CN2892853Y - Apparatus for whole continuous producing diphenylamine from aniline - Google Patents
Apparatus for whole continuous producing diphenylamine from aniline Download PDFInfo
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- CN2892853Y CN2892853Y CN 200620069259 CN200620069259U CN2892853Y CN 2892853 Y CN2892853 Y CN 2892853Y CN 200620069259 CN200620069259 CN 200620069259 CN 200620069259 U CN200620069259 U CN 200620069259U CN 2892853 Y CN2892853 Y CN 2892853Y
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Abstract
The utility model discloses a full continuous aniline producing diphenylamine device, which comprises a raw material elevated tank, a mixer, a feeding pump, a hydrogen pack, a heat exchanger, a first heater, a first reactor, a second heater, a second reactor, a hydrogen-ammonia separator, a front run distillation tower, a condenser at top of the tower, a condensing combination at top of the tower, a front run recovery groove, an aniline distillation tower, a tower reactor reboiler, a middle run distillation tower, a middle run recovery groove, a diphenylamine distillation tower, a recombination partial recovery groove, a decolorizing device, a finished product storage tank and a mechanical vacuum pump. The utility model makes the production used catalyst have good performance and long service life, and little side impurities are produced in the production operation. The utility model has low energy consumption, superior quality product and less environmental impact.
Description
Technical field:
The utility model relates to a kind of manufacturing installation, belong to chemical industry equipment and device technique field with aniline raw material production pentanoic product.
Background technology:
The device of the Aniline Production pentanoic of prior art is to adopt no hydrogen or high-speed to face hydrogen or little nitrogen reaction unit that adds, and the subsequent fine distillation unit is configurations such as common still formula vaporizer (reboiler) and jet of water vacuum apparatus, and end is not provided with the product appearance treatment facility.Then exist catalyst performance decay very fast or production cost is higher, the by-product superpolymer is more, the product appearance quality is not good enough, water body environment had in the production process defective such as certain pollution.
Summary of the invention:
The utility model purpose be to provide a kind of make production with catalyst performance bring into play, the life-span is long, by-product impurity is few in the production run, the energy consumption material consumption is low, product quality is excellent, the full device of Aniline Production pentanoic continuously that environmental influence is little.
Technical solution of the present utility model is:
A kind of full device of Aniline Production pentanoic continuously, it is characterized in that: raw material header tank outlet termination mixing tank entrance end, mixer outlet termination fresh feed pump entrance end, fresh feed pump exit end and the merging of hydrogen bag exit end are connected to the cold journey entrance end of interchanger, the cold journey outlet of interchanger termination primary heater entrance end, the primary heater outlet termination first Reactor inlet end, the entrance end of the first reactor outlet termination secondary heater, the secondary heater outlet termination second Reactor inlet end, the second reactor outlet termination exchanger heat journey entrance end, exchanger heat journey outlet termination hydrogen ammonia separator entrance end, the gaseous phase outlet of hydrogen ammonia separator is connected to the recovery system outside this device, before being connected to, heats up in a steamer the liquid phase exit end of hydrogen ammonia separator the entrance end of rectifying tower, before heat up in a steamer the hot journey entrance end of the gaseous phase outlet termination overhead condenser of rectifying tower, the gaseous phase outlet of overhead condenser is connected to emptying or the rough vacuum system outside this device, the hot journey liquid phase exit end of overhead condenser divides two-way, one the tunnel heats up in a steamer the backflow entrance end of rectifying tower before being connected to, one the tunnel heats up in a steamer the accumulator tank entrance end before connecing, before heat up in a steamer the entrance end of the still liquid outlet termination aniline distillation tower of rectifying tower, the hot journey entrance end of the gaseous phase outlet termination overhead condenser group of aniline distillation tower, the gaseous phase outlet of overhead condenser group is connected to the entrance end of vacuum buffer tank, the hot journey liquid phase exit end of overhead condenser group divides two the tunnel, one the tunnel is connected to the backflow entrance end of aniline distillation tower, one the tunnel is connected to the entrance end of mixing tank, aniline distillation tower still liquid exit end divides two the tunnel, the cold journey entrance end of one road tower still reboiler, the hot journey outlet termination aniline distillation tower gas phase entrance end of tower still reboiler, during connecing, another road heats up in a steamer the rectifying tower entrance end, in heat up in a steamer the hot journey entrance end of the gaseous phase outlet termination overhead condenser group of rectifying tower, the gaseous phase outlet of overhead condenser group is connected to the surge tank entrance end, the hot journey liquid phase exit end of overhead condenser group divides two the tunnel, one the tunnel heats up in a steamer the backflow entrance end of rectifying tower in being connected to, one the tunnel heats up in a steamer the accumulator tank entrance end in connecing, in heat up in a steamer rectifying tower still liquid exit end divide two the tunnel, one the tunnel is connected to the cold journey entrance end of tower still reboiler, heat up in a steamer rectifying tower gas phase entrance end in the hot journey outlet termination of tower still reboiler, another road connects pentanoic rectifying tower entrance end, the hot journey entrance end of the gaseous phase outlet termination overhead condenser group of pentanoic rectifying tower, the gaseous phase outlet of overhead condenser group is connected to the vacuum buffer tank entrance end, the vacuum buffer tank exit end connects mechanical type vacuum pump entrance end, the hot journey liquid phase exit end of overhead condenser group divides two the tunnel, one the tunnel is connected to the backflow entrance end of pentanoic rectifying tower, one the tunnel is connected to the decolorizer entrance end, the decolorizer exit end is connected into product storage tank entrance end, pentanoic rectifying tower bottoms exit end divides two the tunnel, one the tunnel connects the cold journey entrance end of tower still reboiler, the hot journey outlet termination pentanoic rectifying tower gas phase entrance end of tower still reboiler, another road connects the heavy constituent accumulator tank.
Tower still reboiler in the device adopts the film-type evaporator structural shape.
The utility model mainly contains following characteristics: (1), device have been realized the full successive processes of successive reaction, continuous rectification, make that production capacity is bigger, the power consumption feed consumption still less.(2), in device, set up intermittently injection device (hydrogen bag) of micro-hydrogen, suppress the coking of catalyzer duct with this hydrogen and tie charcoal speed, catalyst performance is bringd into play, and increases the service life.(3), device inherent by the hydrogen ammonia separator to before heat up in a steamer rectifying tower, by preceding heating up in a steamer the rectifying tower still to aniline distillation tower charging flow process, saved equipment such as medial launder, line pump, middle heating, simplified operation, saved investment and process cost.(4), rectifying tower still reboiler adopts the film-type evaporator structure, make that material is shorter in the high-temperature zone residence time, by-product impurity still less.(5), set up the product decoloring equipment, at the device end make the product look see whiter, quality is more excellent.(6), select for use the mechanical type vacuum pump to make negative pressure, than water-jet pump, water-ring vacuum pump, stopped the pollution to water body environment such as the aniline that may exist, easily make this partial material obtain efficient recovery again.
Description of drawings:
The utility model is described in further detail below in conjunction with drawings and Examples.
Accompanying drawing is the configuration diagram of an embodiment of the utility model.
Among the figure 1. be the raw material header tank, 2. be mixing tank, 3. be fresh feed pump, 4. be the hydrogen bag, 5. be interchanger, 6. be primary heater, 7. be first reactor, 8. be secondary heater, 9. be second reactor, 10. be heat up in a steamer rectifying tower before hydrogen ammonia separator, are, is an overhead condenser, ,
Be the overhead condenser group, heat up in a steamer accumulator tank before the , is an aniline distillation tower, and
Be the membrane type reboiler,
Heat up in a steamer in being rectifying tower,
Heat up in a steamer in being accumulator tank,
Be the pentanoic rectifying tower,
Be the heavy constituent accumulator tank,
Be decolorizer,
Be the finished product storage tank,
Be vacuum buffer tank,
It is the mechanical type vacuum pump.
Embodiment:
A kind of full device of Aniline Production pentanoic continuously, raw material header tank (1) outlet termination mixing tank (2) entrance end, mixing tank (2) exit end connects fresh feed pump (3) entrance end, fresh feed pump (3) exit end and the merging of hydrogen bag (4) exit end are connected to the cold journey entrance end of interchanger (5), the cold journey outlet of interchanger (5) termination primary heater (6) entrance end, primary heater (6) outlet termination first reactor (7) entrance end, the entrance end of first reactor (7) outlet termination secondary heater (8), secondary heater (8) outlet termination second reactor (9) entrance end, the hot journey entrance end of the second reactor outlet termination interchanger (5), the hot journey outlet of interchanger (5) termination hydrogen ammonia separator (10) entrance end, the gaseous phase outlet of hydrogen ammonia separator (10) is connected to the recovery system outside this device, before being connected to, heats up in a steamer the liquid phase exit end of hydrogen ammonia separator (10) entrance end of rectifying tower (11), before heat up in a steamer the hot journey entrance end of the gaseous phase outlet termination overhead condenser (12) of rectifying tower (11), the gaseous phase outlet of overhead condenser (12) is connected to emptying or the rough vacuum system outside this device, the hot journey liquid phase exit end of overhead condenser (12) divides two-way, one the tunnel heats up in a steamer the backflow entrance end of rectifying tower (11) before being connected to, one the tunnel heats up in a steamer accumulator tank (13) entrance end before connecing, before heat up in a steamer the entrance end of the still liquid outlet termination aniline distillation tower (14) of rectifying tower (11), the hot journey entrance end of the gaseous phase outlet termination overhead condenser group (15) of aniline distillation tower (14), the gaseous phase outlet of overhead condenser group (15) is connected to the entrance end of vacuum buffer tank (25), the hot journey liquid phase exit end of overhead condenser group (15) divides two the tunnel, one the tunnel is connected to the backflow entrance end of aniline distillation tower (14), one the tunnel is connected to the entrance end of mixing tank (2), aniline distillation tower (14) still liquid exit end divides two the tunnel, the cold journey entrance end of one road tower still reboiler (16), hot journey outlet termination aniline distillation tower (14) the gas phase entrance end of tower still reboiler (16), during connecing, another road heats up in a steamer rectifying tower (17) entrance end, in heat up in a steamer the hot journey entrance end of the gaseous phase outlet termination overhead condenser group (18) of rectifying tower (17), the gaseous phase outlet of overhead condenser group (18) is connected to surge tank (25) entrance end, the hot journey liquid phase exit end of overhead condenser group (18) divides two the tunnel, one the tunnel heats up in a steamer the backflow entrance end of rectifying tower (17) in being connected to, one the tunnel heats up in a steamer accumulator tank (19) entrance end in connecing, in heat up in a steamer rectifying tower (17) still liquid exit end divide two the tunnel, one the tunnel is connected to the cold journey entrance end of tower still reboiler (20), heat up in a steamer rectifying tower (17) gas phase entrance end in the hot journey outlet termination of tower still reboiler (20), another road connects pentanoic rectifying tower (21) entrance end, the hot journey entrance end of the gaseous phase outlet termination overhead condenser group (24) of pentanoic rectifying tower, the gaseous phase outlet of overhead condenser group (24) is connected to vacuum buffer tank (25) entrance end, vacuum buffer tank (25) exit end connects mechanical type vacuum pump (26) entrance end, the hot journey liquid phase exit end of overhead condenser group (24) divides two the tunnel, one the tunnel is connected to the backflow entrance end of pentanoic rectifying tower (21), one the tunnel is connected to decolorizer (27) entrance end, decolorizer (27) exit end is connected into product storage tank (28) entrance end, pentanoic rectifying tower (21) still liquid exit end divides two the tunnel, one the tunnel connects the cold journey entrance end of tower still reboiler (22), hot journey outlet termination pentanoic rectifying tower (21) the gas phase entrance end of tower still reboiler (22), another road connects heavy constituent accumulator tank (23).The film-type evaporator structural shape is adopted in tower still reboiler (16) in the device, (20), (22).
Working process of the present utility model is:
After raw material aniline is squeezed into header tank (1), continuously mending mixing tank (2) separates with the aniline distillation tower top enter fresh feed pump (3) after the hot aniline of returning mixes in (2), boost to about 2.4Mpa, again and hydrogen bag (4) send here between mend hydrogen and enter in the lump after interchanger (5) heat exchange heats up, be heated to the required temperature of reaction (325～328 ℃) of catalyzer (Nankai University's manufacturings) through primary heater (6) and enter bottom the reactor (7).At this fixed bed catalyst, after generating the pentanoic finished fluid, part draws by (7) top, mend temperature through secondary heater (8) second-heating and enter second reactor (9) bottom again, after this further reacts the pentanoic finished fluid that generates high density, draw, get back to interchanger (5) and be cooled to below 160 ℃ by (9) top.To 0.15Mpa, enter hydrogen ammonia separator (10) through expenditure and pressure, separate the hydrogen ammonia of sucking-off and draw recovery system by the top: liquid phase (reaction solution) is heated up in a steamer rectifying tower (11) before then drawing and sending bottom hydrogen ammonia separator (10), steam front-end volatiles by cat head and reflux through overhead condenser (12) rear section, part is gathered to before heating up in a steamer accumulator tank (13); Draw liquid and send aniline distillation tower (14) again by preceding heating up in a steamer rectifying tower (11) tower still, by cat head steam that aniline refluxes through overhead condenser group (15) rear section, part adopts and delivers to mixing tank (2) and remove secondary reaction, heat up in a steamer rectifying tower (17) in sending again by aniline distillation tower (14) tower still extraction liquid, by cat head steam in the high density cut through overhead condenser group (18) rear section reflux, part gather in heat up in a steamer accumulator tank (19); By in heat up in a steamer rectifying tower (17) tower still extraction liquid and send pentanoic rectifying tower (21) again, the pentanoic that is steamed by cat head refluxes through overhead condenser group (24) rear section, part is adopted and delivered to decolorizer (27), after this adjusts and reduce pentanoic colourity, lead to finished product storage tank (28) by its bottom, the whole unlap of this product is sold.Be collected into heavy constituent accumulator tank (25) by pentanoic rectifying tower (21) tower still extraction heavy constituent.For making rectifying tower (14), (17), (21) be in negative pressure of vacuum operation, draw vacuum to vacuum buffer tank (25) by corresponding overhead condenser group (15), (18), (24) top, take out the separation of negative back through the mechanical type vacuum pump and draw sky.
Claims (2)
1, a kind of full device of Aniline Production pentanoic continuously, it is characterized in that: raw material header tank (1) outlet termination mixing tank (2) entrance end, mixing tank (2) exit end connects fresh feed pump (3) entrance end, fresh feed pump (3) exit end and the merging of hydrogen bag (4) exit end are connected to the cold journey entrance end of interchanger (5), the cold journey outlet of interchanger (5) termination primary heater (6) entrance end, primary heater (6) outlet termination first reactor (7) entrance end, the entrance end of first reactor (7) outlet termination secondary heater (8), secondary heater (8) outlet termination second reactor (9) entrance end, the hot journey entrance end of the second reactor outlet termination interchanger (5), the hot journey outlet of interchanger (5) termination hydrogen ammonia separator (10) entrance end, the gaseous phase outlet of hydrogen ammonia separator (10) is connected to the recovery system outside this device, before being connected to, heats up in a steamer the liquid phase exit end of hydrogen ammonia separator (10) entrance end of rectifying tower (11), before heat up in a steamer the hot journey entrance end of the gaseous phase outlet termination overhead condenser (12) of rectifying tower (11), the gaseous phase outlet of overhead condenser (12) is connected to emptying or the rough vacuum system outside this device, the hot journey liquid phase exit end of overhead condenser (12) divides two-way, one the tunnel heats up in a steamer the backflow entrance end of rectifying tower (11) before being connected to, one the tunnel heats up in a steamer accumulator tank (13) entrance end before connecing, before heat up in a steamer the entrance end of the still liquid outlet termination aniline distillation tower (14) of rectifying tower (11), the hot journey entrance end of the gaseous phase outlet termination overhead condenser group (15) of aniline distillation tower (14), the gaseous phase outlet of overhead condenser group (15) is connected to the entrance end of vacuum buffer tank (25), the hot journey liquid phase exit end of overhead condenser group (15) divides two the tunnel, one the tunnel is connected to the backflow entrance end of aniline distillation tower (14), one the tunnel is connected to the entrance end of mixing tank (2), aniline distillation tower (14) still liquid exit end divides two the tunnel, the cold journey entrance end of one road tower still reboiler (16), hot journey outlet termination aniline distillation tower (14) the gas phase entrance end of tower still reboiler (16), during connecing, another road heats up in a steamer rectifying tower (17) entrance end, in heat up in a steamer the hot journey entrance end of the gaseous phase outlet termination overhead condenser group (18) of rectifying tower (17), the gaseous phase outlet of overhead condenser group (18) is connected to surge tank (25) entrance end, the hot journey liquid phase exit end of overhead condenser group (18) divides two the tunnel, one the tunnel heats up in a steamer the backflow entrance end of rectifying tower (17) in being connected to, one the tunnel heats up in a steamer accumulator tank (19) entrance end in connecing, in heat up in a steamer rectifying tower (17) still liquid exit end divide two the tunnel, one the tunnel is connected to the cold journey entrance end of tower still reboiler (20), heat up in a steamer rectifying tower (17) gas phase entrance end in the hot journey outlet termination of tower still reboiler (20), another road connects pentanoic rectifying tower (21) entrance end, the hot journey entrance end of the gaseous phase outlet termination overhead condenser group (24) of pentanoic rectifying tower, the gaseous phase outlet of overhead condenser group (24) is connected to vacuum buffer tank (25) entrance end, vacuum buffer tank (25) exit end connects mechanical type vacuum pump (26) entrance end, the hot journey liquid phase exit end of overhead condenser group (24) divides two the tunnel, one the tunnel is connected to the backflow entrance end of pentanoic rectifying tower (21), one the tunnel is connected to decolorizer (27) entrance end, decolorizer (27) exit end is connected into product storage tank (28) entrance end, pentanoic rectifying tower (21) still liquid exit end divides two the tunnel, one the tunnel connects the cold journey entrance end of tower still reboiler (22), hot journey outlet termination pentanoic rectifying tower (21) the gas phase entrance end of tower still reboiler (22), another road connects heavy constituent accumulator tank (23).
2, the full device of Aniline Production pentanoic continuously according to claim 1, it is characterized in that: the film-type evaporator structural shape is adopted in the tower still reboiler (16) in the device, (20), (22).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200620069259 CN2892853Y (en) | 2006-02-13 | 2006-02-13 | Apparatus for whole continuous producing diphenylamine from aniline |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200620069259 CN2892853Y (en) | 2006-02-13 | 2006-02-13 | Apparatus for whole continuous producing diphenylamine from aniline |
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| Publication Number | Publication Date |
|---|---|
| CN2892853Y true CN2892853Y (en) | 2007-04-25 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 200620069259 Expired - Fee Related CN2892853Y (en) | 2006-02-13 | 2006-02-13 | Apparatus for whole continuous producing diphenylamine from aniline |
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| Country | Link |
|---|---|
| CN (1) | CN2892853Y (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104478738A (en) * | 2014-11-19 | 2015-04-01 | 南通新邦化工科技有限公司 | Reaction method for continuously synthesizing diphenylamine from aniline |
-
2006
- 2006-02-13 CN CN 200620069259 patent/CN2892853Y/en not_active Expired - Fee Related
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104478738A (en) * | 2014-11-19 | 2015-04-01 | 南通新邦化工科技有限公司 | Reaction method for continuously synthesizing diphenylamine from aniline |
| CN104478738B (en) * | 2014-11-19 | 2017-01-25 | 南通新邦化工科技有限公司 | Reaction method for continuously synthesizing diphenylamine from aniline |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C56 | Change in the name or address of the patentee |
Owner name: NANTONG XINBANG CHEMICAL TECHNOLOGY CO., LTD. Free format text: FORMER NAME: XINGANG CHEMICAL CO., LTD., NANTONG |
|
| CP03 | Change of name, title or address |
Address after: 226500 No. 38, Binjiang Road, Changjiang Town, Jiangsu, Rugao Patentee after: Nantong Xinbang Chemical Co., Ltd. Address before: 226500 Rugao Port Economic Development Zone, Jiangsu, Rugao Patentee before: Xingang Chemical Co., Ltd., Nantong |
|
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20070425 Termination date: 20150213 |
|
| EXPY | Termination of patent right or utility model |