The process of co-production of isoprene and isobutene or alkenylbenzene

 

(57) Abstract:

A method is proposed for the joint production of isoprene and isobutene or alkenylbenzene of isopentane and isobutane or alkylbenzene with the number of carbon atoms in the alkyl group, 2 - 4, including the zone in which the liquid-phase oxidation of isobutane or alkylbenzene with the formation of hydroperoxide, the catalytic epoxidation of 2-methyl-2-butene specified manner with the formation of oxide 2-methyl-2-butene and alcohol, turning them respectively in isoprene and isobutene or alkylbenzene and separation of reaction mixtures, with 2-methyl-2-butene is obtained by combining at least the processes of dehydrogenation of isopentane, catalytic isomerization formed during the dehydrogenation of 2-methyl-1-butene 2-methyl-2-butene, and the rectification of mixtures formed during the dehydrogenation and isomerization, the isomerization of 2-methyl-1-butene is carried out directly in the node dehydrogenation, which return the mixture after distillation of 2-methyl-2-butene, containing predominantly isopentane and 2-methyl-1-butene, and/or by contacting a stream containing 2-methyl-1-butene and possibly isopentane and 2-methyl-2-butene, with an acidic catalyst at 50-100C., preferably in edusim decomposition formed in the zone of contact with the acidic catalyst alkyl-tert-pentalofos ether at 60-130oWith the return of isopentenyladenosine stream into a dehydrogenation zone and the specified alcohol in the zone of contact with the acidic catalyst, a dedicated thread 2-methyl-2-butene are interacting with the solution of the hydroperoxide obtained in the oxidation of isobutane or alkylbenzene in the presence of an epoxidation catalyst with the formation of oxide 2-methyl-2-butene and tert-butanol or alkylaromatic alcohol, which is then transformed into the target monomers. The technical result is to simplify the process and reduce energy consumption. 6 C.p. f-crystals, 3 tab., 1 Il.

The invention relates to the field of production of isoprene and monovinylacetylene monomers.

A known method of producing isoprene by catalytic gas-phase dehydrogenation of isopentane and isopentanol at high temperatures (530-650oC) involving separation of isopentane-isopentanol, isopentene-isoprene mixtures by extractive distillation with a polar separating agent (usually N, N-dimethylformamide) [P. A. Kirpichnikov, M. C. Beresnev, L. M. Popova Album technological schemes of the main industries of synthetic rubber, L., Chemistry, 1986, S. 53-70].

The disadvantage of this method is the difficulty technologystatus rectification and in the area of dehydrogenation of isopentane.

A known method of producing isoprene from isopentane [US Patent N 3391214 from 02.07.1968], according to which the isopentane is subjected to liquid-phase oxidation with obtaining a solution of tert-pentylcyclohexyl, a solution of tert-pentylcyclohexyl contact zone epoxidation of 2-methyl-2-butene in the presence of a catalyst with the formation of oxide 2-methyl-2-butene and tert-pentanol, from the reaction mixture allocate at least the threads with a predominant content of isopentane returned to the zone of liquid-phase oxidation of 2-methyl-2-butene, returned to the epoxidation zone, tert-pentanol, subjected to dehydration with the return of 2-methyl-2-butene in the area epoxidation and oxide 2-methyl-2-butene being catalyzed transformation into isoprene.

The disadvantage of this method is the low conversion (~ 7-10%) isopentane during its oxidation to hydroperoxide and significant conversion of isopentane (especially when trying to increase his conversion) in by-products, as in the oxidation of isopentane is not only "tertiary carbon atom in position 2, but also the adjacent carbon atom in position "3".

As the previous cited methods, the method according to US Pat 3391214 not simultaneously ] simultaneous receipt of alkadiene(s), in particular isoprene, and monovinylacetylene monomers, in particular isobutene or alkenylbenzene(s), including separate liquid-phase oxidation of the source of the hydrocarbons with the formation of hydroperoxides and partially alcohols (for example, oxidation of isopentane in one reaction zone and the oxidation of isobutane or alkylbenzene in another reaction zone), followed by joint processing of oxidation by-products and recycled 2-methyl-2-butene in the area epoxidation, dehydration of the resulting alcohol with getting monoisostearate monomer and 2-methyl-2-butene, recycled to the epoxidation zone, the transformation produced in the epoxidation zone oxide 2-methyl-2-butene to isoprene and separation of reaction mixtures.

This method is most similar to that proposed by us.

The disadvantage of this method, apart from its complexity, is that at the stage of liquid-phase oxidation of isopentane (2-methylbutane) cannot be achieved sufficiently selective education tert-pentylcyclohexyl and tert-pentanol, because simultaneously with the oxidation of the carbon atom in position "2" is the oxidation of the carbon atom in position "3". The rate of oxidation of isopentane and conversion are the bottom of alagaesia the process of co-production of isoprene and isobutene or alkenylbenzene of isopentane and isobutane or alkylbenzene with the number of carbon atoms in the alkyl group is from 2 to 4, including zone, and in which the liquid-phase oxidation of isobutane or alkylbenzene with the formation of hydroperoxide, the catalytic epoxidation of 2-methyl-2-butene specified manner, the transformation produced in the epoxidation zone oxide 2-methyl-2-butene to isoprene, dehydration forming in the area of epoxidation of alcohol in isobutene or alkenylphenol and separation of reaction mixtures formed in the above reaction zones, namely, that 2-methyl-2-butene is obtained by combining at least the processes of dehydrogenation of isopentane, catalytic isomerization formed during the dehydrogenation of 2-methyl-1-butene 2-methyl-2-butene, and the rectification of mixtures formed during the dehydrogenation and isomerization, the isomerization of 2-methyl-1-butene is carried out directly in the node dehydrogenation, which return the mixture after distillation of 2-methyl-2-butene, containing predominantly isopentane and 2-methyl-1-butene, and/or by contacting a stream containing 2-methyl-1-butene and possibly isopentane and 2-methyl-2-butene, with an acidic catalyst at from 50 to 100oC, preferably in the presence of alcohol and/or water with subsequent or simultaneous distillation of 2-methyl-2-butene may polea when 60-130oC, return isopotential stream into a dehydrogenation zone and the specified alcohol in the zone of contact with the acidic catalyst, a dedicated thread 2-methyl-2-butene are interacting with the solution of the hydroperoxide obtained in the oxidation of isobutane or alkylbenzene in the presence of an epoxidation catalyst with the formation of oxide 2-methyl-2-butene and tert-butanol or alkylaromatic alcohol, which is then transformed into the target monomers.

As a variant of the proposed method lies in the fact that obtained after dehydrogenation of isopentane isopentane-isopentenyl mixture is subjected in the presence of acidic catalyst for the countercurrent contacting with a non-tertiary alcohol C3-C6supplied in quantities above the stoichiometric with respect to the amount of isopentanol, in the system of the reaction-distillation-type and top place isopentenyladenosine stream is returned to the dehydrogenation zone, and the bottom output stream containing C3-C6-non-tertiary alkyl-tert-pentalogy ether, which is then decomposed in the presence of an acidic catalyst to obtain a stream of isopentanol having a high content of 2-methyl-2-butene, which is then distilled 2-Metalocalypse is that from the reaction mixture obtained by the oxidation of isobutane or alkylbenzene before submitting it to the epoxidation zone is distilled off at least part of oxygenated hydrocarbon or mixture of oxygenated hydrocarbons, which return to the zone of oxidation.

As a variant of the proposed method lies in the fact that the mixture obtained by oxidation IsolatedStorage raw materials, possibly after removal of the acid, is mixed with 2-methyl-2-butene, and then distilled off at least a portion of the isobutane, which is returned to the oxidation zone, and the remaining mixture is fed to the epoxidation zone.

As a variant of the proposed method lies in the fact that isolated from epoxidase stream containing predominantly oxide 2-methyl-2-butene, is subjected to catalytic decomposition at elevated temperature, preferably in the presence of water vapor, followed by separation of isoprene from the reaction mixture.

As a variant of the proposed method lies in the fact that the oxide 2-methyl-2-butene initially converted into unsaturated alcohol isomerization in the presence of a catalyst with prevailing basic properties or glycol by hydration in the presence of an alkaline or acidic catalyst with which Aligator.

As a variant of the proposed method lies in the fact that, as the acidic catalyst used sulfonation in+form.

The above options, the relevant paragraphs.2-7 claims, are dependent only on the primary method set forth in paragraph 1 of the claims. They can be used in various combinations while respecting fact, set forth in paragraph 1 of the claims.

As catalysts in the dehydrogenation zone a stream containing predominantly isopentane can be used in a variety of dehydrogenation catalysts, preferably containing aluminum oxide and metals of variable valence, such as chromium, platinum, palladium, Nickel. The dehydrogenation may be carried out in different reactors continuous or periodic (periodic oxidative regeneration or heating) action, in which the catalyst is in a stationary or suspended ("pseudocyesis").

As the acid(s) of catalyst(s) by isomerization of 2-methyl-1-butene 2-methyl-2-butene, decomposition forms(their)SJ ether(s) and dehydration of the alcohol(s), including alcohol produced in the epoxidation zone 2-methyl-2-buta is ethyl-2-butene to isoprene, can be used in a variety of acidic catalysts, such as liquid mineral acids, solid acids, acidic ion exchangers, high-silicon zeolites, palladium or platinum on the carrier, and most preferably the use of high acid ion exchangers, in particular sulfonic cation.

Oxidation of isobutane and alkylbenzene(s) may be oxygen, including oxygen contained in air or in various attackalert mixtures, in the absence of catalyst or in the presence of different oxidation catalysts, such as phthalocyanines, ferrocene etc.

In the area of the epoxidation of 2-methyl-2-butene-hydroperoxide(AMI) can be used various known catalysts for epoxidation, preferably containing compounds of molybdenum, in particular the catalysts containing glycolate molybdenum.

For catalytic decomposition of oxide 2-methyl-2-butene at elevated temperatures can be used in various suitable for this purpose, the catalysts, for example catalysts containing compounds of boron and/or strontium and/or phosphoric acid on a solid carrier.

When turning oxide 2-methyl-2-butene to isoprene in the interim unity lithium chromium, molybdenum, iron, tin, cobalt. Most preferably the use of catalysts containing lithium salts, such as phosphate(s) lithium, possibly in aprotic polar organic solvents, for example N-organic.

At an intermediate stage of hydration of the oxide 2-methyl-2-butene in the glycol can be used in various acidic catalysts such as sulfonic cation exchangers in the H+form, or alkaline catalysts such as sodium hydroxide, potassium, lithium.

The use of the invention is illustrated in the drawing and examples. The drawing and the examples are not exhaustive of all possible embodiments of the invention and other possible technical solutions, while respecting the essence of the invention set forth in the claims.

According to the drawing the original thread F1containing predominantly isopentane (PI), together with recycle stream is dominated by FE (joint thread 1) is subjected to dehydration in the node D-1 and resulting from contact of gas (stream 2) allocate stream 3 containing mainly a mixture of isopentane and isopentanol, mainly 2-methyl-2-butene (MB) and 2-methyl-1-butene (MB).

The specified thread 3 is processed by one of the PIS and MB, which return line 4 to the node D-1, and the bottom stream 5 containing predominantly MB directed further along the line 7' in the system of production of isoprene through intermediate epoxidation MB and receive oxide 2-methyl-2-butene (node epoxidation e and/or distillation column P3).

In variant II stream 3 is sent to the node isomerization, And where the catalytic conversion of a part MB in MB, preferably in the presence of alcohol and/or water. The isomerate stream (stream 5) is subjected to rectification in the column P1 and the top of its output stream, containing mainly FE and partially MB, which is sent to the node on line 4 D-1. CBM product columns P1 (stream 6) is sent to distillation column P2, above which the output stream 7 containing predominantly MB sent to the node e and/or column P3. Bottom-P2 output stream 8 containing alcohol(s), and/or esters and/or water, which at least partially along the line 8 is sent to the node "And" (part of the specified VAT stream can be withdrawn from the system through line 8').

In version III of the thread 3 is sent to distillation column PP1, from which the above supply output stream 6, with a high content MB, which is sent to the node isomerization "the Oia.

Alternatively, the isomerization zone with an acidic coarse catalyst can be placed inside the column PP1.

Higher sampling flow 6 (or higher layer of the catalyst when the internal placement of the reaction zone) PP1 serves stream 8 containing alcohol(s), and/or esters and/or water. Top PP1 output stream containing mainly FE, the return line 4 to the node D-1. Bottom PP1 output stream 5 containing predominantly MB and the above alcohol(s), esters and/or water, which is sent to distillation column P2. Top P2 output stream 7 containing predominantly MB sent to the node e and/or column P3, and the bottom output stream 8 returned in PP1.

In option IV flow 3 sent to the reaction-distillation apparatus PP1 containing at least above the point of power acidic solid catalyst, preferably molded sulfonation. Above the layer of catalyst injected stream 6 containing predominantly non-tertiary alcohol. Top PP1 output stream containing mainly FE, which is in line 4 returns to the node D-1. Bottom PP1 output stream 5 containing esters formed by isopentane with alcohol, and partially unreacted alcohol. Thread 5 serves in the reaction-rectificationed, and the top thread 6', containing predominantly MB, and partly MB, served in the distillation column R. the Top of the column R output stream 8 containing predominantly MB returned in PP1 and the lower stream 7 containing predominantly MB, which is sent to the node e and/or column P3.

The original thread F2(stream 9) containing isobutane and/or alkylbenzene, is subjected to oxidation with oxygen or oxygen-containing gas mixture (stream 10) in the node oxidation "On". Oxidat, containing a solution of tert-butyl hydroperoxide and/or alkylbenzene(s) in line 11 is sent to the node epoxidation e and/or distillation column P3 (preferred option when using isobutane as the oxidizable hydrocarbon). In the latter case, the thread 11 (or part thereof) may mix with the flow MB and above P3 distilled stream 11a containing predominantly isobutane, who return to the site of oxidation Oh, and the bottom output stream 11b sent to the node E.

The flow of epoxide from node e along the line 12 is sent to the node separation OR from which output stream 13 containing predominantly MB returned to the node "e", stream 14 containing predominantly isobutane or alkylbenzene, comes the eating of turning oxide 2M2-butene to isoprene (node), and stream 16 containing predominantly alcohol(s), forming(e)descendants of cumene hydroperoxide(s) during epoxidation MB.

When using isobutane as the oxidizable hydrocarbon as a variant of the resulting tert-butanol fully served with oxide 2-methyl-2-butene on line 15 into the site, where, along with conversion of the oxide 2-methyl-2-butene to isoprene, tert-butanol dehydration in isobutene. In this case, the nodes D-2 and OR do not use.

After transformation into a host BY a thread 17 is sent to the node separation OR, from which derive at least stream 18 containing predominantly isoprene (IPR), you can stream 19 containing isobutene and thread(s) that contain(s) by-products (PP) (stream 20) and water (stream 20A).

Stream 16 containing alcohol(s), submit (if not implemented the option of filing of tert-butanol together with the oxide in the node) to the node in the dehydration of D-2. Part of the stream may be withdrawn through line 16A.

From node dehydration of D-2 the reaction mixture or the separated water from its organic part (stream 21) served in the separation unit UR-3, from which the output stream of the olefin(s) (isobutene or alkylbenzene) in line 22 and the thread(s) by-products of PP and possibly water (line 23).

P is, Ariant 1.

Dehydrogenation of isopentane and simultaneous isomerization MB in MB in the node D-1 is carried out in the presence of fluidized-bed industrial alimohammadi catalyst IM-2201 at 560oC.

As distillation columns R use the column efficiency 50 theory.plates, working with a reflux ratio of 5.0.

The oxidation of isobutane in the site "About" carry oxygen in the absence of catalyst at 135oC.

Epoxidation MB tert-butylhydroperoxide carried out in the node "e" in the presence of a catalyst containing molybdenum glycolate, at 90-100oC.

In the host BY direct mixture containing predominantly oxide 2-methyl-2-butene and tert-butanol (stream 15), and carry out catalytic thermal conversion of the oxide MB in isoprene and tert-butanol in isobutene in the presence of a catalyst containing boron phosphate, 340oC.

The compositions and the number of main streams are given in table. 1.

Example 2. As raw materials use of isopentane and isobutane. Processing is carried out in accordance with drawing, variant II.

Isomerization in the site And carried out in the presence of sulfocationites catalyst Amberlyst-35 (centraly 90% tert-pentanol and 0.2% water. Temperature isomerization 70oC.

Stream 7 containing predominantly MB, before serving in the node epoxidation is mixed with a stream of oxidate from node "O" (stream 11), in column P3 distilled the isobutane stream (stream 11), returned to the site of oxidation "On", and cubic mixture comprising 27.7% of tert-butylhydroperoxide, 29,6% tert-butanol and 20.5% MB, served in the node epoxidation "e" (catalyst based on molybdenum glycolate). Epoxide (stream 12) is subjected to separation in the node OR. Stream 15 containing predominantly oxide MB and tert-butanol, is sent to the node where subjected to catalytic thermal conversion on acidic heterogeneous catalyst containing boron phosphate. The reaction mixture is subjected to separation in the node OR, where, in particular, emit isoprene (stream 18) and isobutene (stream 19).

Supply of raw materials F1and F2respectively 1.0 t/h and 1.44 t/h

The result of 0.53 t/HR of isoprene and of 1.27 t/h of isobutene.

Example 3. As raw materials use of isopentane and isobutane. Processing is carried out in accordance with drawing III.

The dehydrogenation in the node D-1 is carried out in two reactors in the presence of stationary alimohammadi catalyst DV-SMEs hydrocarbons WITH5(stream 3) is subjected to separation in a distillation column PP1, in the upper part of which serves (mostly from Cuba subsequent columns P2) a stream containing predominantly tert-pentanol in an amount to provide its concentration at the point of the output side of the selection 30-40 wt.%. From PP1 output side stream 6, which is directed to the node isomerization And containing sulphidity catalyst Amberlyst-15 (SOY = 4,7). The isomerization is carried out at 60-65oC. From node "And" isomerizate return in the middle or lower part of the column of PP1.

Warded off in R-2 stream 7 to submission to the node "e" is mixed with stream 11 with subsequent distillation stream of isobutane (11a) in the column P3. Node "e" is used a catalyst containing the alcoholate of molybdenum.

Node OR from the reaction mixture (stream 12) allocate stream 15 containing predominantly oxide 2-methyl-2-butene and stream 16 containing predominantly tert-butanol. Department oxide 2-methyl-2-butene from tert-butanol is carried out using rectification in the presence of water as a selective agent.

In the stream 15 oxide 2-methyl-2-butene initially subjected to isomerization of unsaturated alcohol in the presence of a catalyst on the basis of lithium phosphate in 250oC and saarma 90oC.

In the stream 16 carry out the dehydration of tert-butanol in the reaction-distillation apparatus containing molded with polypropylene sulphidity catalyst KU-FPP (SOY = 3.3V) at 70-80oC. the Supply of raw material F1and F2respectively 1.0 t/h and 1.9 t/h

The result of 0.50 tons/HR of isoprene and 1.73 t/h isobutene.

Example 4. As raw materials use of isopentane and isobutane. Processing is carried out in accordance with drawing, option IV.

Dehydrogenation of isopentane in the node D-1 is on platypodinae catalyst at 540oC. Stream 3 is subjected to the countercurrent contacting with n-butanol (stream 6) in the reaction-distillation apparatus PP1 containing molded sulphidity catalyst'KEEFE (SOY = 3,6). N-butanol is served in a molar ratio to the sum of isopentanol of 1.5:1. In the reaction zone keep the temperature of 60-70oC. Top output stream 4 containing concentrated almost isopentane returned in D-1. From the cube output stream containing n-butyl-tert-pentalogy ether and partially n-butanol, which is sent to the reaction-distillation apparatus PP2, also containing catalyst'KEEFE.

Top Rrsi mainly MB, return in PP1.

Of epoxide (stream 12) in the node OR highlight, in particular, stream 15 containing oxide MB and tert-butanol, addressed to the node. The transformation of the oxide MB carried out by hydrating it in a glycol C5in the presence of 1% of potassium hydroxide at 90oC, and then dehydration formed glycol and tert-butanol at 110oC in the reaction-distillation apparatus in the presence of sulfonate catalyst KU-FPP. Node OR from dehydration of the mixture emit isoprene and isobutene.

Supply of raw materials F1and F2respectively 1.0 t/h and of 1.52 t/h

The result of 0.50 tons/HR of isoprene and of 1.27 t/h of isobutene.

Example 5. As raw materials use isopentane (F1) and ethylbenzene (P2). Processing is carried out in accordance with drawing III.

Ethylbenzene is subjected to oxidation coloradostate mixture (50% oxygen) in node "On" when 55oC. Conduct epoxidation of 2-methyl-2-butene obtained by hydropredict of ethylbenzene in the presence of a catalyst containing molybdenum glycolate, at 90-100oC. the epoxidation is formed oxide 2-methyl-2-butene and methylphenylcarbinol.

Reactivat thermocatalytic conversion to isoprene at 350oC in the presence of a heterogeneous catalyst containing strontium, followed by separation of isoprene.

Stream 16 containing predominantly methylphenylcarbinol, is subjected to dehydration in site D-2 in the presence of an acidic heterogeneous catalyst is active alumina at 280oC, after which the node P3 of the reaction mixture produce styrene.

Supply of raw materials F1and F2respectively 1.0 t/h and is 1.51 t/h

The compositions and the number of main streams are given in table. 2

The result of 0.54 t/HR of isoprene and 1.36 t/h of styrene.

Example 6. As raw materials use isopentane (F1) and isopropylbenzene (F2). Processing is carried out in accordance with drawing, option III with the use of catalysts and temperatures in the reaction zones, similar to that used in example 5.

Submission F1and F2respectively 1.0 t/h and 1.54 t/h

The result of 0.54 t/HR of isoprene and 1.38 t/h - methylstyrene.

The compositions and the number of main streams are given in table. 3.

1. The process of co-production of isoprene and isobutene or alkenylbenzene of isopentane and isobutane or alkylbenzene with the number of carbon is cilmente with the formation of hydroperoxide, catalytic epoxidation of 2-methyl-2-butene specified manner, the transformation produced in the epoxidation zone oxide 2-methyl-2-butene to isoprene, dehydration forming in the area of epoxidation of alcohol in isobutene or alkenylphenol and separation of reaction mixtures formed in the above reaction zones, wherein the 2-methyl-2-butene is obtained by combining at least the processes of dehydrogenation of isopentane, catalytic isomerization formed during the dehydrogenation of 2-methyl-1-butene 2-methyl-2-butene and rectification of mixtures formed during the dehydrogenation and isomerization, moreover, the isomerization of 2-methyl-1-butene is carried out directly in the node dehydrogenation, which return the mixture after distillation of 2-methyl-2-butene, containing predominantly isopentane and 2-methyl-1-butene, and/or by contacting a stream containing 2-methyl-1-butene and possibly isopentane and 2-methyl-2-butene, with an acidic catalyst at 50 - 100C, preferably in the presence of alcohol and/or water with subsequent or simultaneous distillation of 2-methyl-2-butene, possible subsequent decomposition formed in the zone of contact with the acidic catalyst alkyl-tert-pentalofos ether at 60 to 130C, vozvrashiaetsea, dedicated thread 2-methyl-2-butene are interacting with the solution of the hydroperoxide obtained in the oxidation of isobutane or alkylbenzene in the presence of an epoxidation catalyst with the formation of oxide 2-methyl-2-butene and tert-butanol or alkylaromatic alcohol, which is then transformed into the target monomers.

2. The method according to p. 1, characterized in that the after dehydrogenation of isopentane isopentane-isopentenyl mixture is subjected in the presence of acidic catalyst for the countercurrent contacting with a non-tertiary alcohol C3-C6supplied in quantities above the stoichiometric with respect to the amount of isopentanol, in the system of the reaction-distillation-type and top place isopentenyladenosine stream is returned to the dehydrogenation zone, and the bottom output stream containing C3-C6-non-tertiary alkyl-tert-pentalogy ether, which is then decomposed in the presence of an acidic catalyst to obtain a stream of isopentanol having a high content of 2-methyl-2-butene, which is then distilled 2-methyl-1-butene and 2-methyl-2-butene sent to the epoxidation zone.

3. The method according to p. 1, characterized in that the reaction mixture obtained by oxidation from Dorada or mixture of oxygenated hydrocarbons, you return to the zone of oxidation.

4. The method according to p. 1, characterized in that the mixture obtained by oxidation IsolatedStorage raw materials, possibly after removal of acid mixed with 2-methyl-2-butene, and then distilled off at least a portion of the isobutane, which is returned to the oxidation zone, and the remaining mixture is fed to the epoxidation zone.

5. The method according to p. 1, wherein selected of epoxide stream containing predominantly oxide 2-methyl-2-butene, is subjected to catalytic decomposition at elevated temperature, preferably in the presence of water vapor, followed by separation of isoprene from the reaction mixture.

6. The method according to p. 1, characterized in that the oxide 2-methyl-2-butene initially converted into unsaturated alcohol isomerization in the presence of a catalyst with prevailing basic properties or glycol by hydration in the presence of an alkaline or acidic catalyst with subsequent dehydration of the obtained unsaturated alcohol or glycol in the isoprene in the presence of an acidic catalyst.

7. The method according to p. 1, characterized in that as the acidic catalyst used sulfonation N+-form.

 

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The invention relates to a method of producing isoprene from isamuanoguchi4hydrocarbon mixtures and formaldehyde by chemical transformations in the presence of acid water-soluble and/or solid catalyst in at least three reaction zones, the first of which carry out the extraction isobutene from hydrocarbon mixtures by hydration, the second is the formation of intermediates that are able to further decompose into isoprene, and the third decomposition intermediates and subsequent separation obtained in this zone, the reaction mixtures and recycling at least part of the selectable isobutene in the area of synthesis intermediates, with part of the source of formaldehyde is fed to the area extraction isobutene, the reaction mass is specified zone rasclaat water and organic flow, water flow, containing at least tertbutanol, 3-methylbutanol-1,3 4,4-dimethyldioxanes-1,3, and the rest of the source of formaldehyde is directed to the zone of the synthesis intermediates of synthesis intermediates deduce aqueous and organic streams that are sent to the zone of decomposition may previously passing through the zone of hydrolysis, and the organic flow zone extraction isobutene served in the node Otho the l and 4.4-dimethyldioxanes-1,3, directed to the area of synthesis intermediates, and/or in the zone of expansion, and/or in the zone of hydrolysis

The invention relates to a method of producing isoprene based on the interaction of formaldehyde and isobutene and/or tert-butanol, carried out in the presence of an acid catalyst and water at elevated temperatures in two successive stages, the first of which carry out the synthesis of intermediates and in the second stage, carry out the decomposition of intermediates in a mixture with other components present in the reaction mass of the first stage, the selection from the top of the reactor of the second stage of the reaction products and parts of water and the release of the reaction products of isoprene, which consists in the fact that the decomposition of intermediates is carried out in a vertical apparatus, having in the lower part of the heated shell and tube zone with the number distributed over the cross section of the tubes is not less than 10, and above her reaction zone, a built-in tube space s & t zone and containing the liquid from the top of the specified reaction zone and/or connected with her separation zone carry out the forced recirculation of the liquid in the lower part of the said apparatus, a built-in tube space

The invention relates to a method of producing isoprene-based liquid-phase interaction of formaldehyde and isobutene by acid catalysis in the presence of water at elevated temperatures, including two serial stages of chemical conversion, the first of which is carried out mainly in the synthesis of intermediates and in the second stage, carry out the decomposition of the intermediates with the formation of isoprene displayed in the composition of the steam flow, and carry out at least the subsequent separation of the reaction products and decomposition intermediates carried out in a reaction system comprising at least heated through the tube space of the shell-and-tube reaction zone and connected with its tubular space test facility reaction zone, the volume of liquid in which at least 1.2 times, preferably 1.5-3 times greater than the volume of liquid in the tube shell-and-tube reaction zone

The invention relates to catalysts for the production of liquid hydrocarbons from dimethyl ether

The invention relates to the production of isoprene, which is used as a monomer in the production of synthetic rubber

The invention relates to the production of isoprene used in the manufacture of synthetic rubber
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