CN202953963U - Device for preparing dicyclopentadiene by thermal dimerisation - Google Patents
Device for preparing dicyclopentadiene by thermal dimerisation Download PDFInfo
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- CN202953963U CN202953963U CN 201220648540 CN201220648540U CN202953963U CN 202953963 U CN202953963 U CN 202953963U CN 201220648540 CN201220648540 CN 201220648540 CN 201220648540 U CN201220648540 U CN 201220648540U CN 202953963 U CN202953963 U CN 202953963U
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- dimerization
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Abstract
The utility model relates to a device for preparing dicyclopentadiene by thermal dimerisation, belonging to the field of chemical equipment. The device comprises a dimerisation reaction buffer tank (2) and a dimerisation reaction generation device, wherein the dimerisation reaction buffer tank (2) and the dimerisation reaction generation device are connected through a pipeline. The device is characterized in that a constant temperature heat exchanger (4) is connected in series to the pipeline between the dimerisation reaction buffer tank (2) and the dimerisation reaction generation device. By using the device disclosed by the utility model, IP (isoprene) polymerization during the dimerisation reaction process of CPD (cyclopentadiene) can be reduced, the reversible depolymerization of DCPD (dicyclopentadiene) can be prevented, and the efficiency and the yield of polymerization of the cyclopentadiene can be increased.
Description
Technical field
A kind of hot dimerization is produced the device of dicyclopentadiene, belongs to the chemical industry equipment field.Be specifically related to a kind of device that is prepared dicyclopentadiene by the cyclopentadiene dimerization.
Background technology
The existing dicyclopentadiene production technology of China obviously falls behind, and serialization, mass-producing and product seriation are the bottlenecks that dicyclopentadiene is produced.For this reason, the new installation of Development and Production dicyclopentadiene, new technology are matters of utmost importance.
Because component in cracking c_5 is many, cause hot dimerization reaction process very complicated, cyclopentadiene (CPD) is easy to dimerization and generates dicyclopentadiene (DCPD) on the one hand, also can generate dipolymer with isoprene (IP) copolymerization simultaneously, reduces productive rate and causes damage; On the other hand, the dimerization of CPD and the depolymerization of DCPD are reversible, and the control of processing condition directly affects the yield of DCPD.Therefore the impact of the technique of the hot dimerization of CPD on dicyclopentadiene yield, isoprene rate of loss in C 5 fraction, directly have influence on the economic benefit that C5 fully utilizes.
Summary of the invention
The technical problems to be solved in the utility model is: overcome the deficiencies in the prior art, a kind of raising CPD dimerization reaction yield is provided, a kind of hot dimerization that reduces the IP dimerization is produced the device of dicyclopentadiene.
The utility model solves the technical scheme that its technical problem adopts: this kind of hot dimerization is produced the device of dicyclopentadiene, comprise dimerization reaction surge tank, hot dimerization reaction generating unit, between dimerization reaction surge tank and hot dimerization reaction generating unit, pipeline is connected, and it is characterized in that: on the pipeline between dimerization reaction surge tank and hot dimerization reaction generating unit, be in series with the constant temperature interchanger.
Between described dimerization reaction surge tank and constant temperature interchanger, flow control valve is installed on connecting pipeline.Flow control valve plays inlet amount and pressure-controlling effect.
Described constant temperature interchanger is provided with the turnover pipeline of secondary reduced steam and circulating condensing water.With the heating of secondary reduced steam, use the circulating condensing water for cooling, effectively control the first hot dipolymer reactor and the second hot dimerization reaction actuator temperature.Described constant temperature interchanger adopts shell and tube heat exchanger, comprises circulating condensing water and secondary reduced steam, and hot dimerization charging is played to the temperature control action kou.
Concrete, described hot dimerization reaction generating unit comprises the first hot dipolymer reactor, the second hot dipolymer reactor, de-isoprene tower and the 3rd hot dipolymer reactor of connecting by pipeline successively.
Preferably, described hot dimerization reaction generating unit comprises the first hot dipolymer reactor, the second hot dipolymer reactor, de-isoprene tower and the 3rd hot dipolymer reactor, the described first hot dipolymer reactor, de-isoprene tower and the 3rd hot dipolymer reactor are connected by pipeline successively, the described second hot dipolymer reactor is in parallel with the first hot dipolymer reactor, and directly by pipeline, connects the constant temperature interchanger.
Be in series with de-isoprene tower feed preheater on the front pipeline of described de-isoprene tower, before the 3rd hot dipolymer reactor, on pipeline, be in series with the 3rd hot dipolymer reactor feed preheater.
The described first hot dipolymer reactor, the second hot dipolymer reactor are provided with the pipeline that returns to the dimerization reaction surge tank, on this return pipeline, pressure regulator valve are installed.Pressure regulator valve plays the effect of decompression to dipolymer reactor.
Before de-isoprene tower, cyclopentadiene is controlled incomplete polymerization, after removing isoprene, by the complete polymerization of the 3rd hot dipolymer reactor.
The dimerization reaction surge tank plays the component stabilization to the charging of hot dimerization reaction.
The utility model can in the situation that the residence time certain, utilize the constant temperature interchanger that the temperature of raw material reaction thing is controlled at after optimal reaction temperature and enters hot dimerization reaction generating unit again and react, realize insufficient conversion in early stage of CPD by the control of temperature, avoid isoprene polymerization, after de-isoprene, fully make again the CPD polymerization.
Compared with prior art, the beneficial effect that a kind of hot dimerization of the utility model is produced the device realization of dicyclopentadiene is: use of the present utility model can reduce the IP polymerization in the hot dimerization reaction process of CPD, prevent the reversible depolymerization of DCPD, increase efficiency and the yield of cyclopentadiene polymerization, increase the overall economic efficiency of carbon five comprehensive utilizations.The stabilising effect in hot dimerization reaction system, the control of temperature played, make hot dipolymer reactor feed composition stable, can heat and can lower the temperature, feed rate valve and pressure regulator valve make in the situation of hot dipolymer reactor pressure-stabilisation, have guaranteed the well-defined reaction temp of dipolymer reactor reaction, and the CPD transformation efficiency is effectively controlled, fully polymerization again after removing isoprene, reduce the polymerization of its isoprene, improved the yield of various products in carbon five comprehensive utilizations, maximum economic benefit.
The accompanying drawing explanation
Fig. 1 is the device schematic diagram that a kind of hot dimerization is produced dicyclopentadiene.
Wherein: 1, dimerization reaction surge tank fresh feed pump 2, dimerization reaction surge tank 3, constant temperature interchanger fresh feed pump 4, the hot dipolymer reactor 7 of the hot dipolymer reactor 6, second of constant temperature interchanger 5, first, de-isoprene tower feed preheater 8, de-isoprene tower 9, the hot dipolymer reactor feed preheater 11 of the 3rd hot dipolymer reactor fresh feed pump the 10, the 3rd, the 3rd hot dipolymer reactor.
Embodiment
Fig. 1 is the preferred forms that a kind of hot dimerization of the utility model is produced the device of dicyclopentadiene, below in conjunction with 1 pair of the utility model of accompanying drawing, is described further.
With reference to accompanying drawing 1: a kind of hot dimerization of the present embodiment is produced the device of dicyclopentadiene, comprises dimerization reaction surge tank fresh feed pump 1, dimerization reaction surge tank 2, constant temperature interchanger fresh feed pump 3, the hot dipolymer reactor 6 of the hot dipolymer reactor 5, second of constant temperature interchanger 4, first, de-isoprene tower feed preheater 7, de-isoprene tower 8, hot dipolymer reactor feed preheater the 10, the 3rd hot dipolymer reactor 11 of the 3rd hot dipolymer reactor fresh feed pump the 9, the 3rd.The opening for feed of dimerization reaction surge tank 2 connects the discharge port of dimerization reaction surge tank fresh feed pump 1 by pipeline, the discharge port of dimerization reaction surge tank 2 connects constant temperature interchanger 4 by pipeline, constant temperature interchanger 4 is connecting the opening for feed of the first hot dipolymer reactor 5 by pipeline, the discharge port of the first hot dipolymer reactor 5 connects the opening for feed of the second hot dipolymer reactor 6 by pipeline, the discharge port of the second hot dipolymer reactor 6 connects the opening for feed of de-isoprene tower feed preheater 7 by pipeline, the discharge port of de-isoprene tower feed preheater 7 connects the opening for feed of de-isoprene tower 8 by pipeline, the discharge port of de-isoprene tower 8 connects the 3rd hot dipolymer reactor fresh feed pump 9 by pipeline, the 3rd hot dipolymer reactor fresh feed pump 9 connects the opening for feed of the 3rd hot dipolymer reactor feed preheater 10 by pipeline, the discharge port of the 3rd hot dipolymer reactor feed preheater 10 connects the 3rd hot dipolymer reactor 11 by pipeline.
Be provided with the pipeline that is connected between constant temperature interchanger 4 and the second hot dipolymer reactor 6.Control by valve, can realize in parallel with the first hot dipolymer reactor 5.
The first hot dipolymer reactor 5 and the second hot dipolymer reactor 6 are provided with the pipeline that returns to dimerization reaction charging surge tank 2, on this return pipeline, pressure regulator valve are installed.
Constant temperature interchanger 4 is provided with secondary reduced steam and circulating condensing water.Available secondary reduced steam heating, also the available cycles water for cooling, effectively control and enter the temperature of the first hot dipolymer reactor 5 and the second hot dipolymer reactor 6 at optimal reaction temperature.Constant temperature interchanger 4 adopts shell and tube heat exchanger, comprises circulating condensing water and secondary reduced steam, and hot dimerization charging is played to the temperature control action kou.
On pipeline, flow control valve is installed between dimerization reaction surge tank 2 and constant temperature interchanger 4.
The specific works process is: dimerization reaction charging surge tank 2 is collected the raw material after the pre-separation that will enter hot dipolymer reactor reaction, fully mix, prevent the larger variation of feed composition that front system fluctuation brings, in feed composition, cyclopentadiene is the 10.9%(massfraction), dimerization reaction charging surge tank liquid level is controlled 60% height, squeeze into constant temperature interchanger 4 by constant temperature interchanger fresh feed pump 3, heat transferring medium secondary reduced steam pressure used is 0.28Mpa, 136 ℃ of temperature, 23 ℃ of circulating condensing water temps, according to circumstances changeable use, make the incomplete polymerization of CPD, measure the 7%(massfraction with CPD in the charging of de-isoprene tower 8), after de-isoprene tower 8 removes isoprene, tower reactor is with the 10.3%(massfraction) material enter the 3rd hot dipolymer reactor 11 and reacted, under the control of the 3rd hot dipolymer reactor preheater 10, the 3rd hot dipolymer reactor 11 pressure are 0.52Mpa, 99 ℃ of temperature, CPD is converted into to DCPD fully.
The above, it is only preferred embodiment of the present utility model, be not the utility model to be done to the restriction of other form, any those skilled in the art may utilize the technology contents of above-mentioned announcement to be changed or be modified as the equivalent embodiment of equivalent variations.But every technical solutions of the utility model content that do not break away from, any simple modification, equivalent variations and the remodeling above embodiment done according to technical spirit of the present utility model, still belong to the protection domain of technical solutions of the utility model.
Claims (7)
1. a hot dimerization is produced the device of dicyclopentadiene, comprise dimerization reaction surge tank (2), hot dimerization reaction generating unit, between dimerization reaction surge tank (2) and hot dimerization reaction generating unit, pipeline is connected, and it is characterized in that: the pipeline between dimerization reaction surge tank (2) and hot dimerization reaction generating unit is provided with constant temperature interchanger (4).
2. a kind of hot dimerization according to claim 1 is produced the device of dicyclopentadiene, it is characterized in that: between described dimerization reaction surge tank (2) and constant temperature interchanger (4), flow control valve is installed on connecting pipeline.
3. a kind of hot dimerization according to claim 1 is produced the device of dicyclopentadiene, it is characterized in that: described constant temperature interchanger (4) is provided with the turnover pipeline of secondary reduced steam and circulating condensing water.
4. a kind of hot dimerization according to claim 1 is produced the device of dicyclopentadiene, it is characterized in that: described hot dimerization reaction generating unit comprises the first hot dipolymer reactor (5), the second hot dipolymer reactor (6), de-isoprene tower (8) and the 3rd hot dipolymer reactor (11) of connecting by pipeline successively.
5. a kind of hot dimerization according to claim 1 is produced the device of dicyclopentadiene, it is characterized in that: described hot dimerization reaction generating unit comprises the first hot dipolymer reactor (5), the second hot dipolymer reactor (6), de-isoprene tower (8) and the 3rd hot dipolymer reactor (11), the described first hot dipolymer reactor (5), de-isoprene tower (8) and the 3rd hot dipolymer reactor (11) are connected by pipeline successively, the described second hot dipolymer reactor (6) is in parallel with the first hot dipolymer reactor (5), and directly by pipeline, connect constant temperature interchanger (4).
6. produce the device of dicyclopentadiene according to the described a kind of hot dimerization of claim 4 or 5, it is characterized in that: be in series with de-isoprene tower feed preheater (7) on the front pipeline of described de-isoprene tower (8), on the front pipeline of the 3rd hot dipolymer reactor (11), be in series with the 3rd hot dipolymer reactor feed preheater (10).
7. produce the device of dicyclopentadiene according to the described a kind of hot dimerization of claim 4 or 5, it is characterized in that: the described first hot dipolymer reactor (5), the second hot dipolymer reactor (6) are provided with the pipeline that returns to dimerization reaction surge tank (2), on this return pipeline, pressure regulator valve are installed.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201220648540 CN202953963U (en) | 2012-11-30 | 2012-11-30 | Device for preparing dicyclopentadiene by thermal dimerisation |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201220648540 CN202953963U (en) | 2012-11-30 | 2012-11-30 | Device for preparing dicyclopentadiene by thermal dimerisation |
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| CN202953963U true CN202953963U (en) | 2013-05-29 |
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| CN 201220648540 Expired - Lifetime CN202953963U (en) | 2012-11-30 | 2012-11-30 | Device for preparing dicyclopentadiene by thermal dimerisation |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104591949A (en) * | 2013-10-30 | 2015-05-06 | 中石化上海工程有限公司 | Method for separating piperylene from petroleum cracking C5 fraction |
| CN104591948A (en) * | 2013-10-30 | 2015-05-06 | 中石化上海工程有限公司 | Method for reducing energy consumption in the process for separation of 1,3-pentadiene from petroleum cracking C5 fraction |
| US11465951B2 (en) | 2018-12-12 | 2022-10-11 | Sabic Global Technologies B.V. | Dimerization of cyclopentadiene using shell and tube heat exchanger |
| CN115489091B (en) * | 2022-11-16 | 2023-01-31 | 淄博鲁华泓锦新材料集团股份有限公司 | Polymerization reaction-based polydicyclopentadiene tube continuous extrusion device and process |
-
2012
- 2012-11-30 CN CN 201220648540 patent/CN202953963U/en not_active Expired - Lifetime
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104591949A (en) * | 2013-10-30 | 2015-05-06 | 中石化上海工程有限公司 | Method for separating piperylene from petroleum cracking C5 fraction |
| CN104591948A (en) * | 2013-10-30 | 2015-05-06 | 中石化上海工程有限公司 | Method for reducing energy consumption in the process for separation of 1,3-pentadiene from petroleum cracking C5 fraction |
| CN104591948B (en) * | 2013-10-30 | 2018-04-24 | 中石化上海工程有限公司 | It is a kind of to reduce the method that pentadiene process energy consumption is separated from petroleum cracking C5 fractions |
| CN104591949B (en) * | 2013-10-30 | 2018-04-24 | 中石化上海工程有限公司 | A kind of method that pentadiene is separated in the C5 fractions from petroleum cracking |
| US11465951B2 (en) | 2018-12-12 | 2022-10-11 | Sabic Global Technologies B.V. | Dimerization of cyclopentadiene using shell and tube heat exchanger |
| CN115489091B (en) * | 2022-11-16 | 2023-01-31 | 淄博鲁华泓锦新材料集团股份有限公司 | Polymerization reaction-based polydicyclopentadiene tube continuous extrusion device and process |
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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: ZIBO LUHUA HONGJIN NEW MATERIAL CO., LTD. Free format text: FORMER NAME: ZIBO LUHUA HONGJIN CHEMICAL CO., LTD. |
|
| CP03 | Change of name, title or address |
Address after: 255411 No. 3, Feng Bei Road, Zhangdian District, Shandong, Zibo Patentee after: ZIBO LUHUA HONGJIN NEW MATERIAL Co.,Ltd. Address before: 16, building 255086, block A, macromolecule material industrial innovation park, Zibo hi tech Zone, Shandong Patentee before: Zibo Luhua Hongjin Chemical Co.,Ltd. |
|
| CP01 | Change in the name or title of a patent holder |
Address after: 255411 No. 3, Feng Bei Road, Zhangdian District, Shandong, Zibo Patentee after: Zibo luhuahongjin New Material Group Co.,Ltd. Address before: 255411 No. 3, Feng Bei Road, Zhangdian District, Shandong, Zibo Patentee before: ZIBO LUHUA HONGJIN NEW MATERIAL Co.,Ltd. |
|
| CP01 | Change in the name or title of a patent holder | ||
| CX01 | Expiry of patent term |
Granted publication date: 20130529 |
|
| CX01 | Expiry of patent term |