CN105669355A - Process for preparation of styrene from ethylbenzene - Google Patents
Process for preparation of styrene from ethylbenzene Download PDFInfo
- Publication number
- CN105669355A CN105669355A CN201410670497.8A CN201410670497A CN105669355A CN 105669355 A CN105669355 A CN 105669355A CN 201410670497 A CN201410670497 A CN 201410670497A CN 105669355 A CN105669355 A CN 105669355A
- Authority
- CN
- China
- Prior art keywords
- dehydrogenation
- reaction
- ethylbenzene
- catalyst
- logistics
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Landscapes
- Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
- Catalysts (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The present invention relates to a process for preparation of styrene from ethylbenzene, and mainly solves the problem that a hydrogen oxidation catalyst is low in catalytic activity and selectivity to further cause low whole process dehydrogenation reaction ethylbenzene conversion rate and styrene selectivity when ethylbenzene dehydrogenation reaction using an iron-potassium-based catalyst for catalysis and ethylbenzene dehydrogenation material hydrogen oxidation reaction using a noble metal catalyst for catalysis are in series connection. The process can well solve the problems, the process comprises a first dehydrogenation reaction step, a potassium removal step, a hydrogen oxidation reaction step and a second dehydrogenation reaction step, a dehydrogenation catalyst for the dehydrogenation reaction steps is Fe-K-based ethylbenzene dehydrogenation catalyst; a potassium retarder is used in the potassium removal step, the potassium retarder comprises, by weight, a) 5 to 90 parts of aluminum calculating on the basis of aluminum oxide and b) 10 to 95 parts of silicon calculating on the basis of silicon dioxide, and the total of the aluminum oxide and the silicon dioxide is 100 parts; and the hydrogen oxidation catalyst is a noble metal-based hydrogen oxidation catalyst; and the process can be used for the industrial production of styrene by ethylbenzene dehydrogenation.
Description
Technical field
The present invention relates to ethylbenzene dehydrogenation-hydroxide reaction technique, especially with regard to a kind of ethylbenzene dehydrogenation-hydroxide reaction technique adopting resistance potassium agent.
Background technology
Styrene is basic Organic Chemicals. Ethylbenzene dehydrogenation technique is to produce cinnamic main method. Ethylbenzene dehydrogenation generates styrene and hydrogen is the balancing response that heat absorption, a molecular number increase. Improve reaction temperature, reduce reaction pressure, use dynamical dehydrogenation, the conversion per pass of ethylbenzene can be improved, but be still limited by the restriction of thermodynamical equilibrium.
Ethylbenzene dehydrogenation oxidation process is increase H 2 selective oxidation on the basis of ethylbenzene dehydrogenation, its elementary process is dehydrogenation-hydroxide-dehydrogenation, that is the first step is dehydrogenation reaction, second step is hydroxide reaction, namely the first step reacts the oxygen generation combustion reaction of hydrogen and the addition produced, and the product that the 3rd step is second step proceeds dehydrogenation reaction. For ethylbenzene dehydrogenation technique, ethylbenzene dehydrogenation-hydroxide technique mainly has 2 advantages: (1) ethylbenzene dehydrogenation is the endothermic reaction, and hydrogen burning produces heat and provides heat for next step dehydrogenation; (2) owing to the hydrogen of one of product is reacted consumption, ethylbenzene dehydrogenation reaction is conducive to move to generating styrene direction, thus improving the conversion ratio of reaction.
It is generally adopted Fe-K catalyst and is used as the catalyst of ethylbenzene dehydrogenation reaction. Such as adopt patent CN1400052A or the CN1443738A catalyst described for the catalyst of ethylbenzene dehydrogenation reaction.
It is generally adopted the noble metal series catalysts catalyst for hydroxide reaction for ethylbenzene dehydrogenation. The catalyst that US4914249, CN1479649A, CN1705510A describe such as is adopted to be used for the catalyst of hydroxide reaction.
The catalyst for phenylethylene dehydrogenation of industrial use contains the potassium of more content, in course of reaction, and the easy loss gradually of the potassium in catalyst for phenylethylene dehydrogenation. Too much potassium can make hydro-oxidation catalyst poisoning, reduces activity and selectivity, reduces hydroxide reaction efficiency. It addition, too low hydroxide activity can make the oxygen in hydroxide process all not consume, remaining oxygen can make follow-up dehydrogenation reaction catalyst poisoning. The low selectivity of hydro-oxidation catalyst means that more aromatic hydrocarbons is burned, adds raw material consumption.
But with Fe-K catalyst catalysis ethylbenzene dehydrogenation reaction with when connecting with the ethylbenzene dehydrogenation material hydroxide reaction of noble metal series catalysts catalysis, cause the problem that hydro-oxidation catalyst catalysis activity and selectivity is low, in turn result in the problem that whole process selectivity of styrene is low and styrene list receipts are low.
Summary of the invention
When the technical problem to be solved is to be connected with the ethylbenzene dehydrogenation material hydroxide reaction of noble metal series catalysts catalysis by the ethylbenzene dehydrogenation reaction of Fe-K catalyst catalysis, cause the problem that hydro-oxidation catalyst catalysis activity and selectivity is low, it is provided that a kind of new for the technique of preparing styrene from ethylbenzene. This technique has the advantage improving hydroxide reaction activity and selectivity, correspondingly has the advantage improving the full-range selectivity of styrene of preparing styrene from ethylbenzene and styrene list receipts.
In order to solve above-mentioned technical problem, the technical solution used in the present invention is as follows: by the technique of preparing styrene from ethylbenzene, comprise the following steps:
(1) in the first dehydrogenation reaction operation, with water for diluent, raw material and the contact of the first dehydrogenation containing ethylbenzene occur ethylbenzene dehydrogenation reaction to generate containing ethylbenzene, hydrogen and cinnamic reaction logistics 1;
(2) reaction logistics 1 obtains reaction logistics 2 in de-potassium operation through contacting with resistance potassium agent;
(3) containing reaction logistics 2 and the material of oxygen in hydroxide reaction operation, contact with hydro-oxidation catalyst and carry out hydroxide reaction and reduce and react hydrogen content in logistics 2 and obtain logistics 3;
(4) logistics 3 contacts with the second dehydrogenation in the second dehydrogenation reaction operation and makes the further dehydrogenation of ethylbenzene generate logistics 4;
Described resistance potassium agent, in parts by weight, comprises aluminum a) in aluminium oxide 5～90 parts, and b) in the silicon of silicon dioxide 10～95 parts, and total number of aluminium oxide and silicon dioxide is 100; Described hydro-oxidation catalyst is noble metal system hydro-oxidation catalyst.
In technique scheme, the first dehydrogenation and/or the second dehydrogenation are preferably Fe-K system catalyst for phenylethylene dehydrogenation.
In technique scheme, the reaction temperature of the first dehydrogenation reaction operation is preferably 550～650 DEG C, and reaction pressure is preferably 0.1～10 kg/cm2, liquid air speed is preferably 0.5～3 hour-1, water/ethylbenzene weight ratio is preferably 0.6～3.
In technique scheme, the reaction temperature of the second dehydrogenation reaction operation is preferably 550～650 DEG C, and reaction pressure is preferably 0.1～10 kg/cm2, liquid air speed is preferably 0.5～3 hour-1, water/ethylbenzene weight ratio is preferably 0.6～3.
In technique scheme, hydro-oxidation catalyst is preferably loaded platinum catalyst.
In technique scheme, the reaction temperature of hydroxide reaction operation is preferably 500～700 DEG C, and reaction pressure is preferably 0.1～10 kg/cm2, liquid air speed is preferably 1～10 hour-1, the mol ratio of hydrogen and oxygen is preferably (2～10): 1.
In technique scheme, the temperature that reaction logistics 1 contacts with resistance potassium agent is preferably 500～700 DEG C, and pressure is preferably 0.1～10 kg/cm2, liquid air speed is preferably 0.2～50 hour-1。
In technique scheme, the consumption of resistance potassium agent is preferably the 5～60% of the first dehydrogenation weight.
In technique scheme, in parts by weight, resistance potassium agent preferably comprises a) aluminum in aluminium oxide 10～70 parts, b) in the silicon of silicon dioxide 30～90 parts.
In technique scheme, resistance potassium agent be preferably shaped to cellular, adjacent two nest locular wall thickness are preferably 30～500 microns, the number of aperture of resistance potassium agent cross section be preferably 3～150 holes/centimetre2。
In technique scheme, potassium agent nest chamber cross-section is conveniently of circular shape in resistance, triangle, square, polygon, trapezoidal, fan-shaped, oval or irregularly shaped. The profile of whole resistance potassium agent cross section is not particularly limited, for instance for circle, ellipse, square, rectangle, polygon, side's arc or irregularly shaped.
The preparation method of the resistance potassium agent that the present invention adopts does not specially require, for instance the method comprised the following steps can be adopted to prepare: by the desired amount of aluminum source, the mixing of silicon source, molding, drying, then roasting obtains described resistance potassium agent.
In technique scheme, sintering temperature is preferably 400～1800 DEG C, and the time of roasting is preferably 2～30 hours. Roasting adopts two-stage roasting to be better than one section of roasting, and during employing two-stage roasting, the sintering temperature of first paragraph is lower than the sintering temperature of second segment. More preferably the sintering temperature of first paragraph is preferably 400～500 DEG C, first paragraph roasting time preferably 1～10 hour; The temperature of the roasting of second segment is preferably 600～1800 DEG C, and the roasting time of second segment is preferably 2～20 hours. The use of resistance potassium agent now makes hydroxide reaction have better activity and selectivity.
In technique scheme, aluminum source preferably is selected from least one in aluminium oxide, aluminum nitrate, aluminum sulfate, aluminum chloride, aluminium fluoride, aluminum-containing mineral, silicon-aluminum containing mineral.
In technique scheme, silicon source preferably is selected from least one in silicon dioxide, silicon fluoride, sodium silicate, Silicon chloride., tetraethyl orthosilicate, Ludox, silicon ash, siliceous mineral, silicon-aluminum containing mineral.
In technique scheme, dry temperature is preferably 90～200 DEG C.
In technique scheme, the dry time is preferably 1～10 hour.
In the present patent application file, all air speeds or liquid air speed, all represent by the raw material of the first dehydrogenation reaction technique, with ethylbenzene metering contained in described raw material, and stereometer during with ethylbenzene for liquid.
Find by studying, for the Fe-K catalyst of ethylbenzene dehydrogenation in ethylbenzene dehydrogenation process, there is potassium lost thus the problem that causes the hydro-oxidation catalyst potassium intoxication in downstream, (such as de-potassium agent can be placed in dehydrogenation reactor internal vent place by processing with the de-potassium agent of the present invention after ethylbenzene dehydrogenation unit and before hydroxide reaction unit, and/or it is placed in the porch within hydroxide reaction device, and/or de-potassium agent is placed in de-potassium container, make the sequential series according to dehydrogenation reactor-Tuo potassium container-hydroxide reaction device), the problem that hydro-oxidation catalyst is subject to potassium intoxication can be avoided.
Oxygen conversion and the oxygen selectivity of indication of the present invention are obtained by mode calculated as below.
Due to the fact that between ethylbenzene dehydrogenation reaction unit and hydroxide reaction unit, add resistance potassium agent, the potassium that catalyst for phenylethylene dehydrogenation runs off can be caught, effectively prevent the potassium of dehydrogenation loss and hydro-oxidation catalyst is caused poisoning, thus the reactivity worth protecting hydro-oxidation catalyst is unaffected, the oxygen selectivity of hydroxide reaction is up to 91.93%, oxygen conversion is up to 100%, and the oxygen selectivity of hydroxide reaction is only 77.12% on year-on-year basis on year-on-year basis when not adopting the present invention to take off potassium agent, oxygen conversion is only 99.31%; Simultaneously as resistance potassium agent adopts cellular, add gas-solid contact area, improve resistance potassium agent service efficiency, reduce resistance potassium agent consumption simultaneously, save the device space, achieve good technique effect.
Detailed description of the invention
[comparative example 1]
Catalyst for phenylethylene dehydrogenation is according to the preparation of embodiment in patent CN1443738A 1.
Hydro-oxidation catalyst is according to the preparation of embodiment in patent CN1704160A 2.
Reaction evaluating technique and condition: reaction carries out in three tandem reactors: the first reactor carries out the first dehydrogenation reaction, and the second reactor carries out hydroxide reaction, and the 3rd reactor carries out the second dehydrogenation reaction.
First dehydrogenation reaction carries out in 25 millimeters of rustless steel isotherm formula fixed bed reactors of internal diameter, wherein reaction pressure is normal pressure, liquid air speed is 1.0 liters of ethylbenzene/liter catalyst hour, reaction temperature is 610 DEG C, water is diluent, water ratio (water/ethylbenzene) 2.0 (weight ratio), catalyst amount 100 milliliters.
Hydroxide reaction carries out in 25 millimeters of rustless steel isotherm formula fixed bed reactors of internal diameter, and wherein reaction pressure is normal pressure, and reaction temperature is 580 DEG C, catalyst amount 30 milliliters. After material adding oxygen after the first reactor reaction, enter hydroxide reaction device. Oxygen content in hydroxide reaction device entrance material is 1.1 (V) %.
Second dehydrogenation reaction carries out in 25 millimeters of rustless steel isotherm formula fixed bed reactors of internal diameter, wherein reaction pressure is normal pressure, liquid air speed is 1.0 liters of ethylbenzene/liter catalyst hour, reaction temperature is 615 DEG C, water ratio (water/ethylbenzene) 2.0 (weight ratio), catalyst amount 100 milliliters.
Reaction due to upstream catalyst for phenylethylene dehydrogenation potassium lost so that catalyst for hydroxide reaction reactivity worth is gradually reduced, reaches steady statue after reacting 20 days after starting. Reaction Ahau sample analysis, calculates oxygen selectivity and the oxygen conversion of hydroxide reaction, as the hydroxide reaction performance of comparative example 1. The hydroxide reaction results of property of comparative example 1 is in Table 1. The full-range selectivity of styrene of preparing styrene from ethylbenzene and styrene list are received in Table 2.
[embodiment 1]
With comparative example 1, but after the dehydrogenation of the first reactor, add 30 grams of resistance potassium agent. Resistance potassium agent reaction temperature 620 DEG C, normal pressure.
Resistance potassium agent preparation is as follows: take 50 grams of aluminium oxidies and 950 grams of silicon dioxide, mediates, extrusion, 120 DEG C of bakings 4 hours, 450 DEG C of roastings 1 hour, then 1500 DEG C of roastings 4 hours.
The hydroxide reaction performance of embodiment 1 is in Table 1. The full-range selectivity of styrene of full preparing styrene from ethylbenzene and styrene list are received in Table 2.
[comparative example 2]
Except replace the resistance potassium agent in embodiment 1 with aluminium oxide, all the other are all with embodiment 1. Particularly as follows: add 30 grams of aluminium oxidies after the dehydrogenation of the first reactor as resistance potassium agent. Resistance potassium agent temperature is 620 DEG C, normal pressure.
Resistance potassium agent preparation is as follows: take aluminium oxide, extrusion, and 120 DEG C dry 4 hours, 450 DEG C of roastings 1 hour, then 1500 DEG C of roastings 4 hours.
Hydroxide reaction performance is in Table 1. The full-range selectivity of styrene of preparing styrene from ethylbenzene and styrene list are received in Table 2.
[comparative example 3]
Except with the resistance potassium agent in silicon oxide instead embodiment 1, all the other are all with embodiment 1. Particularly as follows: add 30 grams of silicon oxides after the dehydrogenation of the first reactor as resistance potassium agent. Resistance potassium agent temperature is 620 DEG C, normal pressure.
Resistance potassium agent preparation is as follows: take silicon oxide, extrusion, and 120 DEG C dry 4 hours, 450 DEG C of roastings 1 hour, then 1500 DEG C of roastings 4 hours.
Hydroxide reaction performance is in Table 1. The full-range selectivity of styrene of preparing styrene from ethylbenzene and styrene list are received in Table 2.
[embodiment 2]
With embodiment 1, but change resistance potassium agent preparation method.
Resistance potassium agent preparation is as follows: take 1103 gram of nine water aluminum nitrate and 850 grams of silicon dioxide, mediates, extrusion, 120 DEG C of bakings 4 hours, 500 DEG C of roastings 4 hours, then 1500 DEG C of roastings 4 hours.
The hydroxide reaction performance of embodiment 2 is in Table 1. The full-range selectivity of styrene of preparing styrene from ethylbenzene and styrene list are received in Table 2.
[embodiment 3]
With embodiment 1, but between the first dehydrogenation reactor and hydroxide reaction device, increase resistance nak response device. Resistance nak response carries out in 25 millimeters of rustless steel fixed bed reactors of internal diameter, and wherein reaction temperature is 500 DEG C, catalyst amount 30 grams, and reaction pressure is 0.5 kg/cm2.Through the first reacted material of dehydrogenation reactor, it is directly entered resistance nak response device.
Resistance nak response device reacting rear material adds oxygen, enters hydroxide reaction device. Oxygen content in hydroxide reaction device entrance material is 1.1 (V) %.
Resistance potassium agent preparation is as follows: take 400 grams of aluminium oxidies and 1875 grams of waterglass containing 32% (weight) silicon dioxide, mediates, extrusion, 120 DEG C of bakings 4 hours, 450 DEG C of roastings 10 hours, then 1100 DEG C of roastings 4 hours.
The hydroxide reaction performance of embodiment 3 is in Table 1. The full-range selectivity of styrene of preparing styrene from ethylbenzene and styrene list are received in Table 2.
[embodiment 4]
With embodiment 3, but resistance potassium agent reaction temperature is 580 DEG C, and reaction pressure is 0.8 kg/cm2, reaction velocity is 0.2 liter of ethylbenzene/liter catalyst hour. Change resistance potassium agent preparation method simultaneously.
Resistance potassium agent preparation is as follows: take 2348 grams of aluminum sulfate and 300 grams of silicon dioxide, mediates, extrusion, 120 DEG C of bakings 4 hours, 420 DEG C of roastings 2 hours, then 800 DEG C of roastings 4 hours.
The hydroxide reaction performance of embodiment 4 is in Table 1. The full-range selectivity of styrene of preparing styrene from ethylbenzene and styrene list are received in Table 2.
[embodiment 5]
With embodiment 3, but resistance potassium agent reaction temperature is 620 DEG C, and reaction pressure is 0.1 kg/cm2, reaction velocity is 10 liters of ethylbenzene/liter catalyst hour. Change resistance potassium agent preparation method simultaneously.
Resistance potassium agent preparation is as follows: take 900 grams of aluminium oxidies and 500 grams of Ludox containing 20% (weight) silicon dioxide, mediates, extrusion, 120 DEG C of bakings 4 hours, 480 DEG C of roastings 8 hours, then 600 DEG C of roastings 4 hours.
The hydroxide reaction performance of embodiment 5 is in Table 1. The full-range selectivity of styrene of preparing styrene from ethylbenzene and styrene list are received in Table 2.
[embodiment 6]
With embodiment 1, being different in that in the preparation process of resistance potassium agent, calcination procedure is different. Resistance potassium agent preparation is following particularly as follows: take 50 grams of aluminium oxidies and 950 grams of silicon dioxide, mixing, extrusion, 120 DEG C dry 4 hours, 450 DEG C of roastings 5 hours.
Hydroxide reaction performance is in Table 1. The full-range selectivity of styrene of preparing styrene from ethylbenzene and styrene list are received in Table 2.
[embodiment 7]
With embodiment 1, being different in that in the preparation process of resistance potassium agent, calcination procedure is different. Resistance potassium agent preparation is following particularly as follows: take 50 grams of aluminium oxidies and 950 grams of silicon dioxide, mixing, extrusion, 120 DEG C dry 4 hours, 1500 DEG C of roastings 5 hours.
Hydroxide reaction performance is in Table 1. The full-range selectivity of styrene of preparing styrene from ethylbenzene and styrene list are received in Table 2.
[embodiment 8]
With embodiment 1, being different in that in the preparation process of resistance potassium agent, calcination procedure is different. Resistance potassium agent preparation is following particularly as follows: take 50 grams of aluminium oxidies and 950 grams of silicon dioxide, mixing, extrusion, 120 DEG C dry 4 hours, 1300 DEG C of roastings 5 hours.
Hydroxide reaction performance is in Table 1. The full-range selectivity of styrene of preparing styrene from ethylbenzene and styrene list are received in Table 2. Table 1
| Oxygen selectivity/% | Oxygen conversion/% | |
| Comparative example 1 | 77.12 | 99.31 |
| Embodiment 1 | 91.85 | 99.85 |
| Comparative example 2 | 79.12 | 99.33 |
| Comparative example 3 | 78.21 | 99.35 |
| Embodiment 2 | 91.92 | 100 |
| Embodiment 3 | 91.90 | 100 |
| Embodiment 4 | 91.93 | 100 |
| Embodiment 5 | 91.88 | 99.93 |
| Embodiment 6 | 88.65 | 99.75 |
| Embodiment 7 | 89.16 | 99.79 |
| Embodiment 8 | 89.21 | 99.81 |
Table 2
| Selectivity of styrene/% | Styrene list receipts/% | |
| Comparative example 1 | 88.2 | 68.2 |
| Embodiment 1 | 93.9 | 81.8 |
| Comparative example 2 | 89.1 | 69.2 |
| Comparative example 3 | 88.9 | 68.9 |
| Embodiment 2 | 94.1 | 82.2 |
| Embodiment 3 | 94.2 | 82.1 |
| Embodiment 4 | 94.3 | 82.1 |
| Embodiment 5 | 94.0 | 81.9 |
| Embodiment 6 | 92.6 | 80.7 |
| Embodiment 7 | 93.1 | 81.2 |
| Embodiment 8 | 93.0 | 81.0 |
Claims (10)
1., by the technique of preparing styrene from ethylbenzene, comprise the following steps:
(1) in the first dehydrogenation reaction operation, with water for diluent, raw material and the contact of the first dehydrogenation containing ethylbenzene occur ethylbenzene dehydrogenation reaction to generate containing ethylbenzene, hydrogen and cinnamic reaction logistics 1;
(2) reaction logistics 1 obtains reaction logistics 2 in de-potassium operation through contacting with resistance potassium agent;
(3) containing reaction logistics 2 and the material of oxygen in hydroxide reaction operation, contact with hydro-oxidation catalyst and carry out hydroxide reaction and reduce and react hydrogen content in logistics 2 and obtain logistics 3;
(4) logistics 3 contacts with the second dehydrogenation in the second dehydrogenation reaction operation and makes the further dehydrogenation of ethylbenzene generate logistics 4;
Described resistance potassium agent, in parts by weight, comprises aluminum a) in aluminium oxide 5～90 parts, and b) in the silicon of silicon dioxide 10～95 parts, and total number of aluminium oxide and silicon dioxide is 100; Described hydro-oxidation catalyst is noble metal system hydro-oxidation catalyst.
2. technique according to claim 1, is characterized in that the first dehydrogenation and/or the second dehydrogenation are Fe-K system catalyst for phenylethylene dehydrogenation.
3. technique according to claim 1, is characterized in that the reaction temperature of the first dehydrogenation reaction operation is 550～650 DEG C.
4. technique according to claim 2, is characterized in that the reaction temperature of the second dehydrogenation reaction operation is 550～650 DEG C.
5. technique according to claim 1, is characterized in that hydro-oxidation catalyst is loaded platinum catalyst.
6. technique according to claim 5, it is characterised in that the reaction temperature of hydroxide reaction operation is 500～700 DEG C.
7. technique according to claim 1, is characterized in that the temperature that reaction logistics 1 contacts with resistance potassium agent is 500～700 DEG C.
8. technique according to claim 1, is characterized in that consumption is the first dehydrogenation weight the 5～60% of resistance potassium agent.
9. technique according to claim 1, is characterized in that in parts by weight, and resistance potassium agent comprises a) aluminum in aluminium oxide 10～70 parts, b) in the silicon of silicon dioxide 30～90 parts.
10. technique according to claim 1, what it is characterized in that resistance potassium agent is shaped as cellular, and adjacent two nest locular wall thickness are 30～500 microns, the number of aperture of resistance potassium agent cross section be 3～150 holes/centimetre2。
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410670497.8A CN105669355A (en) | 2014-11-20 | 2014-11-20 | Process for preparation of styrene from ethylbenzene |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410670497.8A CN105669355A (en) | 2014-11-20 | 2014-11-20 | Process for preparation of styrene from ethylbenzene |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN105669355A true CN105669355A (en) | 2016-06-15 |
Family
ID=56957694
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201410670497.8A Pending CN105669355A (en) | 2014-11-20 | 2014-11-20 | Process for preparation of styrene from ethylbenzene |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN105669355A (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111704548A (en) * | 2020-05-20 | 2020-09-25 | 郑州师范学院 | Method for preparing nitroolefin from aryl ethane and nitrate |
| CN112717970A (en) * | 2019-10-14 | 2021-04-30 | 中国石油化工股份有限公司 | Process for dehydrogenating alkylaromatic hydrocarbons |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH01180045A (en) * | 1988-01-08 | 1989-07-18 | Fuji Xerox Co Ltd | Central processor |
| CN1704160A (en) * | 2004-05-28 | 2005-12-07 | 中国石油化工股份有限公司 | Catalyst for hydrogen oxidation reaction in ethylbenzene dehydrogenation process |
| JP2007016027A (en) * | 2005-06-10 | 2007-01-25 | Mitsubishi Chemicals Corp | Method for producing styrene |
| CN103626623A (en) * | 2012-08-23 | 2014-03-12 | 中国石油天然气股份有限公司 | Ethylbenzene dehydrogenation-hydrogen selective oxidation method used for producing styrene |
-
2014
- 2014-11-20 CN CN201410670497.8A patent/CN105669355A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH01180045A (en) * | 1988-01-08 | 1989-07-18 | Fuji Xerox Co Ltd | Central processor |
| CN1704160A (en) * | 2004-05-28 | 2005-12-07 | 中国石油化工股份有限公司 | Catalyst for hydrogen oxidation reaction in ethylbenzene dehydrogenation process |
| JP2007016027A (en) * | 2005-06-10 | 2007-01-25 | Mitsubishi Chemicals Corp | Method for producing styrene |
| CN103626623A (en) * | 2012-08-23 | 2014-03-12 | 中国石油天然气股份有限公司 | Ethylbenzene dehydrogenation-hydrogen selective oxidation method used for producing styrene |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112717970A (en) * | 2019-10-14 | 2021-04-30 | 中国石油化工股份有限公司 | Process for dehydrogenating alkylaromatic hydrocarbons |
| CN112717970B (en) * | 2019-10-14 | 2023-08-08 | 中国石油化工股份有限公司 | Method for dehydrogenating alkyl aromatic hydrocarbon |
| CN111704548A (en) * | 2020-05-20 | 2020-09-25 | 郑州师范学院 | Method for preparing nitroolefin from aryl ethane and nitrate |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102259007A (en) | Method for preparing mercury-free catalyst for synthesis of chloroethylene by acetylene process | |
| CN105251486A (en) | Supported platinum group catalyst applied to propane dehydrogenation propylene preparation and preparation method of supported platinum group catalyst | |
| CN105032503B (en) | A kind of renovation process of noble metal catalyst | |
| CN104945262A (en) | Method for preparing prepare methyl nitrite by catalyzing methanol to reduce dilute nitric acid | |
| CN106582629B (en) | A kind of catalyst of preparing propylene by dehydrogenating propane and its preparation method and application | |
| CN105669355A (en) | Process for preparation of styrene from ethylbenzene | |
| CN111468101A (en) | Chromium-based catalyst and preparation method and application thereof | |
| CN105214697B (en) | A kind of low paraffin dehydrogenation alkene catalyst and preparation method | |
| CN103191758A (en) | Pt-Cu catalyst for acetylene hydrochlorination, and preparation method of same | |
| CN103058809A (en) | Method for preparing low-carbon alkenes by low-carbon alkane dehydrogenation | |
| CN103224591B (en) | Bimetallic catalytic hydrogenation method of nitrile rubber | |
| CN101491759A (en) | Catalyst for hydrogen selective catalytic combustion reaction in ethyl benzene dehydrogenation process | |
| CN105646125B (en) | Ethylbenzene dehydrogenation hydroxide reaction technique | |
| CN103537292A (en) | Dehydrogenation catalyst used for preparing styrene | |
| CN106881084B (en) | One kind is for reverse water-gas-shift reaction noble metal catalyst and its preparation and application | |
| CN103910342A (en) | Nitrogen purification device | |
| CN100352544C (en) | Catalyst used for methanol oxidation oxidizing and reforming hydrogen production and preparation method thereof | |
| CN105664904B (en) | Hinder the preparation method of potassium agent | |
| CN105622318A (en) | Heterotype potassium retarder used for ethylbenzene dehydrogenation-hydrogen oxidation reaction | |
| CN102218314B (en) | Hydrogen selective oxidation catalyst used in the propane dehydrogenation process and preparation method thereof | |
| JP6300281B2 (en) | Method for producing conjugated diene and reaction apparatus | |
| CN103331179B (en) | Catalyst used for synthesizing methyl chloride by gas-solid phase reaction and preparation method thereof | |
| CN100408167C (en) | Catalyst for ethylbenzene dehydrogenation-hydroxide reaction | |
| CN103030496B (en) | Method of selective oxidation of hydrogen in propane dehydrogenation process | |
| CN202621125U (en) | High-pressure reaction unit |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| RJ01 | Rejection of invention patent application after publication | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20160615 |