Catalysis Communications, Volume 31, 10 January 2013, Pages 76–80
Oxidative dehydrogenation of 1-butene to
1,3-butadiene over BiFe0.65NixMo oxide catalysts: Effect
of nickel content
Jung-Hyun Park (a), Kyoungho Row (b), Chae-Ho
Shin (a)
a Department of Chemical Engineering, Chungbuk National University, Chungbuk
361-763, Republic of Korea
b Process Solution Team, Kumho Petrochemical R&BD Center, Daejeon 305-348,
Republic of Korea
Abstract
Researchers fabricated BiFe0.65NixMo
oxide catalysts (x = 0–0.2) for the oxidative
dehydrogenation of butenes to 1,3-butadiene. Temperature programmed reoxidation
(TPRO) measurements showed that catalytic activity was closely linked to oxygen
mobility.
Surface modification by
small amounts of nickel addition is favorable in this reaction. Of the
catalysts in this study, BiFe0.65Ni0.05Mo oxide catalyst
showed the highest conversion and BD yield due to high oxygen mobility. The
catalyst is quite stable. No deactivation during the 100 h reaction was observed.
Full Text Source (Subscription or Fee): http://www.sciencedirect.com/science/article/pii/S1566736712004396
Wednesday, April 23, 2014
Production of high purity butene-1 from C4 olefins/paraffins mixed gas (Korea Institute Of Energy Research)
PATENT
Production of high purity butene-1 from C4 olefins/paraffins mixed gas (Korea Institute Of Energy Research)
Publication number US8431762 B2
Application number US 12/593,252
Publication date Apr 30, 2013
CN101657396A
Inventors
Jong-Ho Park, 8 More »
Original Assignee
Korea Institute Of Energy Research, Sk Energy Co., Ltd
Abstract
The present invention relates to a hybrid process comprising an adsorption process and a distillation process for the separation of butene-1 from a C4 hydrocarbon mixture gas including butene-1, trans-2-butene, cis-2-butene, normal butane, isobutane, etc. The above hybrid process comprises introducing a gaseous C4 mixture into the adsorption tower loaded with adsorbents which adsorb olefins selectively to discharge C4 paraffins to the outlet of the tower, desorbing C4 olefins selectively adsorbed in the adsorption tower to produce high purity C4 olefins mixture gas in which isobutane and normal butane was removed, and separating the high C4 olefins mixture gas (a mixture of butene-1, trans-2-butene, cis-2-butene, and a trace amount of C4 paraffins) via distillation to obtain high purity butene-1 including a trace amount of isobutane in the top of the distillation tower and obtain a mixture gas including trans-2-butene, cis-2-butene and a trace amount of normal butane in the bottom of the tower.
Description
TECHNICAL FIELD
The present invention relates to a method and its apparatus for the separation of butene-1 from a C4 hydrocarbon mixed gas including butene-1, trans-2-butene, cis-2-butene, normal butane, isobutane, etc. by using a hybrid process composed of an adsorption process and a distillation process.
BACKGROUND ART
The known method for the separation of butene-1 from a C4 hydrocarbon mixed gas including C4 olefins (butene-1, trans-2-butene, cis-2-butene, et.) and C4 paraffins (normal butane, isobutane, etc.) involves mainly a distillation process. However, the known method requires the use of distillation towers with a large number of fractionation plates due to the small boiling-point difference of the products to be separated and thus leads to high consumption of energy and to high investment costs.
U.S. Pat. No. 4,718,986 (1988) discloses a process for producing butene-1 of more than 99 wt % from the C4 hydrocarbon mixture of butene-1/isobutane/normal butane/butene-2 by using two distillation towers. According to the above patent invention, the C4 mixture is introduced into the first distillation tower to remove isobutane from the top of the tower. The lower stream from the first distillation tower is introduced into the second distillation tower, obtaining butene-1 with a purity of 99 wt % from the top of the second tower and discharging a mixture of normal butane, butene-2 and butene-1 from the bottom of the second tower. However, since a considerable amount of butene-1 is discharged with the isobutane stream from the top of the first tower and also with the mixture of normal butane, butene-2 and butene-1 from the bottom of the second tower, the above process results in much loss of butene-1.
There are a number of known techniques relating to the adsorption-separation processes for a C4 hydrocarbon mixture, for example, a technique for separating butene-1 from a mixture including butene-1/butene-2/isobutylene by using type X or Y zeolite containing potassium ion or barium ion (U.S. Pat. No. 3,723,561, Mar. 27, 1973), a technique for separating butene-1 from a liquid C4 hydrocarbon mixture by using type K-X zeolite (U.S. Pat. No. 4,119,678, Oct. 10, 1978), a technique for separating normal C4 hydrocarbon mixture and isobutylene by using a molecular sieve selective to normal C4 hydrocarbon mixture (U.S. Pat. No. 4,455,445, Jun. 19, 1984), a technique for selectively separating alfa olefin alone from olefins having more than 4 carbon atoms by a liquid adsorption process using a zeolite molecular sieve (U.S. Pat. No. 5,132,485, 1992), a pressure-swing adsorption process for the separation of olefins/paraffins having 2-6 carbon atoms in vapor phase by using type 4A zeolite (U.S. Pat. No. 5,365,011, 1994), and a technique for separating paraffins from a mixture of olefins/paraffins having 2-6 carbon atoms in vapor phase using type X or Y zeolite and reproducing the adsorbents used in the adsorption process by using desorbents (EP 0708070 B1, 1999). The U.S. Pat. No. 5,955,640 (1999) discloses a process of improving the yield of butene-1 by converting butene-2 components into butene-1 while removing a portion of paraffin components by using an adsorption process in order to prevent the accumulation of unreacted paraffin components in the process.
However, distillation using two towers connected in series as shown in the above U.S. Pat. No. 4,718,986 (1998) is the only process used for obtaining butene-1 with high purity from the C4 olefins/paraffins mixture gas. Till now, there is no adsorptive-separation techniques that can separate butene-1 with high purity from a mixture of C4 olefins/paraffins by selectively separating C4 olefin mixture gas from C4 olefins/paraffins mixture by an adsorption process and then obtaining high purity butene-1 from C4 olefin mixture gas selectively separated from the adsorption process by a distillation process, as can be achieved by the present invention.
DISCLOSURE OF INVENTION Technical Problem
The existing distillation processes for separating betene-1 from a mixture of olefins/paraffins use two sequential distillation towers to remove isobutane from the first distillation and obtain high purity butene-1 from the second distillation tower. However, a significant amount of butene-1 is discharged together with a isobutane stream to the top of the first tower and also discharged to the bottom of the second distillation tower and thus butene-1 loss is large. In addition, since the difference in relative volatilities among C4 components is small, the above distillation processes require high consumption of energy and high investment costs.
Technical Solution
In the above circumstance, the inventors of the present invention have designed a hybrid process of removing paraffins by the C4 olefins/paraffins adsorption separation process and thereafter separating the C4 olefins via distillation to obtain high purity butene-1.
If olefins are selectively separated from the C4 olefins/paraffins mixture gas by using the adsorption separation process, the paraffin components are selectively removed, butene-1 loss which is accompanied at the time of removing isobutane can be reduced, also the concentration of the normal butane in the gas introduced into the distillation process for the production of high purity butene-1 is lowered, and thus the production of butene-1 is easy and the yield of butene-1 in the whole process increases.
Advantageous Effects
The present invention can reduce the butene-1 loss and investment costs over the process consisted only of multi-stage distillation tower by using a hybrid process consisted of a olefins/paraffins adsorption separation process and a olefin distillation process.
Now, some embodiments of the present invention are illustrated with reference to the drawings accompanied. However, it is understood that the illustrated embodiments of the present invention are intended to be examples only and the invention is not limited to any embodiments.
Free Full Text Source: http://www.google.com/patents/US8431762
Production of high purity butene-1 from C4 olefins/paraffins mixed gas (Korea Institute Of Energy Research)
Publication number US8431762 B2
Application number US 12/593,252
Publication date Apr 30, 2013
CN101657396A
Inventors
Jong-Ho Park, 8 More »
Original Assignee
Korea Institute Of Energy Research, Sk Energy Co., Ltd
Abstract
The present invention relates to a hybrid process comprising an adsorption process and a distillation process for the separation of butene-1 from a C4 hydrocarbon mixture gas including butene-1, trans-2-butene, cis-2-butene, normal butane, isobutane, etc. The above hybrid process comprises introducing a gaseous C4 mixture into the adsorption tower loaded with adsorbents which adsorb olefins selectively to discharge C4 paraffins to the outlet of the tower, desorbing C4 olefins selectively adsorbed in the adsorption tower to produce high purity C4 olefins mixture gas in which isobutane and normal butane was removed, and separating the high C4 olefins mixture gas (a mixture of butene-1, trans-2-butene, cis-2-butene, and a trace amount of C4 paraffins) via distillation to obtain high purity butene-1 including a trace amount of isobutane in the top of the distillation tower and obtain a mixture gas including trans-2-butene, cis-2-butene and a trace amount of normal butane in the bottom of the tower.
Description
TECHNICAL FIELD
The present invention relates to a method and its apparatus for the separation of butene-1 from a C4 hydrocarbon mixed gas including butene-1, trans-2-butene, cis-2-butene, normal butane, isobutane, etc. by using a hybrid process composed of an adsorption process and a distillation process.
BACKGROUND ART
The known method for the separation of butene-1 from a C4 hydrocarbon mixed gas including C4 olefins (butene-1, trans-2-butene, cis-2-butene, et.) and C4 paraffins (normal butane, isobutane, etc.) involves mainly a distillation process. However, the known method requires the use of distillation towers with a large number of fractionation plates due to the small boiling-point difference of the products to be separated and thus leads to high consumption of energy and to high investment costs.
U.S. Pat. No. 4,718,986 (1988) discloses a process for producing butene-1 of more than 99 wt % from the C4 hydrocarbon mixture of butene-1/isobutane/normal butane/butene-2 by using two distillation towers. According to the above patent invention, the C4 mixture is introduced into the first distillation tower to remove isobutane from the top of the tower. The lower stream from the first distillation tower is introduced into the second distillation tower, obtaining butene-1 with a purity of 99 wt % from the top of the second tower and discharging a mixture of normal butane, butene-2 and butene-1 from the bottom of the second tower. However, since a considerable amount of butene-1 is discharged with the isobutane stream from the top of the first tower and also with the mixture of normal butane, butene-2 and butene-1 from the bottom of the second tower, the above process results in much loss of butene-1.
There are a number of known techniques relating to the adsorption-separation processes for a C4 hydrocarbon mixture, for example, a technique for separating butene-1 from a mixture including butene-1/butene-2/isobutylene by using type X or Y zeolite containing potassium ion or barium ion (U.S. Pat. No. 3,723,561, Mar. 27, 1973), a technique for separating butene-1 from a liquid C4 hydrocarbon mixture by using type K-X zeolite (U.S. Pat. No. 4,119,678, Oct. 10, 1978), a technique for separating normal C4 hydrocarbon mixture and isobutylene by using a molecular sieve selective to normal C4 hydrocarbon mixture (U.S. Pat. No. 4,455,445, Jun. 19, 1984), a technique for selectively separating alfa olefin alone from olefins having more than 4 carbon atoms by a liquid adsorption process using a zeolite molecular sieve (U.S. Pat. No. 5,132,485, 1992), a pressure-swing adsorption process for the separation of olefins/paraffins having 2-6 carbon atoms in vapor phase by using type 4A zeolite (U.S. Pat. No. 5,365,011, 1994), and a technique for separating paraffins from a mixture of olefins/paraffins having 2-6 carbon atoms in vapor phase using type X or Y zeolite and reproducing the adsorbents used in the adsorption process by using desorbents (EP 0708070 B1, 1999). The U.S. Pat. No. 5,955,640 (1999) discloses a process of improving the yield of butene-1 by converting butene-2 components into butene-1 while removing a portion of paraffin components by using an adsorption process in order to prevent the accumulation of unreacted paraffin components in the process.
However, distillation using two towers connected in series as shown in the above U.S. Pat. No. 4,718,986 (1998) is the only process used for obtaining butene-1 with high purity from the C4 olefins/paraffins mixture gas. Till now, there is no adsorptive-separation techniques that can separate butene-1 with high purity from a mixture of C4 olefins/paraffins by selectively separating C4 olefin mixture gas from C4 olefins/paraffins mixture by an adsorption process and then obtaining high purity butene-1 from C4 olefin mixture gas selectively separated from the adsorption process by a distillation process, as can be achieved by the present invention.
DISCLOSURE OF INVENTION Technical Problem
The existing distillation processes for separating betene-1 from a mixture of olefins/paraffins use two sequential distillation towers to remove isobutane from the first distillation and obtain high purity butene-1 from the second distillation tower. However, a significant amount of butene-1 is discharged together with a isobutane stream to the top of the first tower and also discharged to the bottom of the second distillation tower and thus butene-1 loss is large. In addition, since the difference in relative volatilities among C4 components is small, the above distillation processes require high consumption of energy and high investment costs.
Technical Solution
In the above circumstance, the inventors of the present invention have designed a hybrid process of removing paraffins by the C4 olefins/paraffins adsorption separation process and thereafter separating the C4 olefins via distillation to obtain high purity butene-1.
If olefins are selectively separated from the C4 olefins/paraffins mixture gas by using the adsorption separation process, the paraffin components are selectively removed, butene-1 loss which is accompanied at the time of removing isobutane can be reduced, also the concentration of the normal butane in the gas introduced into the distillation process for the production of high purity butene-1 is lowered, and thus the production of butene-1 is easy and the yield of butene-1 in the whole process increases.
Advantageous Effects
The present invention can reduce the butene-1 loss and investment costs over the process consisted only of multi-stage distillation tower by using a hybrid process consisted of a olefins/paraffins adsorption separation process and a olefin distillation process.
Now, some embodiments of the present invention are illustrated with reference to the drawings accompanied. However, it is understood that the illustrated embodiments of the present invention are intended to be examples only and the invention is not limited to any embodiments.
Free Full Text Source: http://www.google.com/patents/US8431762
Tuesday, April 22, 2014
Catalytic synthesis of propylene carbonate from propylene oxide and carbon dioxide in the presence of rhodium complexes modified with organophosphorus ligands and chitosan
Petroleum Chemistry, November 2013, Volume 53, Issue 6, pp 412-417
Catalytic synthesis of propylene carbonate from propylene oxide and carbon dioxide in the presence of rhodium complexes modified with organophosphorus ligands and chitosan
I. G. Korosteleva, N. A. Markova, N. V. Kolesnichenko, N. N. Ezhova, S. N. Khadzhiev, N. I. Trukhmanova
Topchiev Institute of Petrochemical Synthesis, Russian Academy of Sciences, Moscow, Russia
Abstract
Reports a study of the reaction between CO2 and propylene oxide to produce propylene carbonate in the presence of rhodium complexes modified with organophosphorus ligands and chitosan. Highly effective catalysts mediating the reaction with almost a 100% yield and 100% selectivity were fabricated using rhodium compounds modified with triphenylphosphine and chitosan.
Full Text Source (Subscription or Fee): http://link.springer.com/article/10.1134/S0965544113060108#
Catalytic synthesis of propylene carbonate from propylene oxide and carbon dioxide in the presence of rhodium complexes modified with organophosphorus ligands and chitosan
I. G. Korosteleva, N. A. Markova, N. V. Kolesnichenko, N. N. Ezhova, S. N. Khadzhiev, N. I. Trukhmanova
Topchiev Institute of Petrochemical Synthesis, Russian Academy of Sciences, Moscow, Russia
Abstract
Reports a study of the reaction between CO2 and propylene oxide to produce propylene carbonate in the presence of rhodium complexes modified with organophosphorus ligands and chitosan. Highly effective catalysts mediating the reaction with almost a 100% yield and 100% selectivity were fabricated using rhodium compounds modified with triphenylphosphine and chitosan.
Full Text Source (Subscription or Fee): http://link.springer.com/article/10.1134/S0965544113060108#
Dynamic simulation – A new tool for process engineers
Chemical Technology, March 2013
Dynamic simulation – A new tool for process engineers
Kevin Brooks , BluESP, Johannesburg, South Africa
Abstract
Steady-state simulation of process plants has been a key tool in process design and operation for many years, with a number of sophisticated products available in the market place. The use of dynamic simulation is less widespread, with applications tending to be limited to specific areas of the process or to specific fields such as process control.
A possible reason for this has been that large scope dynamic simulations are very computer intensive, leading to less than real-time execution. With the modern computing power available this is no longer likely to be a constraint. This article discusses the application of dynamic simulation to important plant issues such as:
Hazop studies
Sizing of relief equipment
Start-up and shut-down procedures
Trip scenarios in multi-train plants
Base level and advanced process control.
The extra information required for dynamic simulation is described, and the extra effort evaluated. This allows for the trade-off with the benefits achieved to be quantified.
Figure 1 shows a simplified flowsheet for propylene glycol production, and Figure 2 shows the same flowsheet adapted for dynamic simulation. In this case the software recommended the addition of the various valves; the simulation engineer added the control system and the holdup data.
Free Full Text Source: http://bluesp.co.za/downloads/ChemTech%2013%20Mar%2012-14%20CIE%2001.pdf
Dynamic simulation – A new tool for process engineers
Kevin Brooks , BluESP, Johannesburg, South Africa
Abstract
Steady-state simulation of process plants has been a key tool in process design and operation for many years, with a number of sophisticated products available in the market place. The use of dynamic simulation is less widespread, with applications tending to be limited to specific areas of the process or to specific fields such as process control.
A possible reason for this has been that large scope dynamic simulations are very computer intensive, leading to less than real-time execution. With the modern computing power available this is no longer likely to be a constraint. This article discusses the application of dynamic simulation to important plant issues such as:
Hazop studies
Sizing of relief equipment
Start-up and shut-down procedures
Trip scenarios in multi-train plants
Base level and advanced process control.
The extra information required for dynamic simulation is described, and the extra effort evaluated. This allows for the trade-off with the benefits achieved to be quantified.
Figure 1 shows a simplified flowsheet for propylene glycol production, and Figure 2 shows the same flowsheet adapted for dynamic simulation. In this case the software recommended the addition of the various valves; the simulation engineer added the control system and the holdup data.
Free Full Text Source: http://bluesp.co.za/downloads/ChemTech%2013%20Mar%2012-14%20CIE%2001.pdf
Effect of Nano-sized TiO2 Additional Support in WO3/SiO2 Catalyst Systems on Metathesis of Ethylene and Trans-2-Butene to Propylene
Catalysis Letters, September 2013, Volume 143, Issue 9, pp 919-925
Effect of Nano-sized TiO2 Additional Support in WO3/SiO2 Catalyst Systems on Metathesis of Ethylene and Trans-2-Butene to Propylene
Wimonrat Limsangkass, Suphot Phatanasri, Piyasan Praserthdam, Joongjai Panpranot, Wuttithep Jareewatchara, Sirachaya Kunjara Na Ayudhya, Kongkiat Suriye
1. Center of Excellence on Catalysis and Catalytic Reaction Engineering, Department of Chemical Engineering, Faculty of Engineering, Chulalongkorn University, Bangkok, 10330, Thailand
2. SCG Chemicals, Co., Ltd., 1 Siam Cement Road, Bangsue, Bangkok, 10800, Thailand
Abstract
Researchers used TiO2 as an additional support by physically mixing it with the WO3/SiO2 catalysts. This was used in the metathesis of ethylene and trans-2-butene for propylene production. Having nano-sized TiO2 as the additional support could enhance trans-2-butene conversion and propylene yield.
Results indicated that tungsten could migrate from an original support and form more well-dispersed surface tetrahedral tungsten oxide species on the additional support, leading to a better dispersion. Results also revealed that TiO2 having nano size could provide better spreading of the tungsten species than the micro size. The study offers guidance in supplementing existing catalysts as a simple way to improve catalytic performance.
Full Text Source (Subscription or Fee): http://link.springer.com/article/10.1007/s10562-013-1074-7#
Effect of Nano-sized TiO2 Additional Support in WO3/SiO2 Catalyst Systems on Metathesis of Ethylene and Trans-2-Butene to Propylene
Wimonrat Limsangkass, Suphot Phatanasri, Piyasan Praserthdam, Joongjai Panpranot, Wuttithep Jareewatchara, Sirachaya Kunjara Na Ayudhya, Kongkiat Suriye
1. Center of Excellence on Catalysis and Catalytic Reaction Engineering, Department of Chemical Engineering, Faculty of Engineering, Chulalongkorn University, Bangkok, 10330, Thailand
2. SCG Chemicals, Co., Ltd., 1 Siam Cement Road, Bangsue, Bangkok, 10800, Thailand
Abstract
Researchers used TiO2 as an additional support by physically mixing it with the WO3/SiO2 catalysts. This was used in the metathesis of ethylene and trans-2-butene for propylene production. Having nano-sized TiO2 as the additional support could enhance trans-2-butene conversion and propylene yield.
Results indicated that tungsten could migrate from an original support and form more well-dispersed surface tetrahedral tungsten oxide species on the additional support, leading to a better dispersion. Results also revealed that TiO2 having nano size could provide better spreading of the tungsten species than the micro size. The study offers guidance in supplementing existing catalysts as a simple way to improve catalytic performance.
Full Text Source (Subscription or Fee): http://link.springer.com/article/10.1007/s10562-013-1074-7#
Direct Transformation of Ethylene into Propylene on H-SSZ-13
Sixth
Asia-Pacific Congress on Catalysis (APCAT-6), Taipei, Taiwan, October 13-17,
2013
Direct Transformation of Ethylene into Propylene on H-SSZ-13
Weili Dai, Bo Tang, Guangjun Wu, Landong Li*, Naijia Guan, Michael Hunger
Key Laboratory of Advanced Energy Materials Chemistry (Ministry of Education), College of Chemistry, Nankai University, Tianjin, 300071, P.R.China.
lild@nankai.edu.cn
Abstract
Ethene is selectively converted to propylene over H-SSZ-13 at 673 K with a yield of 52.8% and selectivity of 64.8% at ethylene conversion of 81.5%. After dealuminzation, the lifetime with high propylene yield can be obtained up to 7 h in fixed-bed flow reactor.
Introduction
Propylene is one of the most important chemicals for the production of polypropylene, acrylonitrile, and propylene oxide. In the current chemical industry, propylene is mainly produced as a coproduct of ethylene via steam cracking of naphtha.
Because the demand for propylene is growing much faster than that for ethylene, due to higher needs for propylene derivatives such as polypropylene and propylene oxide, the development of other routes for propylene production has become urgent. A more sustainable route for the production of propene would be the conversion of biomass to propene using ethanol as a feedstock, which can be easily transferred to ethene. The challenging step would be the reaction from ethene directly to propene. The phenomenon of propylene formation from ethylene was observed in a few early papers on some catalysts, but the activity was quite low.
In the present study, HSSZ-13 zeolite with strong acid sites and 8-membered ring windows was studied as the ETP catalyst. As in our previous reports, the intermediate species formed during the ethylene conversion on the catalysts were monitored by in situ UV/Vis and FTIR spectroscopy. Furthermore, catalyst samples were quenched after the ETP reaction and taken from the fixed-bed reactor for GC-MS and 1H solid-state NMR studies.
Free Full Text Source: http://guan.nankai.edu.cn/pdf/2013/20131023165023855.pdf
Direct Transformation of Ethylene into Propylene on H-SSZ-13
Weili Dai, Bo Tang, Guangjun Wu, Landong Li*, Naijia Guan, Michael Hunger
Key Laboratory of Advanced Energy Materials Chemistry (Ministry of Education), College of Chemistry, Nankai University, Tianjin, 300071, P.R.China.
lild@nankai.edu.cn
Abstract
Ethene is selectively converted to propylene over H-SSZ-13 at 673 K with a yield of 52.8% and selectivity of 64.8% at ethylene conversion of 81.5%. After dealuminzation, the lifetime with high propylene yield can be obtained up to 7 h in fixed-bed flow reactor.
Introduction
Propylene is one of the most important chemicals for the production of polypropylene, acrylonitrile, and propylene oxide. In the current chemical industry, propylene is mainly produced as a coproduct of ethylene via steam cracking of naphtha.
Because the demand for propylene is growing much faster than that for ethylene, due to higher needs for propylene derivatives such as polypropylene and propylene oxide, the development of other routes for propylene production has become urgent. A more sustainable route for the production of propene would be the conversion of biomass to propene using ethanol as a feedstock, which can be easily transferred to ethene. The challenging step would be the reaction from ethene directly to propene. The phenomenon of propylene formation from ethylene was observed in a few early papers on some catalysts, but the activity was quite low.
In the present study, HSSZ-13 zeolite with strong acid sites and 8-membered ring windows was studied as the ETP catalyst. As in our previous reports, the intermediate species formed during the ethylene conversion on the catalysts were monitored by in situ UV/Vis and FTIR spectroscopy. Furthermore, catalyst samples were quenched after the ETP reaction and taken from the fixed-bed reactor for GC-MS and 1H solid-state NMR studies.
Free Full Text Source: http://guan.nankai.edu.cn/pdf/2013/20131023165023855.pdf
Catalyst for oxidative dehydrogenation of propane to propylene (King Fahd University Of Petroleum And Minerals)
PATENT
Catalyst for oxidative dehydrogenation of propane to propylene (King Fahd University Of Petroleum And Minerals)
Publication number US8609568 B2
Application number US 12/897,686
Publication date Dec 17, 2013
Inventors
Shakeel Ahmed, Faizur Rahman, Uwais Baduruthamal
Original Assignee
King Fahd University Of Petroleum And Minerals
Abstract
The catalyst for oxidative dehydrogenation of propane to propylene includes vanadium and aluminum incorporated into the framework of a mesoporous support, viz., MCM-41, to form V—Al-MCM-41, and nickel impregnated onto the walls of the mesoporous support. Nickel loading is preferably in the range of 5 to 15% by weight of the catalyst. A process for the production of propylene from propane includes steps of placing the catalyst in a fixed bed reactor, introducing a flow of feedstock in a propane:oxygen:nitrogen ratio of about 6:6:88 by volume, maintaining the reactor at atmospheric pressure and in a temperature range of about 400 to 550° C., collecting the product, and separating propylene from the product. The process achieves propane conversion between about 6 to 22%, and a selectivity for propylene between about 22 and 70%, depending upon percent nickel content and temperature of the reaction.
BACKGROUND OF THE INVENTION
1. Field of the Invention
The present invention relates to catalysts for converting alkanes to alkenes, and particularly to a catalyst for the oxidative dehydrogenation of propane to propylene.
2. Description of the Related Art
Propylene is a commercially valuable product. The reactivity of the allylic carbon makes propylene useful for the production of polypropylene, acrylonitrile, propylene oxide, propylene glycol, cumene, and other products, which are useful as final products and as intermediates in the synthesis or production of other commodities.
The majority of propylene is produced by steam hydrocracking of crude petroleum, or by distillation. However, such processes are not highly selective or produce propylene in low yield. Recently, there has been renewed interest in oxidative dehydrogenation of propane for the production of propylene. Oxidative dehydrogenation is attractive because it can be accomplished at lower temperatures than cracking or distillation processes, thereby avoiding complications and expense resulting from coking of the catalyst. Nevertheless, oxidative dehydrogenation is not currently used for the production of propylene, largely due to low yields and lack of selectivity of the currently known catalysts.
Thus, a catalyst for oxidative dehydrogenation of propane to propylene solving the aforementioned problems is desired.
SUMMARY OF THE INVENTION
The catalyst for oxidative dehydrogenation of propane to propylene includes vanadium and aluminum incorporated into the framework of a mesoporous support, viz., MCM-41, to form V—Al-MCM-41, and nickel impregnated onto the walls of the mesoporous support. Nickel loading is preferably in the range of 5 to 15% by weight of the catalyst. A process for the production of propylene from propane includes steps of placing the catalyst in a fixed bed reactor, introducing a flow of feedstock in a propane:oxygen:nitrogen ratio of about 6:6:88 by volume, maintaining the reactor at atmospheric pressure and in a temperature range of about 400 to 550° C., collecting the product, and separating propylene from the product. The process achieves propane conversion between about 6 to 22%, and a selectivity for propylene between about 22 and 70%, depending upon percent nickel content and temperature of the reaction.
These and other features of the present invention will become readily apparent upon further review of the following specification and drawings.
Free Full Text Source: http://www.google.com/patents/US8609568
Catalyst for oxidative dehydrogenation of propane to propylene (King Fahd University Of Petroleum And Minerals)
Publication number US8609568 B2
Application number US 12/897,686
Publication date Dec 17, 2013
Inventors
Shakeel Ahmed, Faizur Rahman, Uwais Baduruthamal
Original Assignee
King Fahd University Of Petroleum And Minerals
Abstract
The catalyst for oxidative dehydrogenation of propane to propylene includes vanadium and aluminum incorporated into the framework of a mesoporous support, viz., MCM-41, to form V—Al-MCM-41, and nickel impregnated onto the walls of the mesoporous support. Nickel loading is preferably in the range of 5 to 15% by weight of the catalyst. A process for the production of propylene from propane includes steps of placing the catalyst in a fixed bed reactor, introducing a flow of feedstock in a propane:oxygen:nitrogen ratio of about 6:6:88 by volume, maintaining the reactor at atmospheric pressure and in a temperature range of about 400 to 550° C., collecting the product, and separating propylene from the product. The process achieves propane conversion between about 6 to 22%, and a selectivity for propylene between about 22 and 70%, depending upon percent nickel content and temperature of the reaction.
BACKGROUND OF THE INVENTION
1. Field of the Invention
The present invention relates to catalysts for converting alkanes to alkenes, and particularly to a catalyst for the oxidative dehydrogenation of propane to propylene.
2. Description of the Related Art
Propylene is a commercially valuable product. The reactivity of the allylic carbon makes propylene useful for the production of polypropylene, acrylonitrile, propylene oxide, propylene glycol, cumene, and other products, which are useful as final products and as intermediates in the synthesis or production of other commodities.
The majority of propylene is produced by steam hydrocracking of crude petroleum, or by distillation. However, such processes are not highly selective or produce propylene in low yield. Recently, there has been renewed interest in oxidative dehydrogenation of propane for the production of propylene. Oxidative dehydrogenation is attractive because it can be accomplished at lower temperatures than cracking or distillation processes, thereby avoiding complications and expense resulting from coking of the catalyst. Nevertheless, oxidative dehydrogenation is not currently used for the production of propylene, largely due to low yields and lack of selectivity of the currently known catalysts.
Thus, a catalyst for oxidative dehydrogenation of propane to propylene solving the aforementioned problems is desired.
SUMMARY OF THE INVENTION
The catalyst for oxidative dehydrogenation of propane to propylene includes vanadium and aluminum incorporated into the framework of a mesoporous support, viz., MCM-41, to form V—Al-MCM-41, and nickel impregnated onto the walls of the mesoporous support. Nickel loading is preferably in the range of 5 to 15% by weight of the catalyst. A process for the production of propylene from propane includes steps of placing the catalyst in a fixed bed reactor, introducing a flow of feedstock in a propane:oxygen:nitrogen ratio of about 6:6:88 by volume, maintaining the reactor at atmospheric pressure and in a temperature range of about 400 to 550° C., collecting the product, and separating propylene from the product. The process achieves propane conversion between about 6 to 22%, and a selectivity for propylene between about 22 and 70%, depending upon percent nickel content and temperature of the reaction.
These and other features of the present invention will become readily apparent upon further review of the following specification and drawings.
Free Full Text Source: http://www.google.com/patents/US8609568
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