CN102690163A - Continuous production method and device utilizing dipentene to prepare p-cymene - Google Patents
Continuous production method and device utilizing dipentene to prepare p-cymene Download PDFInfo
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- CN102690163A CN102690163A CN201210172436XA CN201210172436A CN102690163A CN 102690163 A CN102690163 A CN 102690163A CN 201210172436X A CN201210172436X A CN 201210172436XA CN 201210172436 A CN201210172436 A CN 201210172436A CN 102690163 A CN102690163 A CN 102690163A
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- kautschin
- paracymene
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Abstract
The invention provides a continuous production method and a device utilizing dipentene to prepare p-cymene. The method comprises the following steps: firstly, filling a catalyst in a fixed bed reactor, filling nitrogen, preheating dipentene by a preheater and then feeding dipentene into the fixed bed reactor to conduct dehydrogenation reaction; and colling and distilling materials subjected to dehydrogenation reaction so as to obtain a high-purity product. The invention also discloses a device, which utilizes the method and the structure that the production process including three fixed bed reactors connected in series instead of one fixed bed reactor in the prior art is adopted, the unstable state during the dehydrogenation reaction is improved, the production efficiency is improved, and the service life of the catalyst is prolonged; and meanwhile, automatic control is conveniently adopted in the production process, the product quality is stable, the purposes of safety, high efficiency and low consumption are achieved, the production scale is easy to enlarge.
Description
Technical field
The present invention relates to a kind of kautschin prepares the Paracymene continuous production method and can effectively utilize this kind method to carry out Paracymene quantity-produced relative unit.
Background technology
Kautschin is the one type of monocyclic terpene by product (comprising Foxlene, terpinene, Paracymene or the like, the general designation kautschin) during from afforestation product turps SYNTHETIC CAMPHOR DAB 6 and Terpineol 350, and kautschin is most of as paint solvent at present, is worth not high.Therefore, how to develop kautschin, processing more, value product is a big problem.The kautschin shortening is processed Paracymene, as spices midbody, pesticide intermediate or processing other products, can improve turps converted products added value then.
The synthetic Paracymene of industrial dipentene catalytic dehydrogenation has vapor phase process and liquid phase method usually.Vapor phase process has been realized industriallization abroad, and used dehydrogenation catalyst mainly is catalyzer such as carried noble metal Pd, R, and productive rate is higher, but this technology catalyst system therefor is very expensive; Vapor phase process gasification condensation increases energy consumption in addition, makes production cost high like this.Though existing liquid phase method can use relatively cheap catalyzer, energy consumption reduces relatively, and impurity is many in the products obtained therefrom, causes separating difficulty, causes the pure Gao Bugao of product.Also there is following subject matter simultaneously:
(1) problem that adopts the rhythmic reaction production technique to exist: the rhythmic reaction production technique is kautschin to be placed on intermittently react in the dehydrogenation reaction still, after raw material and catalyst by proportion drop into reaction kettle, under whisking appliance stirs, heats up then and reacts; Through reaction in several hours, after the sampling detection is qualified, could shut down discharging; Remove by filter catalyzer and obtain product, need to change after isolated catalyzer is reused 3 ~ 10 times, work-ing life is short; Reclaiming often; Catalyzer mass consumption, the less stable of quality product, industrial scale are difficult to amplify.
(2) problem that adopts continuous fixed-bed process for preparing to exist: the one, catalyst system therefor, work-ing life is not long, grow most only about 3 months, make the production operation process become loaded down with trivial details, production cost is higher; The 2nd, when adopting single fixed-bed reactor to produce, often because need the higher temperature of reaction of control in the fixed-bed reactor, long-time high temperature can make the catalyst life that is seated in the reactor drum shorten.
(3) need to solve production process whole process using computer automation control problem, otherwise be difficult to guarantee its final product quality.
Summary of the invention
The objective of the invention is provides a kind of product purity is high, quality kautschin good, that production safety is stable, easy to operate prepares Paracymene continuous production method and device thereof to being the problem that exists in the production of feedstock production Paracymene with the kautschin at present.
The technical problem that the present invention solved adopts following technical scheme to realize:
The continuous production method that the present invention's kautschin prepares Paracymene may further comprise the steps:
(1) dehydrogenation reaction: catalyzer is respectively charged into three fixed-bed reactor; Feed nitrogen, open charge pump, the raw material kautschin is after preheating; Send into the import of fixed-bed reactor I; Three fixed-bed reactor of flowing through successively carry out dehydrogenation reaction, and the material that exports out from the fixed-bed reactor III is the material of accomplishing after the dehydrogenation reaction.
Said catalyzer is a HS particle ambrose alloy, and be 3 ~ 12 months work-ing life, disposable joining respectively in three fixed-bed reactor, and the add-on of each fixed-bed reactor is 600kg ~ 2000kg.
In above-mentioned dehydrogenation reaction process, the kautschin preheating temperature is 170 ℃ ~ 180 ℃.
The operational condition of dehydrogenation reaction is: the kautschin flow that gets into fixed-bed reactor is 0.1 m
3/ h ~ 0.5 m
3/ h, the fixed-bed reactor reaction pressure is 0.01Mpa ~ 5Mpa, and fixed-bed reactor I temperature of reaction is 170 ℃ ~ 190 ℃, and fixed-bed reactor II temperature of reaction is 190 ℃ ~ 220 ℃, and fixed-bed reactor III temperature of reaction is 220 ℃ ~ 260 ℃.
(2) cooling: the material of accomplishing dehydrogenation reaction comes out to get into water cooler by fixed-bed reactor III bottom and is cooled to room temperature, and being with the Paracymene is the liquid mixture of main body, through rectifying separation, can obtain high purity Paracymene product again.
From the material that comes out in fixed-bed reactor III bottom; Contained Paracymene massfraction is 62% ~ 82% in the product, and in the dehydrogenation product Paracymene and to the Meng alkane purity high, other by products are seldom; Make things convenient for rectifying separation, can obtain highly purified Paracymene product and sub product alkane in the Meng.
It should be noted that; Before dehydrogenation reaction is stable; Should be according to the transformation efficiency of kautschin in the sample of water cooler bottom discharge port sampling Detection and the purity of Paracymene, control gets into the material feed rate of fixed-bed reactor, regulates the temperature and pressure of fixed-bed reactor internal reaction.Paracymene massfraction 62% ~ 82% in the discharging product of control fixed-bed reactor III bottom.
Production process is carried out continuously: the I opening for feed constantly adds kautschin to the fixed-bed reactor I from the fixed-bed reactor top; The III discharge port is constantly emitted the Paracymene product from the fixed-bed reactor bottom; Form continuous production; The full scale production process is sent to computer center through pressure, temperature, the flow sensor at each reference mark, implements the continuous production full automatic control.
Said preheating or heating thermal source can be electric heater unit, superheated vapour or thermal oil.
The present invention's kautschin prepares the relative unit of the continuous production method of Paracymene; Mainly form by material storaging tank, charge pump, under meter, preheater, fixed-bed reactor I, fixed-bed reactor II, fixed-bed reactor III, water cooler, product storage tank; Wherein, the material storaging tank outlet links to each other with the charge pump import, and the charge pump outlet links to each other with the under meter import; The outlet of under meter links to each other with the preheater import; The preheater outlet links to each other with fixed-bed reactor I upper inlet, and fixed-bed reactor I lower part outlet links to each other with fixed-bed reactor II upper inlet, and the lower part outlet of fixed-bed reactor II links to each other with the upper inlet of fixed-bed reactor III; The lower part outlet of fixed-bed reactor III links to each other with cooler inlet, and cooler outlet links to each other with product storage tank.Be respectively arranged with TP or pressure transmitter or flow sensor in the fixed-bed reactor, TP, pressure transmitter and flow sensor all are connected with computer controlling center.Pressure or temperature or the flow sensor of full scale production process parameter information through each reference mark is sent to computer center, implements the continuous production full automatic control.
In device of the present invention, said fixed-bed reactor are round shape, and its inside is provided with the screen cloth that is used for fixing catalyzer, is provided with TP and pressure transmitter in the fixed-bed reactor; The fixed-bed reactor periphery is provided with the heating cooling jacket, heating cooling jacket import through one valve is housed arm link to each other with heating medium pipe, heat-eliminating medium pipe.
Described charge pump is reciprocal plunger metering pump.
Described preheater is a kind of in double-pipe exchanger, shell and tube heat exchanger, the plate-type heat exchanger.
Said water cooler is tubular heat exchanger or plate-type heat exchanger.
Compared with prior art, the present invention has following advantage:
(1) the fixed bed continuous dehydrogenation production technique that adopts; Be beneficial to and improve unsteady state in the production; Enhance productivity, conveniently adopt automatic control system in process of production, help reducing the manual operation deviation; Make production process reach the requirement of constant product quality, safe and efficient low consumption, be easy to industrial scale and amplify;
(2) behind three placed in-line fixed-bed reactor of employing; The differing temps of the different dehydrogenation stages of convenient control, the temperature of reaction of first fixed bed is lower, and the 3rd fixed bed reaction temperature is than the first two individual height; So, can conveniently control the temperature of the catalyzer in the fixed-bed reactor.Avoid catalyzer long-time running at high temperature and caused inactivation, thereby prolonged the work-ing life of catalyzer;
(3) through selecting HS particle nickel-copper catalyst for use, active high to the kautschin catalysis dehydrogenation, good stability; Convenient regeneration reaches 6 ~ 12 months work-ing life, has solved the past because of the catalyst life weak point; In the production repeatedly more the cost that causes of catalyst changeout increase problem such as plant factor is low.
Description of drawings
Fig. 1 prepares Paracymene serialization production equipment synoptic diagram for kautschin of the present invention.
Embodiment
Below in conjunction with accompanying drawing and embodiment the present invention is done further explain.
Embodiment 1 is Paracymene serialization production equipment embodiment of the present invention
Referring to the synoptic diagram of embodiment of relative unit for preparing the continuous production method of Paracymene among the present invention of Fig. 1 based on kautschin; In the present embodiment; Form by material storaging tank 1, charge pump 2, under meter 2, preheater 4, fixed-bed reactor I 5, fixed-bed reactor II 6, fixed-bed reactor III 7, water cooler 8, product storage tank 9; Material storaging tank 1 outlet links to each other with charge pump 2 imports; Charge pump 2 outlets link to each other with under meter 3 imports, and the outlet of under meter 3 links to each other with preheater 4 imports, and preheater 4 outlets link to each other with fixed-bed reactor I 5 upper inlet; Fixed-bed reactor I 5 lower part outlets link to each other with fixed-bed reactor II 6 upper inlet; The lower part outlet of fixed-bed reactor II 6 links to each other with the upper inlet of fixed-bed reactor III 7, and the lower part outlet of fixed-bed reactor III 7 links to each other with water cooler 8 imports, and water cooler 8 outlets link to each other with product storage tank 9.Fixed-bed reactor I 5, fixed-bed reactor II 6, fixed-bed reactor III 7 are respectively arranged with TP, pressure transmitter and flow sensor, and TP, pressure transmitter and flow sensor all are connected with computer controlling center.Full scale production process parameter information is sent to computer center through pressure, temperature, the flow sensor at each reference mark, implements the continuous production full automatic control.
In the present embodiment, fixed-bed reactor I 5, fixed-bed reactor II 6, fixed-bed reactor III 7 are round shape, and its inside is provided with screen cloth, is used for fixing catalyzer; Be provided with TP and pressure transmitter in the fixed-bed reactor; The fixed-bed reactor periphery is provided with the heating cooling jacket, heating cooling jacket import through one valve is housed arm link to each other with heating medium pipe, heat-eliminating medium pipe, the heating thermal source is an electric heater.
Embodiment 2 is prepared the continuous production method operation steps embodiment of Paracymene by kautschin
Catalyzer is respectively charged into fixed-bed reactor I 5, fixed-bed reactor II 6 and fixed-bed reactor III 7; Feed nitrogen; Open the heating jacket of three fixed-bed reactor; Fixed-bed reactor I 5 is preheating to 180 ℃, and fixed-bed reactor II 6 is preheating to 190 ℃, and fixed-bed reactor III 7 is preheating to 220 ℃; With being stored in raw material kautschin in the material storaging tank 1 with 0.5m
3The flow of/h; Deliver in the preheater 4; Kautschin is preheating to 170 ℃, sends into 5 imports of fixed-bed reactor I, and flow through successively fixed-bed reactor II 6 and fixed-bed reactor III 7; Carry out dehydrogenation reaction, the material that comes out from fixed-bed reactor III 7 is the material of accomplishing after the dehydrogenation reaction.
The operational condition of dehydrogenation reaction is: the kautschin flow that gets into fixed-bed reactor is 0.3 m
3/ h, the fixed-bed reactor reaction pressure is 3Mpa, and fixed-bed reactor I 5 temperature of reaction are 180 ℃, and fixed-bed reactor II 6 temperature of reaction are 200 ℃, and fixed-bed reactor III 7 temperature of reaction are 250 ℃.
Catalyzer can be HS particle ambrose alloy, and the catalyzer add-on can be 800kg, and the kautschin preheating temperature is 180 ℃; The heating thermal source is an electric heater.
Before dehydrogenation reaction is stable; Transformation efficiency and Paracymene product gas purity according to kautschin in the sample of fixed-bed reactor III 7 bottom discharge mouth sampling Detection; Control gets into the kautschin feed rate of fixed-bed reactor, regulates the temperature and pressure of fixed-bed reactor internal reaction.The product of fixed-bed reactor III 7 bottom discharges, product Paracymene relative mass mark should reach 62 ~ 82%.
Constantly add kautschin to fixed-bed reactor I 5 from fixed-bed reactor I 5 top fed mouths, constantly emit alkane product in the Meng, form continuous production from fixed-bed reactor III 7 bottom discharge mouths.
Following examples are operating procedure condition embodiment, and catalyzer is HS particle ambrose alloy, and operation steps is all identical with embodiment 2.
Embodiment 3 ~ 6
Dehydrogenation reaction conditions control: set three equal 500kg of fixed bed reactor catalyst add-on, 1000kg, 1500kg, 2000 kg, 2500kg respectively, the kautschin preheating temperature is 170 ℃ ~ 180 ℃; The kautschin flow that gets into fixed-bed reactor is 0.1 m3/h, 0.2 m3/h, 0.3 m3/h, 0.4 m3/h, 0.5 m3/h; Fixed bed device reaction pressure is 0.01Mpa, 1 Mpa, 3 Mpa, 4Mpa, 5Mpa; Fixed-bed reactor I temperature of reaction is 170 ℃, 175 ℃, 180 ℃, 185 ℃, 190 ℃; Fixed-bed reactor II temperature of reaction is 190 ℃, 195 ℃, 200 ℃, 210 ℃, 220 ℃, and fixed-bed reactor III temperature of reaction is 220 ℃, 230 ℃, 240 ℃, 250 ℃, 260 ℃.
Question response conditional stability, Paracymene relative mass mark is respectively 69.3%, 77.2%, 81.1%, 75.3%, 71.8%, 62.5% in the sampling analysis dehydrogenation product.
More than show and described 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; That describes in the foregoing description and the specification sheets just explains principle of the present invention; Under the prerequisite that does not break away from spirit and scope of the invention, the present invention also has various changes and modifications, and these variations and improvement all fall in the scope of the invention that requires protection.The present invention requires protection domain to be defined by appending claims and equivalent thereof.
Claims (8)
1. kautschin prepares the continuous production method of Paracymene, it is characterized in that, may further comprise the steps:
(1) dehydrogenation reaction: catalyzer is respectively charged into three fixed-bed reactor; Feed nitrogen, open charge pump, the raw material kautschin is after preheating; Send into the import of fixed-bed reactor I; Three the placed in-line fixed-bed reactor of flowing through successively carry out dehydrogenation reaction, and the kautschin flow that gets into fixed-bed reactor is 0.1 m
3/ h ~ 0.5 m
3/ h; The fixed-bed reactor reaction pressure is 0.01Mpa ~ 5Mpa; Fixed-bed reactor I temperature of reaction is 170 ℃ ~ 190 ℃; Fixed-bed reactor II temperature of reaction is 190 ℃ ~ 220 ℃, and fixed-bed reactor III temperature of reaction is 220 ℃ ~ 260 ℃, and the material that exports out from the fixed-bed reactor III is the material of accomplishing after the dehydrogenation reaction;
(2) cooling: the material of accomplishing dehydrogenation reaction comes out to get into water cooler by fixed-bed reactor III bottom and is cooled to room temperature, and promptly Paracymene is the bulk liquid mixture, through rectifying separation, obtains high purity Paracymene product.
2. kautschin according to claim 1 prepares the continuous production method of Paracymene; It is characterized in that; Said catalyzer is a HS particle ambrose alloy, disposable joining respectively in three fixed-bed reactor, and the amount that adds in each fixed-bed reactor is 600kg ~ 1000kg.
3. kautschin according to claim 1 prepares the continuous production method of Paracymene, it is characterized in that, said kautschin preheating temperature is 170 ℃ ~ 180 ℃.
4. relative unit for preparing the continuous production method of Paracymene based on the said kautschin of claim 1; It is characterized in that; Mainly be made up of material storaging tank, charge pump, under meter, preheater, fixed-bed reactor I, fixed-bed reactor II, fixed-bed reactor III, water cooler, basin, the material storaging tank outlet links to each other with the charge pump import, and the charge pump outlet links to each other with the under meter import; The outlet of under meter links to each other with the preheater import; The preheater outlet links to each other with fixed-bed reactor I upper inlet, and fixed-bed reactor I lower part outlet links to each other with fixed-bed reactor II upper inlet, and the lower part outlet of fixed-bed reactor II links to each other with the upper inlet of fixed-bed reactor III; The lower part outlet of fixed-bed reactor III links to each other with cooler inlet, and cooler outlet links to each other with basin; Simultaneously, fixed-bed reactor equipment is respectively arranged with TP or pressure transmitter or flow sensor, and TP, pressure transmitter and flow sensor all are connected with computer controlling center.
5. the relative unit for preparing the continuous production method of Paracymene based on kautschin according to claim 1; It is characterized in that; Said fixed-bed reactor are round shape, and its inside is provided with the screen cloth that is used for fixing catalyzer, are provided with TP and pressure transmitter in the fixed-bed reactor; The fixed-bed reactor periphery is provided with the heating cooling jacket, heating cooling jacket import through one valve is housed arm link to each other with heating medium pipe, heat-eliminating medium pipe.
6. according to claim 1ly prepare the relative unit of the continuous production method of Paracymene, it is characterized in that said charge pump is reciprocal plunger metering pump based on kautschin.
7. according to claim 1ly prepare the relative unit of the continuous production method of Paracymene based on kautschin, it is characterized in that, said liquor preheater is a kind of in double-pipe exchanger, shell and tube heat exchanger, the plate-type heat exchanger.
8. according to claim 1ly prepare the relative unit of the continuous production method of Paracymene, it is characterized in that said water cooler is tubular heat exchanger or plate-type heat exchanger based on kautschin.
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| CN201210172436XA CN102690163A (en) | 2012-05-30 | 2012-05-30 | Continuous production method and device utilizing dipentene to prepare p-cymene |
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| CN201210172436XA CN102690163A (en) | 2012-05-30 | 2012-05-30 | Continuous production method and device utilizing dipentene to prepare p-cymene |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111821919A (en) * | 2020-07-10 | 2020-10-27 | 吉林凯莱英制药有限公司 | Continuous catalytic hydrogenation equipment and continuous catalytic hydrogenation method for pyridine compounds |
| CN114751802A (en) * | 2021-11-23 | 2022-07-15 | 辽宁抚清助剂有限公司 | Industrial preparation method of p-menthane |
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| CN1006061B (en) * | 1986-03-21 | 1989-12-13 | 采煤化学公司 | Process for manufacturing styrene |
| CN101462923A (en) * | 2009-01-07 | 2009-06-24 | 中国林业科学研究院林产化学工业研究所 | Method for producing p-cymene by continuous production and apparatus thereof |
-
2012
- 2012-05-30 CN CN201210172436XA patent/CN102690163A/en active Pending
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1006061B (en) * | 1986-03-21 | 1989-12-13 | 采煤化学公司 | Process for manufacturing styrene |
| CN101462923A (en) * | 2009-01-07 | 2009-06-24 | 中国林业科学研究院林产化学工业研究所 | Method for producing p-cymene by continuous production and apparatus thereof |
Non-Patent Citations (1)
| Title |
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| 李凝: "以松节油为原料合成对异丙基甲苯", 《精细化工》 * |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111821919A (en) * | 2020-07-10 | 2020-10-27 | 吉林凯莱英制药有限公司 | Continuous catalytic hydrogenation equipment and continuous catalytic hydrogenation method for pyridine compounds |
| CN114751802A (en) * | 2021-11-23 | 2022-07-15 | 辽宁抚清助剂有限公司 | Industrial preparation method of p-menthane |
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Application publication date: 20120926 |