but-2-ene

Conditions: temp:0.00; pressure:0.00; stir:

Conditions: temp:0.00; pressure:0.00; stir:; See reaction.notes.procedure_details.

Procedure: In a first reactor R1, 1-butene, 2-butene and isobutene are reacted in the presence of the metathesis catalyst of the present invention to give propene, 2-pentene and 2-methyl-2-butene. For this purpose, a raffinate I stream is fed to the reactor. The reactor is followed by a distillation column D1 at the top of which propene and ethene formed as by-product are removed. Unreacted raffinate I is taken off at the middle offtake. Some of it may: also be returned to the reactor R1 (not shown in FIG. 1). 2-Pentene, 2-methyl-2-butene and 3-hexene formed as by-product as well as high boilers are taken off at the bottom of D1. The bottoms are then fed together with added ethene to a reactor R2 which again contains a metathesis catalyst of the present invention. In this reactor R2, the reaction of 2-pentene and 2-methyl-2-butene with ethene to give 1-butene, isobutene and propene takes place. The reaction product from reactor R2 is fed to a distillation column D2 at the top of which propene and unreacted ethene are taken off. 1-Butene and isobutene formed are taken off at the middle offtake and at least sore is preferably returned to the reactor R1. Unreacted 2-pentene, 2-methyl-2-butene and also, as by-products, 3-hexene and high boilers are obtained at the bottom of D2. These are preferably returned to the reactor R2. The mixtures of propene and by-product ethene taken off at the top of D1 and D2 are fractionated in a further distillation column D3. Ethene is obtained at the top of D3 and this is preferably returned to the reactor R2 (not shown in FIG. 1), or discharged as co-cracker feed. The propene obtained at the bottom of D3 is the desired reaction product of the process of the present invention. D1 and D2 are designed such that a low-boiling phase, in particular a C2/3 phase comprising ethene and propene, is taken off at the top of the column. C4 streams, in particular butenes and butanes, are taken off as intermediate-boiling phase. As bottoms, C≧5-hydrocarbons are discharged.

Conditions: temp:0.00; pressure:0.00; stir:; See reaction.notes.procedure_details.

Procedure: In a first reactor R1, 1-butene, 2-butene and isobutene are reacted in the presence of the metathesis catalyst of the present invention to give propene, 2-pentene and 2-methyl-2-butene. For this purpose, a raffinate I stream is fed to the reactor. The reactor is followed by a distillation column D1 at the top of which propene and ethene formed as by-product are removed. Unreacted raffinate I is taken off at the middle offtake. Some of it may: also be returned to the reactor R1 (not shown in FIG. 1). 2-Pentene, 2-methyl-2-butene and 3-hexene formed as by-product as well as high boilers are taken off at the bottom of D1. The bottoms are then fed together with added ethene to a reactor R2 which again contains a metathesis catalyst of the present invention. In this reactor R2, the reaction of 2-pentene and 2-methyl-2-butene with ethene to give 1-butene, isobutene and propene takes place. The reaction product from reactor R2 is fed to a distillation column D2 at the top of which propene and unreacted ethene are taken off. 1-Butene and isobutene formed are taken off at the middle offtake and at least sore is preferably returned to the reactor R1. Unreacted 2-pentene, 2-methyl-2-butene and also, as by-products, 3-hexene and high boilers are obtained at the bottom of D2. These are preferably returned to the reactor R2. The mixtures of propene and by-product ethene taken off at the top of D1 and D2 are fractionated in a further distillation column D3. Ethene is obtained at the top of D3 and this is preferably returned to the reactor R2 (not shown in FIG. 1), or discharged as co-cracker feed. The propene obtained at the bottom of D3 is the desired reaction product of the process of the present invention. D1 and D2 are designed such that a low-boiling phase, in particular a C2/3 phase comprising ethene and propene, is taken off at the top of the column. C4 streams, in particular butenes and butanes, are taken off as intermediate-boiling phase. As bottoms, C≧5-hydrocarbons are discharged.

Conditions: temp:0.00; pressure:0.00; stir:

Conditions: temp:0.00; pressure:0.00; stir:; See reaction.notes.procedure_details.

Procedure: Particular preference is given to the reaction of toluene with ethene or propene to give propylbenzene or isobutylbenzene, the reaction of cumene with ethene to give tert-amylbenzene and the reaction of xylenes with butadiene to give 5-tolylpentenes, and the reaction of p-xylene with 1-butene or 2-butene to give 1-tolyl-2-methylbutane.

Conditions: temp:0.00; pressure:0.00; stir:; See reaction.notes.procedure_details.

Procedure: Particular preference is given to the reaction of toluene with ethene or propene to give propylbenzene or isobutylbenzene, the reaction of cumene with ethene to give tert-amylbenzene and the reaction of xylenes with butadiene to give 5-tolylpentenes, and the reaction of p-xylene with 1-butene or 2-butene to give 1-tolyl-2-methylbutane.

Conditions: temp:0.00; pressure:0.00; stir:; See reaction.notes.procedure_details.

Procedure: The crystalline material of this invention can be used to catalyze a wide variety of chemical conversion processes including many of present commercial/industrial importance. Specific examples of chemical conversion processes which are effectively catalyzed by the crystalline material of this invention, by itself or in combination with one or more other catalytically active substances including other crystalline catalysts, include the following: cracking hydrocarbons with reaction conditions including a temperature of from about 300° C. to about 700° C., a pressure of from about 0.1 atmosphere (bar) to about 30 atmospheres and a weight hourly space velocity of from about 0.1 to about 20; dehydrogenating hydrocarbon compounds with reaction conditions including a temperature of from about 300° C. to about 700° C., a pressure of from about 0.1 atmosphere to about 10 atmospheres and a weight hourly space velocity of from about 0.1 to about 20; converting paraffins to aromatics with reaction conditions including a temperature of from about 100° C. to about 700° C., a pressure of from about 0.1 atmosphere to about 60 atmospheres, a weight hourly space velocity of from about 0.5 to about 400 and a hydrogen/hydrocarbon mole ratio of from about 0 to about 20; converting olefins to aromatics, e.g., benzene, toluene and xylenes, with reaction conditions including a temperature of from about 100° C. to about 700° C., a pressure of from about 0.1 atmosphere to about 60 atmospheres, a weight hourly space velocity of from about 0.5 to about 400 and a hydrogen/hydrocarbon mole ratio of from about 0 to about 20; converting alcohols, e.g., methanol, or ethers, e.g., dimethylether, or mixtures thereof to hydrocarbons including aromatics with reaction conditions including a temperature of from about 300° C. to about 550° C., more preferably from about 370° C. to about 500° C., a pressure of from about 0.01 psi to about 2000 psi, more preferably from about 0.1 psi to about 500 psi, and a liquid hourly space velocity of from about 0.5 to about 100; isomerizing xylene feedstock components with reaction conditions including a temperature of from about 230° C. to about 510° C., a pressure of from about 3 atmospheres to about 35 atmospheres, a weight hourly space velocity of from about 0.1 to about 200 and a hydrogen/hydrocarbon mole ratio of from about 0 to about 100; disproportionating toluene with reaction conditions including a temperature of from about 200° C. to about 760° C., a pressure of from about atmospheric to about 60 atmospheres and a weight hourly space velocity of from about 0.08 to about 20; alkylating isoalkanes, e.g., isobutane, with olefins, e.g., 2-butene, with reaction conditions including a temperature of from about -25° C. to about 400° C., e.g., from about 75° C. to about 200° C., a pressure of from below atmospheric to about 5000 psig, e.g., from about atmospheric to about 1000 psig, a weight hourly space velocity based on olefin of from about 0.01 to about 100, e.g., from about 0.1 to about 20, and a mole ratio of total isoalkane to total olefin of from about 1:2 to about 100:1, e.g., from about 3:1 to about 30:1; alkylating aromatic hydrocarbons, e.g., benzene and alkylbenzenes, in the presence of an alkylating agent, e.g., olefins, formaldehyde, alkyl halides and alcohols, with reaction conditions including a temperature of from about 340° C. to about 500° C., a pressure of from about atmospheric to about 200 atmospheres, a weight hourly space velocity of from about 2 to about 2000 and an aromatic hydrocarbon/alkylating agent mole ratio of from about 1/1 to about 20/1; transalkylating aromatic hydrocarbons in the presence of polyalkylaromatic hydrocarbons with reaction conditions including a temperature of from about 340° C. to about 500° C., a pressure of from about atmospheric to about 200 atmospheres, a weight hourly space velocity of from about 10 to about 1000 and an aromatic hydrocarbon/polyalkylaromatic hydrocarbon mole ratio of from about 1/1 to about 16/1; reacting olefins, e.g., isobutene or isopentene, with alcohols, e.g., methanol, to produce ethers with reaction conditions including a temperature of from about 20° C. to about 200° C., a total system pressure of from about 1 to about 200 atmospheres, an alcohol to olefin mole ratio of from about 0.1 to about 5 and a weight hourly space velocity of from 0.1 to about 200; converting light olefins, e.g., having 2 to 7 carbon atoms, to alcohol(s), ether(s) or mixtures thereof by reacting said light olefins with water under reaction conditions including a temperature from about 50° C. to about 300° C., a total pressure of at least about 5 atmospheres; and a mole ratio of water to total olefin of from about 0.1 to about 30; and transferring hydrogen from paraffins to olefins with reaction conditions including a temperature from about -25° C. to about 400° C., e.g., from about 75° C. to about 200° C., a pressure from below atmospheric to about 5000 psig, e.g., from about atmospheric to about 1000 psig, a mole ratio of total paraffin to total olefin of from about 1:2 to about 500:1, e.g., from about 5:1 to about 100:1; and a weight hourly space velocity based on olefin of from about 0.01 to about 100, e.g., from about 0.05 to about 5. with reaction conditions of from about 300° C. to about 700° C. of from about 300° C. to about 700° C. of from about 100° C. to about 700° C. of from about 100° C. to about 700° C. of from about 300° C. to about 550° C. more preferably from about 370° C. to about 500° C. of from about 230° C. to about 510° C. of from about 200° C. to about 760° C. of from about -25° C. to about 400° C., e.g. from about 75° C. to about 200° C. of from about 340° C. to about 500° C. of from about 340° C. to about 500° C.

Conditions: temp:0.00; pressure:0.00; stir:; See reaction.notes.procedure_details.

Procedure: Into a reaction vessel equipped with a stirrer, gas blowing tube, thermometer and condenser is fed cresol into which sulfuric acid has been dissolved (sulfuric acid is dissolved in 1.2% by weight based on 100% by weight of cresol) at 795 g/hr, further, butylation reaction is conducted for 8 hours at 65° C. under normal pressure with blowing in an isobutyrene mixed gas containing 1-butene, 2-butene and the like, and the resulted butylated reaction mixture is neutralized with an aqueous NaOH solution. For the neutralization, 1.5 equivalent NaOH is added per charged sulfuric acid and the treatment is conducted for 3 hours at 110° C., then an aqueous layer is separated, and the resulted oil layer is washed with water to obtain 11.79 kg of t-butylcresol mixture (cresolcontent6.4%, 4M2B contentl6.3%, 3M6B content 13.3%, dibutylated isomer content 58.6%, content of other components 5.4%). Into a reaction vessel equipped with a stirrer has been dissolved further, butylation reaction mixed gas the like, and the resulted reaction mixture the treatment is conducted for 3 hours at 110° C. an aqueous layer is separated the resulted oil layer is washed with water

Conditions: temp:0.00; pressure:0.00; stir:; See reaction.notes.procedure_details.

Procedure: The crystalline material of this invention can be used to catalyze a wide variety of chemical conversion processes including many of present commercial/industrial importance. Specific examples of chemical conversion processes which are effectively catalyzed by the crystalline material of this invention, by itself or in combination with one or more other catalytically active substances including other crystalline catalysts, include the following: cracking hydrocarbons with reaction conditions including a temperature of from about 300° C. to about 700° C., a pressure of from about 0.1 atmosphere (bar) to about 30 atmospheres and a weight hourly space velocity of from about 0.1 to about 20; dehydrogenating hydrocarbon compounds with reaction conditions including a temperature of from about 300° C. to about 700° C., a pressure of from about 0.1 atmosphere to about 10 atmospheres and a weight hourly space velocity of from about 0.1 to about 20: converting paraffins to aromatics with reaction conditions including a temperature of from about 100° C. to about 700° C., a pressure of from about 0.1 atmosphere to about 60 atmospheres, a weight hourly space velocity of from about 0.5 to about 400 and a hydrogen/hydrocarbon mole ratio of from about 0 to about 20; converting olefins to aromatics, e.g., benzene, toluene and xylenes, with reaction conditions including a temperature of from about 100° C. to about 700° C., a pressure of from about 0.1 atmosphere to about 60 atmospheres, a weight hourly space velocity of from about 0.5 to about 400 and a hydrogen/hydrocarbon mole ratio of from about 0 to about 20; converting alcohols, e.g., methanol, or ethers, e.g., dimethylether, or mixtures thereof to hydrocarbons including aromatics with reaction conditions including a temperature of from about 300° C. to about 550° C., more preferably from about 370° C. to about 500° C., a pressure of from about 0.01 psi to about 2000 psi, more preferably from about 0.1 psi to about 500 psi, and a liquid hourly space velocity of from about 0.5 to about 100; isomerizing xylene feedstock components with reaction conditions including a temperature of from about 230° C. to about 510° C., a pressure of from about 3 atmospheres to about 35 atmospheres, a weight hourly space velocity of from about 0.1 to about 200 and a hydrogen/hydrocarbon mole ratio of from about 0 to about 100; disproportionating toluene with reaction conditions including a temperature of from about 200° C. to about 760° C., a pressure of from about atmospheric to about 60 atmospheres and a weight hourly space velocity of from about 0.08 to about 20 ; alkylating isoalkanes, e.g., isobutane, with olefins, e.g., 2-butene, with reaction conditions including a temperature of from about -25° C. to about 400° C., e.g., from about 75° C. to about 200° C., a pressure of from below atmospheric to about 5000 psig, e.g., from about atmospheric to about 1000 psig, a weight hourly space velocity based on olefin of from about 0.01 to about 100, e.g., from about 0.1 to about 20, and a mole ratio of total isoalkane to total olefin of from about 1:2 to about 100:1, e.g., from about 3:1 to about 30:1; alkylating aromatic hydrocarbons, e.g., benzene and alkylbenzenes, in the presence of an alkylating agent, e.g., olefins, formaldehyde, alkyl halides and alcohols, with reaction conditions including a temperature of from about 340° C. to about 500° C., a pressure of from about atmospheric to about 200 atmospheres, a weight hourly space velocity of from about 2 to about 2000 and an aromatic hydrocarbon/alkylating agent mole ratio of from about 1/1 to about 20/1; transalkylating aromatic hydrocarbons in the presence of polyalkylaromatic hydrocarbons with reaction conditions including a temperature of from about 340° C. to about 500° C., a pressure of from about atmospheric to about 200 atmospheres, a weight hourly space velocity of from about 1 to about 1000 and an aromatic hydrocarbon/polyalkylaromatic hydrocarbon mole ratio of from about 1/1 to about 16/1; reacting olefins, e.g., isobutene or isopentene, with alcohols, e.g., methanol, to produce ethers with reaction conditions including a temperature of from about 20° C. to about 200° C., a total system pressure of from about 1 to about 200 atmospheres, an alcohol to olefin mole ratio of from about 0.1 to about 5 and a weight hourly space velocity of from 0.1 to about 200; converting light olefins, e.g., having 2 to 7 carbon atoms, to alcohol(s), ether(s) or mixtures thereof by reacting said light olefins with water under reaction conditions including a temperature from about 50° C. to about 300° C., a total pressure of at least about 5 atmospheres: and a mole ratio of water to total olefin of from about 0.1 to about 30; and transferring hydrogen from paraffins to olefins with reaction conditions including a temperature from about -25° C. to about 400° C., e.g., from about 75° C. to about 200° C., a pressure from below atmospheric to about 5000 psig, e.g., from about atmospheric to about 1000 psig, a mole ratio of total paraffin to total olefin of from about 1:2 to about 500:1, e.g., from about 5:1 to about 100:1; and a weight hourly space velocity based on olefin of from about 0.01 to about 100, e.g., from about 0.05 to about 5. with reaction conditions of from about 300° C. to about 700° C. of from about 300° C. to about 700° C. with reaction conditions of from about 100° C. to about 700° C. of from about 100° C. to about 700° C. of from about 300° C. to about 550° C. more preferably from about 370° C. to about 500° C. of from about 230° C. to about 510° C. of from about 200° C. to about 760° C. of from about -25° C. to about 400° C., e.g. from about 75° C. to about 200° C. of from about 340° C. to about 500° C. of from about 340° C. to about 500° C.

Conditions: temp:335.01; pressure:0.00; stir:; See reaction.notes.procedure_details.

Procedure: A mixture of 18.1 g (1.1 moles) of anhydrous ammonia, 27.5 g (0.5 mole) of cis, trans-2-butenes, 79.1 g of water and 43.5 g (0.10 mole) of ammonium iodide were charged to a 300 cm3 stainless steel autoclave. The autoclave was heated to 335° C. and held there for five hours with agitation; the maximum system pressure was 3,100 psig. A total of 3.3 g of mono-sec-butylamine, 0.01 g of di-sec-butylamine, 0.42 g of mono-n-butylamine, 1.29 g of sec-butyl alcohol, 0.06 g n-butyl alcohol, 0.35 g methylethylketone and 0.93 g of a hydrocarbon oil were obtained, corresponding to a 2-butene conversion of 19.9%, an amines yield of 52.1%, an alcohol yield of 25.9%, MEK yield of 5.0% and an oil yield of 17.0%.

Conditions: temp:0.00; pressure:0.00; stir:; See reaction.notes.procedure_details.

Procedure: The method of the invention to give the bicyclo[2.2.1]heptane derivatives in one step comprises reacting 2-butene with cyclopentadiene in the presence of an isomerization catalyst for simultaneous isomerization to give 2-methylene-3-methylbicyclo[2.2.1]heptane and/or 2,3-dimethylbicyclo[2.2.1]hept-2-ene.

Conditions: temp:0.00; pressure:0.00; stir:; See reaction.notes.procedure_details.

Procedure: Particular preference is given to the reaction of toluene with ethene or propene to give propylbenzene or isobutylbenzene, the reaction of cumene with ethene to give tert-amylbenzene and the reaction of xylenes with butadiene to give 5-tolylpentenes, and the reaction of p-xylene with 1-butene or 2-butene to give 1-tolyl-2-methylbutane.