Oxidative dehydrogenation process with hydrocarbon moderator gas and reduced nitrogen feed

Oxidative dehydrogenation includes: (a) providing a gaseous feed stream to a catalytic reactor, the feed stream comprising a dehydrogenation reactant, oxygen, superheated steam, hydrocarbon moderator gas and optionally nitrogen, wherein the molar ratio of moderator gas to oxygen in feed stream is typically from 4:1 to 1:1 and the molar ratio of oxygen to nitrogen in the feed stream is at least 2; (b) oxidatively dehydrogenating the reactant in the reactor to provide a dehydrogenated product enriched effluent product stream; and (c) recovering dehydrogenated product from the effluent product stream. One preferred embodiment is a process for making butadiene including dimerizing ethylene to n-butene in a homogeneous reaction medium to provide a hydrocarbonaceous n-butene rich feed stream and oxidatively dehydrogenating the n-butene so formed.

Low-fluoride, reactive polyisobutylene

A method of making a low-fluoride reactive PIB composition includes in one embodiment: a) providing an isobutylene-enriched C4 feedstock by way of blending a first mixed C4 feedstock with a second feedstock having a lower LB/IsoB index; (b) feeding the isobutylene-enriched C4 feedstock to a polymerization reactor with a catalyst complex comprising BF 3 and a modifier selected from alcohols, ethers and mixtures thereof; (c) polymerizing the isobutylene-enriched C4 feedstock in the reactor while maintaining the reactor at a temperature above −40° C. and most preferably above −15° C. and utilizing a residence time less than 45 minutes to produce a crude PIB composition in a polymerization mixture; and (d) recovering a purified PIB composition from the polymerization mixture having a molecular weight, Mn, from 250 to 5000 Daltons and an alpha vinylidene content of at least 50 mol %. The crude PIB composition suitably has a fluoride content of less than 100 ppm and the purified PIB composition has a fluoride content of less than 20 ppm. In another aspect, ammonium salts are used to neutralize the catalyst and fluoride salts are sublimed from the product at elevated temperatures.

CATALYST FOR REDUCED NITROGEN OXIDE (NOx) EMISSIONS IN AN OXODEHYDROGENATION PROCESS

The present invention discloses a process to treat a ferrite based catalyst useful in the oxidative dehydrogenation of monololefins and diolefins which process includes a preheat step prior to use of the catalyst in the OXO-D reactor. The catalyst is preferably a zinc ferrite catalyst for the production of butadiene. It has been observed that substantially no nitrogen oxide emissions result from the use of this treated catalyst in the reactor unit during the oxidative dehydrogenation reaction.

Manufacture of butadiene from ethylene

A method of producing butadiene includes: (1) dimerizing ethylene to butene followed by (2) oxidatively dehydrogenating the butene to butadiene and (3) recovering the butadiene by (i) absorbing the product with a hydrocarbon absorber oil and (ii) stripping a crude product stream from the absorber oil. The absorber oil is selected so as to be effective to sequester ethylene dimerization-derived impurities from the system.

Production of acetic acid with high conversion rate

A process for producing acetic acid comprising the steps of reacting carbon monoxide and at least one of methanol and a methanol derivative in a first reactor under conditions effective to produce a crude acetic acid product; separating the crude acetic acid product into at least one derivative stream, at least one of the at least one derivative stream comprising residual carbon monoxide; and reacting at least a portion of the residual carbon monoxide with at least one of methanol and a methanol derivative over a metal catalyst in a second reactor to produce additional acetic acid.

Low-fluoride, reactive polyisobutylene

A method of making a low-fluoride reactive PIB composition includes (a) providing a modified C4 feedstock by way of blending a mixed C4 feedstock with a second feedstock having a lower LB/IsoB ratio; or providing a C4 feedstock with an LB/IsoB index of less than 10%; (b) feeding the modified C4 feedstock or the C4 feedstock with an LB/IsoB index of less than 10% to a CSTR with a homogeneous catalyst comprising BF 3 and a modifier selected from alcohols, ethers and mixtures thereof; (c) polymerizing the modified C4 feedstock or the C4 feedstock with an LB/IsoB index of less than 10% in the reactor while maintaining the reactor at a temperature above −15° C. and utilizing a residence time less than 45 minutes to produce a crude PIB composition in a polymerization mixture; and (d) recovering a purified PIB composition from the polymerization mixture having a molecular weight, Mn, from 250 to 5000 Daltons and an alpha vinylidene content of at least 50 mol %. The crude PIB composition suitably has a fluoride content of less than 100 ppm and the purified PIB composition has a fluoride content of less than 20 ppm in preferred embodiments. In the most preferred embodiments, ammonium salts are used to neutralize the catalyst and fluoride salts are sublimed from the product at elevated temperatures.

PRODUCTION OF ACETIC ACID WITH HIGH CONVERSION RATE

A process for producing acetic acid comprising the steps of reacting carbon monoxide and at least one of methanol and a methanol derivative in a first reactor under conditions effective to produce a crude acetic acid product; separating the crude acetic acid product into at least one derivative stream, at least one of the at least one derivative stream comprising residual carbon monoxide; and reacting at least a portion of the residual carbon monoxide with at least one of methanol and a methanol derivative over a metal catalyst in a second reactor to produce additional acetic acid. 1. A process for producing acetic acid , comprisingreacting carbon monoxide and at least one of methanol and a methanol derivative in a first reactor under conditions effective to produce a crude acetic acid product;separating the crude acetic acid product into at least one derivative stream, at least one of the at least one derivative stream comprising residual carbon monoxide; andreacting at least a portion of the residual carbon monoxide with at least one of methanol and a methanol derivative over a metal catalyst in a second reactor to produce additional acetic acid.2. The process of claim 1 , wherein a product stream exiting the second reactor comprises less than 40 mol % carbon monoxide.3. The process of claim 1 , wherein the overall conversion of carbon monoxide is greater than 90%.4. The process of claim 1 , wherein the at least one derivative stream comprising residual carbon monoxide claim 1 , comprises:from 10 mol % to 95 mol % carbon monoxide; andfrom 5 mol % to 90 mol % at least one of methanol and a methanol derivative.5. The process of claim 1 , wherein the metal catalyst comprises a solid catalyst.6. The process of claim 5 , wherein the second reactor comprises a fixed bed reactor and the fixed bed reactor comprises the solid catalyst disposed in a catalyst bed.7. The process of claim 5 , wherein the second reactor comprises a trickle bed reactor and the trickle bed ...

Oxidative Dehydrogenation Process With Hydrocarbon Moderator Gas and Reduced Nitrogen Feed

Oxidative dehydrogenation includes: (a) providing a gaseous feed stream to a catalytic reactor, the feed stream comprising a dehydrogenation reactant, oxygen, superheated steam, hydrocarbon moderator gas and optionally nitrogen, wherein the molar ratio of moderator gas to oxygen in feed stream is typically from 4:1 to 1:1 and the molar ratio of oxygen to nitrogen in the feed stream is at least 2; (b) oxidatively dehydrogenating the reactant in the reactor to provide a dehydrogenated product enriched effluent product stream; and (c) recovering dehydrogenated product from the effluent product stream. One preferred embodiment is a process for making butadiene including dimerizing ethylene to n-butene in a homogeneous reaction medium to provide a hydrocarbonaceous n-butene rich feed stream and oxidatively dehydrogenating the n-butene so formed. 1. A method of oxidatively dehydrogenating a dehydrogenation reactant comprising: 'wherein the molar ratio of hydrocarbon moderator gas to oxygen in the feed stream is from 50:1 to 0.5:1;', '(a) providing a gaseous feed steam to a catalytic reactor, the feed stream comprising a dehydrogenation reactant, oxygen, superheated steam and a hydrocarbon moderator gas,'}(b) oxidatively dehydrogenating the dehydrogenation reactant in the reactor to generate an effluent product stream enriched in a dehydrogenated product derived from said dehydrogenation reactant; and(c) recovering said dehydrogenated product from the effluent product stream.23-. (canceled)4. The method according to claim 1 , wherein the molar ratio of hydrocarbon moderator gas to oxygen in the feed stream is from 8:1 to 0.5:1.5. (canceled)6. The method according to claim 1 , wherein the molar ratio of hydrocarbon moderator gas to oxygen in the feed stream is from 3:1 to 1.5:1.7. The method according to claim 1 , wherein the feed stream optionally comprises nitrogen and the molar ratio of oxygen:nitrogen in the feed stream is at least 0.5.8. The method according to claim 4 ...

Manufacture of Butadiene from Ethylene

A method of producing butadiene includes: (1) dimerizing ethylene to butene followed by (2) oxidatively dehydrogenating the butene to butadiene and (3) recovering the butadiene by (i) absorbing the product with a hydrocarbon absorber oil and (ii) stripping a crude product stream from the absorber oil. The absorber oil is selected so as to be effective to sequester ethylene dimerization-derived impurities from the system. 1. A method of producing butadiene from an ethylene raw material feed comprising:providing ethylene to a homogeneous reaction medium housed in a dimerization reactor;dimerizing ethylene to butene in the homogeneous reaction medium to provide a hydrocarbonaceous butene rich feed with ethylene dimerization-derived impurities therein;mixing said hydrocarbonaceous butene rich feed with steam and an oxygen rich gas to form an oxidative dehydrogenation reactor feed stream and superheating said oxidative dehydrogenation reactor feed stream to a temperature of at least 204° C. (400° F.),feeding the oxidative dehydrogenation reactor feed stream to an oxidative dehydrogenation reactor;oxidatively dehydrogenating said reactor feed stream in the oxidative dehydrogenation a reactor over an oxidative dehydrogenation catalyst thereby forming a butadiene enriched product stream;feeding the butadiene enriched product stream to a C4 absorber wherein C4's including butadiene and ethylene dimerization-derived impurities which may be present in oxidative dehydrogenation reactor effluent are absorbed into a compatible absorption oil;providing the absorption oil to a stripper in which C4 volatiles including butadiene are desorbed and stripped from said absorption oil under reduced pressure to provide a crude product stream; andrecovering butadiene from said crude product stream.2. The method according to claim 1 , wherein the hydrocarbonaceous feed stream has greater than 100 ppm of ethylene dimerization-derived impurities.3. The method according to claim 1 , wherein the ...

Multi-Stage Oxidative Dehydrogenation Process with Inter-Stage Cooling

A method of oxidatively dehydrogenating a dehydrogenation reactant includes providing a first gaseous feed stream to a first adiabatic, catalytic reaction zone with less than a stoichiometric amount of oxygen and superheated steam, oxidatively dehydrogenating dehydrogenation reactant in said first adiabatic, catalytic reaction zone and subsequently cooling the effluent, adding additional oxygen and reacting the effluent stream in at least one subsequent adiabatic reaction zone. The deydrogenation system enables higher conversion and yield per pass and in some cases greatly reduces steam usage and energy costs. In a preferred integrated process, ethylene is converted to n-butene which is then oxidatively dehydrogenated to butadiene.

Isobutylene Copolymers, Method for Making Isobutylene Copolymers and Isobutylene Copolymer Products

Isobutylene copolymer includes repeat units derived from isobutylene and one or more comonomers selected from isoprene, butadiene, cyclopentadiene, dicyclopentadiene, limonene, substituted styrenes, and C4 to C10 dienes other than isoprene, butadiene, limonene, cyclopentadiene, or dicyclopentadiene, wherein the molar ratio of isobutylene derived repeat units to the comonomer derived repeat units is from 75:1 to 1.5:1. The copolymers have a molecular weight, Mn, of from 200 to 20,000 Daltons and typically have a high double bond content and a high vinylidene double bond content when diene monomers are utilized. 151-. (canceled)53. The method according to claim 52 , wherein the reactor is maintained at a temperature of up to 35° C.54. The method according to claim 53 , wherein the reactor is maintained at a temperature of 5° C. or above.55. The method according to claim 54 , wherein the reactor is maintained at a temperature of 10° C. or above.56. The method according to claim 52 , utilizing a reactor residence time of 20 minutes or less.57. The method according to claim 56 , utilizing a reactor residence time of 10 minutes or less.58. The method according to claim 52 , wherein the conversion of comonomer is from 45% to 80%.59. The method according to claim 52 , wherein polymerization is carried out in a loop reactor.60. The method according to claim 52 , wherein the molar ratio of isobutylene to the one or more comonomers is from 3:5 to 1:1.61. The method according to claim 52 , further comprising incorporating the copolymer into a sizing composition.62. The method according to claim 52 , further comprising incorporating the copolymer into an unsaturated polyester resin.63. The method according to claim 52 , further comprising incorporating the copolymer into an epoxy resin.64. The method according to claim 52 , further comprising incorporating the copolymer into a polyurethane resin.65. An isobutylene copolymer comprising repeat units derived from isobutylene and ...

HEAT RECOVERY IN THE PROCESS OF PRODUCTION OF BUTADIENE

The process to recover heat in oxidative dehydrogenation of butene to butadiene is presented. The process utilizes heat recovered in oxidative dehydrogenation of butene to butadiene to generate steam. The process utilizes the circulated water stream generated in oxidative dehydrogenation of butene to butadiene for steam generation. A feedstream comprising butene is mixed with steam and preheated air at the inlet of the oxidative dehydrogenation reactor. 2. The process of further comprising passing the generated steam from the disengaging drum to the oxidative dehydrogenation reactor.3. The process of further comprising mixing the feedstream comprising butene with the steam and superheating the mixture to a temperature of at least 205° C.4. The process of wherein the product stream is cooled with water from the disengaging drum.5. The process of further comprising passing the product stream to the heat exchanger to vaporize a portion of the circulating water stream and generate steam.6. The process of wherein the circulating water stream is partially vaporized by heat exchange with the product stream comprising butadiene.7. The process of wherein the oxidative dehydrogenation reactor is a two stage reactor with the first stage generating an intermediate stream and passing the intermediate stream to the second stage claim 1 , further comprising heat exchanging the steam with the intermediate stream.8. The process of further comprising superheating the steam.9. The process of further comprising passing the superheated steam to the oxidative dehydrogenation reactor.10. The process of further comprising passing the product stream comprising butadiene to an oxygenate scrubber to generate a scrubbed stream.11. The process of further comprising passing the scrubbed stream to oxygenate stripper to generate a stripped stream and a vapor stream.12. The process of further comprising passing the stripped stream and an absorption oil to a C4 absorber to generate an absorption ...

Use of c4 absorber overhead for stripping aldehydes

A process is presented for the production of butadienes. The process includes the separation of oxygenates from the product stream from an oxidative dehydrogenation reactor. The process includes quenching the product stream and solvent and oxygenates from the product stream. The oxygenates are stripped from the solvent with an inert gas to reduce the energy consumption of the process, and the solvent is recycled and reused in the process.

Flexible Manufacturing System for Selectively Producing Different Linear Alpha Olefins

A flexible manufacturing system for selectively producing different alpha-olefins from ethylene includes: (a) a reaction section with ethylene feed operative to oligomerize ethylene; (b) a catalyst feed system comprising a plurality of independent homogeneous catalyst feeders connected with the reaction section for alternatively providing different selective homogeneous catalyst compositions to the reaction section; (c) an ethylene recycle column coupled to the reaction section and adapted to receive crude product and unreacted ethylene therefrom, the recycle column being operative to separate ethylene and optionally lower oligomers from the crude product which are recycled to the ethylene feed to the reaction section, the ethylene recycle column being further operative to provide a crude product bottoms stream; (d) a catalyst removal section coupled to the reaction section adapted to remove spent catalyst from the system; and (e) a first product separation column connected to the recycle column receiving the crude product stream therefrom, the product separation column being operative to separate purified oligomer from the crude product stream. Optionally provided is a second product separation column

Isobutylene copolymers, method for making isobutylene copolymers and isobutylene copolymer products

Isobutylene copolymer includes repeat units derived from isobutylene and one or more comonomers selected from isoprene, butadiene, cyclopentadiene, dicyclopentadiene, limonene, substituted styrenes, and C4 to C10 dienes other than isoprene, butadiene, limonene, cyclopentadiene, or dicyclopentadiene, wherein the molar ratio of isobutylene derived repeat units to the comonomer derived repeat units is from 75:1 to 1.5:1. The copolymers have a molecular weight, Mn, of from 200 to 20,000 Daltons and typically have a high double bond content and a high vinylidene double bond content when diene monomers are utilized.

Non-random isobutylene copolymers

Non-random isobutylene copolymer includes repeat units derived from isobutylene and one or more comonomers selected from isoprene, butadiene, cyclopentadiene, dicyclopentadiene, limonene, substituted styrenes, and C4 to CIO dienes other than isoprene, butadiene, limonene, cyclopentadiene, or dicyclopentadiene, wherein the molar ratio of isobutylene derived repeat units to the comonomer derived repeat units is from 75: 1 to 1.5: 1. The non-random copolymers have a molecular weight, Mn, of from 200 to 20,000 Daltons and typically have a high double bond content and a high vinylidene double bond content when diene monomers are utilized.

Non-random isobutylene copolymers

Non-random isobutylene copolymer includes repeat units derived from isobutylene and one or more comonomers selected from isoprene, butadiene, cyclopentadiene, dicyclopentadiene, limonene, substituted styrenes, and C4 to C10 dienes other than isoprene, butadiene, limonene, cyclopentadiene, or dicyclopentadiene, wherein the molar ratio of isobutylene derived repeat units to the comonomer derived repeat units is from 75:1 to 1.5:1. The non-random copolymers have a molecular weight, Mn, of from 200 to 20,000 Daltons and typically have a high double bond content and a high vinylidene double bond content when diene monomers are utilized.

Asphalt blends containing sulfonated elastomer microemulsions

Low-fluoride, reactive polyisobutylene

A method of making a low-fluoride reactive PIB composition includes (a) providing a modified C4 feedstock by way of blending a mixed C4 feedstock with a second feedstock having a lower LB/IsoB ratio; or providing a C4 feedstock with an LB/IsoB index of less than 10%; (b) feeding the modified C4 feedstock or the C4 feedstock with an LB/IsoB index of less than 10% to a CSTR with a homogeneous catalyst comprising BF3 and a modifier selected from alcohols, ethers and mixtures thereof; (c) polymerizing the modified C4 feedstock or the C4 feedstock with an LB/IsoB index of less than 10% in the reactor while maintaining the reactor at a temperature above -15°C and utilizing a residence time less than 45 minutes to produce a crude PIB composition in a polymerization mixture; and (d) recovering a purified PIB composition from the polymerization mixture having a molecular weight, Mn, from 250 to 5000 Daltons and an alpha vinylidene content of at least 50 mol %. The crude PIB composition suitably has a fluoride content of less than 100 ppm and the purified PIB composition has a fluoride content of less than 20 ppm in preferred embodiments. In the most preferred embodiments, ammonium salts are used to neutralize the catalyst and fluoride salts are sublimed from the product at elevated temperatures.

Low-fluoride, reactive polyisobutylene

A method of making a low-fluoride reactive PIB composition incudes in one embodiment: a) providing an isobutylene-enriched C4 feedstock by way of blending a first mixed C4 feedstock with a second feedstock having a lower LB/IsoB index; (b) feeding the isobutylene-enriched C4 feedstock to a polymerization reactor with a catalyst complex comprising BF 3 and a modifier selected from alcohols, ethers and mixtures thereof; (c) polymerizing the isobutylene-enriched C4 feedstock in the reactor while maintaining the reactor at a temperature above -40°C and most preferably above -15°C and utilizing a residence time less than 45 minutes to produce a crude PIB composition in a polymerization mixture; and (d) recovering a purified PIB composition from the polymerization mixture having a molecular weight, Mn, from 250 to 5000 Daltons and an alpha vinylidene content of at least 50 mol %. The crude PIB composition suitably has a fluoride content of less than 100 ppm and the purified PIB composition has a fluoride content of less than 20 ppm. In another aspect, ammonium salts are used to neutralize the catalyst and fluoride salts are sublimed from the product at elevated temperatures.

production of acetic acid with high conversion rate

produção de ácido acético com alta taxa de conversão. a presente invenção, em uma modalidade, se refere a um processo para produzir ácido acético. o processo compreende a etapa de reagir (i) uma alimentação de monóxido de carbono; e (ii) ao menos um dentre metanol e um derivado de metanol em um primeiro reator, sob condições eficazes para produzir um produto de ácido acético bruto. em modalidades preferenciais, a alimentação de monóxido de carbono compreende menos de 99,5 mol% de monóxido de carbono. o processo, em algumas modalidades, compreende, adicionalmente, a etapa de purgar a partir do primeiro reator, uma corrente de purga de monóxido de carbono compreendendo uma primeira quantidade de monóxido de carbono residual e uma ou mais impurezas. de preferência, a primeira quantidade é maior do que 20 mol%. o processo compreende, adicionalmente, a etapa de separar o produto de ácido acético bruto em pelo menos uma corrente derivada. ao menos uma da(s) corrente(s) derivada(s) compreende uma segunda quantidade de monóxido de carbono residual. o processo compreende, adicionalmente, a etapa de reagir pelo menos uma porção da segunda quantidade de monóxido de carbono residual e pelo menos um dentre metanol e um derivado de metanol em um segundo reator sob condições eficazes para produzir ácido acético adicional. como resultado, o processo da invenção alcança uma conversão total de monóxido de carbono de pelo menos 95%, com base na quantidade total de monóxido de carbono na alimentação de monóxido de carbono. production of acetic acid with high conversion rate. the present invention, in one embodiment, relates to a process for producing acetic acid. the process comprises the step of reacting (i) a carbon monoxide feed; and (ii) at least one of methanol and one methanol derivative in a first reactor, under conditions effective to produce a crude acetic acid product. in preferred embodiments, the carbon monoxide feed comprises less than 99.5 mol% of carbon monoxide. the ...

Use of c4 absorber for stripping aldehydes

A process is presented for the production of butadienes. The process includes the separation of oxygenates from the product stream from an oxidative dehydrogenation reactor. The process includes quenching the product stream and solvent and oxygenates from the product stream. The oxygenates are stripped from the solvent with an inert gas to reduce the energy consumption of the process, and the solvent is recycled and reused in the process.

Production of acetic acid with high conversion rate

Isobutylene copolymers, method for making isobutylene copolymers and isobutylene copolymer products

Isobutylene copolymer includes repeat units derived from isobutylene and one or more comonomers selected from isoprene, butadiene, cyclopentadiene, dicyclopentadiene, limonene, substituted styrenes, and C4 to CIO dienes other than isoprene, butadiene, limonene, cyclopentadiene, or dicyclopentadiene, wherein the molar ratio of isobutylene derived repeat units to the comonomer derived repeat units is from 75: 1 to 1.5: 1. The copolymers have a molecular weight, Mn, of from 200 to 20,000 Daltons and typically have a high double bond content and a high vinylidene double bond content when diene monomers are utilized.

Catalyst for reduced nitrogen oxide (NOx) emissions in an oxodehydrogenation process

The present invention discloses a process to treat a ferrite based catalyst useful in the oxidative dehydrogenation of monololefins and diolefins which process includes a preheat step prior to use of the catalyst in the OXO-D reactor. The catalyst is preferably a zinc ferrite catalyst for the production of butadiene. It has been observed that substantially no nitrogen oxide emissions result from the use of this treated catalyst in the reactor unit during the oxidative dehydrogenation reaction.

Manufacture of butadiene from ethylene

A method of producing butadiene includes: (1) dimerizing ethylene to butene followed by (2) oxidatively dehydrogenating the butene to butadiene and (3) recovering the butadiene by (i) absorbing the product with a hydrocarbon absorber oil and (ii) stripping a crude product stream from the absorber oil. The absorber oil is selected so as to be effective to sequester ethylene dimerization-derived impurities from the system.

Use of c4 absorber for stripping aldehydes

Dehydrogenation process and system with reactor re-sequencing

A dehydrogenation system includes a plurality of dehydrogenation reactors valved to operate in alternating dehydrogenation modes and regeneration modes in a timed sequence in a system cycle by way of the plurality of valves; a digital programmable controller connected to the plurality of valves for sequencing the reactors; and means for determining the productivity characteristics of each reactor over a system cycle. The digital controller is operable to re-sequence the reactors to reduce either peak productivity or productivity deltas over an initial system cycle. After resequencing, production may be increased with the more uniform productivity profile of the re-sequenced system without exceeding system limits, such as compressor operating limits.

Dehydrogenation process and system with reactor re-sequencing

A dehydrogenation system includes a plurality of dehydrogenation reactors valved to operate in alternating dehydrogenation modes and regeneration modes in a timed sequence in a system cycle by way of the plurality of valves; a digital programmable controller connected to the plurality of valves for sequencing the reactors; and means for determining the productivity characteristics of each reactor over a system cycle. The digital controller is operable to re-sequence the reactors to reduce either peak productivity or productivity deltas over an initial system cycle. After resequencing, production may be increased with the more uniform productivity profile of the re-sequenced system without exceeding system limits, such as compressor operating limits.

Dehydrogenation process and system with reactor re-sequencing

Copolímeros de isobutileno no aleatorios

Non-random isobutylene copolymers

Non-random isobutylene copolymer includes repeat units derived from isobutylene and one or more comonomers selected from isoprene, butadiene, cyclopentadiene, dicyclopentadiene, limonene, substituted styrenes, and C4 to C10 dienes other than isoprene, butadiene, limonene, cyclopentadiene, or dicyclopentadiene, wherein the molar ratio of isobutylene derived repeat units to the comonomer derived repeat units is from 75:1 to 1.5:1. The non-random copolymers have a molecular weight, Mn, of from 200 to 20,000 Daltons and typically have a high double bond content and a high vinylidene double bond content when diene monomers are utilized. (Fig. 1)

Isobutylene copolymers, method for making isobutylene copolymers and isobutylene copolymer products

Isobutylene copolymer includes repeat units derived from isobutylene and one or more comonomers selected from isoprene, butadiene, cyclopentadiene, dicyclopentadiene, limonene, substituted styrenes, and C4 to C10 dienes other than isoprene, butadiene, limonene, cyclopentadiene, or dicyclopentadiene, wherein the molar ratio of isobutylene derived repeat units to the comonomer derived repeat units is from 75:1 to 1.5:1. The copolymers have a molecular weight, Mn, of from 200 to 20,000 Daltons and typically have a high double bond content and a high vinylidene double bond content when diene monomers are utilized.