still very high.
Summary of the invention:
The object of the invention is the defective at above-mentioned existence, proposes a kind of cancellation synthetic ammonia installation, fundamentally reaches the aniline syntehsizing diphenylamine method that adds nitrogen in reactor that reduces cost, the preparation pentanoic.Technical solution of the present invention: its processing step is followed successively by: the metering of (1) aniline, the aniline raw material is measured and sends into the aniline well heater by aniline scale tank, volume pump; (2) aniline heating, the aniline raw material after the metering is heated to 330-370 ℃; (3) reaction, the raw material aniline after heating is located in the reactor that catalyzer is housed, and carries out chemical reaction, lowers the temperature by the raw produce interchanger then, makes temperature below 150 ℃; (4) gas-liquid separation, decompression afterreaction intermediate liquid carries out gas-liquid separation in gas-liquid separator; (5) intermediate liquid heating through the liquid phase behind the gas-liquid separator, is carried out heat temperature raising by medial launder, fresh feed pump, well heater; (6) separation and purification, enter aniline distillation tower to the intermediate liquid behind the heat temperature raising, liquid phase wherein enters the pentanoic rectifying tower and is purified to the pentanoic finished product, it is characterized in that processing step (3) reaction, in reactor, add nitrogen, pressure in the reactor is 1.6-2.5MPa, and aniline is 0.15-0.2/h with the air speed ratio of catalyzer, and temperature is 320-360 ℃.Advantage of the present invention: compared with prior art, owing to cancelled synthetic ammonia installation, number of devices is reduced, greatly reduce production cost, the condition operation at no hydrogen has reduced anti-hazard classification, has improved safety performance.
Accompanying drawing is a process flow sheet of the present invention.
Among the figure 1 is aniline metering, the 2nd, aniline heating, the 3rd, reaction, the 4th, gas-liquid separation, the 5th, intermediate liquid heating, the 6th, separation and purification, the 7th, finished product packing.
Embodiment
Aniline is by aniline scale tank volume (v=6m
3), volume pump (ram pump), the metering back is with the 2t/h flow, through nitrogen buffering gas bag (P=2.0MPa, V=0.3m
3) after enter raw produce interchanger preheating in the aniline heating 2, be heated to 340 ℃ through electric heater again and enter in the reactor, add nitrogen in the reactor, the pressure in the reactor is 2MPa, adds catalyzer 10m in the reactor
3Be 0.2/h with the air speed ratio of aniline, temperature is 340 ℃.The model of catalyzer is selected FD-20, it is to be produced by Fushun petrochemical industry research institute, reactor outlet material is reduced to below 150 ℃ through the raw produce interchanger, after be decompressed to below the 0.1MPa, enter the high-temperature separator in the gas-liquid separator 4, gas phase in the high-temperature separator is cooled to below 40 ℃ through condenser and enters low-temperature separator, the liquid phase of high-temperature separator and low-temperature separator enters the middle liquid bath of reaction in the intermediate liquid heating 5, through fresh feed pump (process pump), heat exchanger, well heater (heat interchanging area S=30m
2) be heated to 184 ℃, enter aniline distillation tower and separate, cat head aniline is cooled to below 100 ℃ through heat exchanger, condenser, partial reflux, the aniline scale tank that part is returned in the aniline metering 1 is recycled.The material that the tower still is 300 ℃ is purified for a collection of pentanoic rectifying tower that enters for per 5 tons, earlier light component is boiled off, and can steam finished product pentanoic, finished product packing then.
Claims (1)
1, add the aniline syntehsizing diphenylamine method of nitrogen in the reactor, its processing step is followed successively by: the metering of (1) aniline, the aniline raw material is measured and sends into the aniline well heater by aniline scale tank, volume pump; (2) aniline heating, the aniline raw material after the metering is heated to 330-370 ℃; (3) reaction, the raw material aniline after heating is located in the reactor that catalyzer is housed, and carries out chemical reaction, lowers the temperature by the raw produce interchanger then, makes temperature below 150 ℃; (4) gas-liquid separation, decompression afterreaction intermediate liquid carries out gas-liquid separation in gas-liquid separator; (5) intermediate liquid heating through the liquid phase behind the gas-liquid separator, is carried out heat temperature raising by medial launder, fresh feed pump, well heater; (6) separation and purification, enter aniline distillation tower to the intermediate liquid behind the heat temperature raising, liquid phase wherein enters the pentanoic rectifying tower and is purified to the pentanoic finished product, it is characterized in that processing step (3) reaction, in reactor, add nitrogen, pressure in the reactor is 1.6-2.5MPa, and aniline is 0.15-0.2/h with the air speed ratio of catalyzer, and temperature is 320-360 ℃.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB02112535XA CN1169779C (en) | 2002-01-14 | 2002-01-14 | Process for synthesizing biphenylamine from phenylamine by adding nitrogen gas to reactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB02112535XA CN1169779C (en) | 2002-01-14 | 2002-01-14 | Process for synthesizing biphenylamine from phenylamine by adding nitrogen gas to reactor |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1363550A true CN1363550A (en) | 2002-08-14 |
| CN1169779C CN1169779C (en) | 2004-10-06 |
Family
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB02112535XA Expired - Lifetime CN1169779C (en) | 2002-01-14 | 2002-01-14 | Process for synthesizing biphenylamine from phenylamine by adding nitrogen gas to reactor |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1169779C (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102250651A (en) * | 2011-06-17 | 2011-11-23 | 西安聚德新能源技术有限公司 | Production process and device of large-proportion methanol gasoline for molecular sieve catalytic synthesis vehicle |
| 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 |
-
2002
- 2002-01-14 CN CNB02112535XA patent/CN1169779C/en not_active Expired - Lifetime
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102250651A (en) * | 2011-06-17 | 2011-11-23 | 西安聚德新能源技术有限公司 | Production process and device of large-proportion methanol gasoline for molecular sieve catalytic synthesis vehicle |
| CN102250651B (en) * | 2011-06-17 | 2014-07-09 | 西安聚德新能源技术有限公司 | Production process and device of large-proportion methanol gasoline for molecular sieve catalytic synthesis vehicle |
| 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 |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1169779C (en) | 2004-10-06 |
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|---|---|---|---|
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
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| C14 | Grant of patent or utility model | ||
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| EE01 | Entry into force of recordation of patent licensing contract |
Assignee: Jiangsu Feiya Chemical Industry Co., Ltd. Assignor: Cao Hongsheng Contract fulfillment period: 2009.2.8 to 2014.2.7 Contract record no.: 2009320000139 Denomination of invention: Process for synthesizing biphenylamine from phenylamine by adding nitrogen gas to reactor Granted publication date: 20041006 License type: Exclusive license Record date: 20090225 |
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| LIC | Patent licence contract for exploitation submitted for record |
Free format text: EXCLUSIVE LICENSE; TIME LIMIT OF IMPLEMENTING CONTACT: 2009.2.8 TO 2014.2.7; CHANGE OF CONTRACT Name of requester: JIANGSU FEIYA CHEMISTRY INDUSTRY CO.,LTD. Effective date: 20090225 |
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| CX01 | Expiry of patent term | ||
| CX01 | Expiry of patent term |
Granted publication date: 20041006 |