A comprehensive method of producing butene-1

 

(57) Abstract:

A comprehensive method of producing butene-1, characterized in that it includes flow C4hydrocarbons in the installation for the separation of butene-1 and return to the same installation of the product stream remaining after processing in section isomerization contact for the purpose of conversion of butenes-2 to butene-1, to purge cyclic paraffins in the processing of hydrocarbons in the vapor phase include a separating installation with molecular sieves. The method makes it possible to blow out a stream of paraffins, containing no olefin, this, in turn, allows almost full use of the available olefins, maximizing thus the production of butene-1. This reduces the concentration of paraffins in the cycle, thus reducing capital and energy costs. 15 C.p. f-crystals, 2 tab., 5 Il.

The invention relates to an integrated method of producing butene-1.

More specifically, the present invention relates to an integrated method of producing butene-1, which contains, together with the CIS - and TRANS-isomers of butene-2 in the product flow C4.

Still more, the present invention relates to maximize the use of fratina-1 from a mixture, which contains it along with CIS - and TRANS-isomers of butene-2. For example, U.S. Patent 4718986 describes the method for the separation of butene-1 contained in the flows of products C4of different origin, for example, in the flow of products from plants to cracking in the vapor phase or catalytic cracking, using a suitable regeneration unit. According to this patent, the flow of product C4pre-processed to remove isobutene and butadiene and possible acetylene hydrocarbons, is fed into the apparatus for extracting butene-1, consisting of the first distillation column, from the top of which take away a fraction of isobutane, isobutane containing not only a significant amount of butene-1. The product from the bottom of the first column serves the second column from the upper part of which is extracted butene-1 of high purity (> 99%), while butane fraction containing mainly n-butane, CIS - and TRANS butenes-2 and butene-1, away from the bottom. In fact, n-butane has an intermediate relative volatility between the volatility of butene-1 and CIS - and TRANS-isomers of butene-2; therefore, its removal leads to the complete destruction of butene-2, along with a certain amount of butene-1.

Shadowmist, as for blowing the top of the first distillation column, and by blowing the bottom of the second distillation column.

Another disadvantage of the known in the practice of the method is that there is no disposal of CIS - and TRANS-butene-2, contained in the output stream of product C4who, therefore, must be regenerated separately.

Applicants have discovered a new method of producing butene-1 from a stream C4-hydrocarbon product mainly contains no isobutene, and this method overcomes the disadvantages of the known technology. In fact, this method involves combining section for extracting butene-1 known way with isomerization installation for the conversion of CIS - and TRANS-butene-2, contained in exhaust streams, butene-1 and the return flow isomerizing thus the product section for the extraction of butene-1.

As in the complex method of this kind is possible undesirable accumulation of paraffin hydrocarbons, n-butane and isobutane, in the cycle include the installation for the separation of paraffins.

In more detail, the flow of the blown products coming from partitions to retrieval of butene-1 containing paraffin aktivna adsorption of olefins. Adsorbed thus olefins can be regenerated by desorption and then be put back into the cycle. This way you can regenerate the quantity of butene-1 and CIS - and TRANS-isomers of butene-2 which might otherwise be lost in the flow of the blown products.

This result can now be achieved by reducing the cost of the process, if done in the Department of molecular sieves in the vapor phase, since the operation in the liquid phase may give undesirable results due to the required complexity of the installation.

Therefore, the present invention relates to an integrated method of producing butene-1, which includes:

a) fresh stream C4hydrocarbons consisting mainly of linear butenes, butane and possibly butadiene, along with possible traces of acetylene compounds, together with return back into the cycle the product stream rich in butene-1 and contains probable traces of butadiene, in the section selective hydrogenation of butadiene and possible acetylene compounds;

b) flow hydrogenated products, mainly containing butadiene and acetylene compounds, in the section for the separation of butene-1 with the aim pleasego mainly of paraffins and olefins (butene-1, butenes-2);

C) flow residual hydrocarbons or their fractions in the vapor phase in a separating section with molecular sieves for the separation of paraffins (consisting mainly of butane) from olefins (consisting mainly of butene-1 and butenes-2), the separation of olefins and blowing paraffins;

d) flow of hydrocarbons containing the separated olefins together with a possible faction is not loaded on the stage (C), section isomerization contact for the purpose of conversion of CIS - and TRANS butenes-2 to butene-1;

d) the return flow of isomerized products in the selective hydrogenation section (a) after mixing with fresh stream C4of hydrocarbons.

Alternative comprehensive method of producing butene-1 includes:

a') a fresh stream C4hydrocarbons consisting mainly of linear butenes, butane and possibly butadiene, and possible traces of acetylene compounds, together with returned back into the process stream, rich in butene-1 and contains probable traces of butadiene, in the section selective hydrogenation of butadiene and possible acetylene compounds;

b') flow hydrogenated hydrocarbons or their fractions in the vapor phase in a separating section with molecular and butenes-2), the separation of olefins and blowing paraffins;

in') the flow of hydrocarbons containing the selected olefins together with a possible faction is not loaded on the stage (b'), in the section for the separation of butene-1 in order to obtain a stream comprising butene-1 of high purity (> 99%), and the remaining flow of hydrocarbons consisting primarily of paraffins and olefins (butene-1 and butene-2);

g') flow remaining hydrocarbons in the section for the isomerization of contact for the purpose of conversion of CIS - and TRANS butenes-2 to butene-1;

d') the return flow of isomerized products in the selective hydrogenation section (a') after mixing with fresh stream C4of hydrocarbons.

Fresh flow C4the hydrocarbons used in the method of the present invention mainly contains no isobutene, as it does, for example, from plants to obtain tert-butyl ether (MTBE) and consists of isobutane, n-butane, butene-1, butene-2 (TRANS - and CIS-), butadiene and possibly small amounts of acetylene hydrocarbons and C3and/or C5of hydrocarbons. This thread is basically should not contain isobutene, which otherwise could contaminate the final product butene-1, as isobutene and butene-1 are SUB>4hydrocarbons before serving in the installation of selective hydrogenation stage (a) or (a'), usually using etherification installation, in which the alkyl tert-butyl ether, for example, methyl tert-butyl ether (MTBE) or ethyl tert-butyl ether (ETBE), as disclosed in U.S. patents 3979461, 4039590, 4071567, 4447653, 4465870, 4475005, the UK patent 2116546 or published European patent 470655.

At the end of treatment in order to remove and/or exclude isobutene stream C4products may contain (in addition to a small number of C3and C5constituting, for example, from 0 to 5 weight percent) of about 0.5 to 55 weight percent isobutane; 1 to 30 weight percent n-butane; 0 to 60 percent by weight of butadiene; linear butenes in addition to 100%. The stream may also contain other components at level 0 - 5000 million shares, such as MTBE, ETBE, dimethyl ether, tert-butyl alcohol, methanol, ethanol, water, etc.

Section selective hydrogenation eliminates acetylene compounds that may be present in fresh load and transform BUTADIENES in linear butenes.

If no fresh download or returned back into the cycle, the flow does not contain butadiene, you can exclude set is ubuu installation. For example, you can use the installation fractional distillation, installation extractive distillation or installation, operating by adsorption on molecular sieves. It is preferable to install fractional distillation, usually consisting of two distillation columns mounted in series. In a typical location in the first column (upper part) carry out the separation is still present in the feed stream of isobutane (isobutane vapor), while in the second column, which loads the bottom product of the first column, in its upper part to receive the butene-1 with a degree of purity higher than 99%, and in the lower part of the column to receive the stream rich in the remaining n-butane, CIS - and TRANS-isomers of butene-2 and containing butene-1 (pair butene). The operating conditions are described in U.S. patent 4718986 and Canadian patent 1232919.

In an alternative embodiment, the separation of butene-1 by way of fractional distillation, the position of the columns may be reversed. With this arrangement, from the bottom of the first column output stream of butene, while in the lower part of the second column, downloadable product from the upper part first, get butene-1 of high purity, and its upper part display isobutane (partnach substances, including paraffin hydrocarbons, mainly n-butane and isobutane. In the section you can enter either the flow of the remaining hydrocarbons coming from the section for separating butene-1 and consisting, for example, of the amount of isobutane stream and butenes stream, or the stream, leaving a section of hydrogenation. In both cases, you can enter all the product stream, or a fraction containing more than 5 weight %.

In the method of the present invention can be used in any molecular sieve type zeolites having a selectivity relative to the two olefinic linkages. For example, it is possible to apply the compounds corresponding to General formula

(Cat2/nO)xMe2O3(SiO2)y,

where

Cat represents a cation with a valence of "n" that can be exchanged with calcium (Ca), such as sodium, lithium, potassium, magnesium, and others;

X is a number from 0.7 to 1.5;

Me is boron or aluminum;

y is a number from 0.8 to 200, preferably from 1.3 to 4.

The preferred zeolites of type X and Y with a particle size of from 0.1 to 3 mm Such zeolites allow you to get the coefficient of the selectivity of olefins/paraffins of 3 to 12, while the selectivity is defined as

S = (Ro/Po)/(Rpoand Ppin pairs.

Separation of aliphatic hydrocarbons is carried out in the vapor phase at a temperature of from 20 to 180oC, preferably from 70 to 140oC and an absolute pressure of from 1 to 10 bar, preferably from 1 to 5 bar. To guarantee the continuity of the process of the present invention, it is preferable to use at least two sections, mounted in parallel so that while one section is in phase adsorption, the other was in the desorption phase. Desorption is carried out by elution of olefins adsorbed on molecular sieves, desorbers agent, such as aliphatic hydrocarbons, such as pentane, hexane, heptane, octane, etc. in the vapor phase, followed by distillation of the mixture for the regeneration of olefins.

A separating section with molecular sieves method of the present invention allows to obtain a stream of aliphatic hydrocarbons to purge, almost not containing olefins or olefin content of not more than 5 weight %.

In the section for isomerization, which provide a stream of olefins, leaving the separating section with molecular sieves, or thread the remaining uglevodosoderjati can be for example, the method described in U.S. patent 4814542, using as catalyst the product on the basis of aluminum oxide and oxides of the metals.

The output section isomerization get a product stream rich in butene-1, may contain traces of butadiene, which is recycled back into the selective hydrogenation section. Any possible generated in this phase, the C3-and C5+hydrocarbons together with the hydrocarbons may be present in fresh boot, removed, for example by distillation.

If a partition for separating butene-1 consists of the installation of fractional partitions working with two serially mounted distillation columns, a comprehensive method of producing butene-1 may include the following stage of the process:

i) fresh stream C4hydrocarbons consisting mainly of linear butenes, butane and possibly butadiene, along with possible traces of acetylene compounds, together with return back into the cycle the product stream rich in butene-1 and contains probable traces of butadiene, in the section selective hydrogenation of butadiene and possible acetylene compounds;

ii) feeding the hydrogenated stream of uglevodorov who were mainly of butane) from olefins (consisting mainly of butene-1 and butenes-2), regeneration of olefins and blowing paraffins;

iii) flow of hydrocarbons containing the separated olefins, together with factions, not loaded on the stage (ii), in the first column section for separating butene-1, and this section consists of two distillation columns mounted in series;

iv) returning back into the separating section with molecular sieves (ii) the product stream from the top of the first column of stage (iii), consisting mainly of isobutane and butene-1, while the flow of product from the lower portion flows into the second distillation column;

v) removal from the upper part of the second column of a stream, consisting mainly of butene-1 of high purity (> 99%), and the direction of flow of the product from the bottom of the second column, consisting mainly of butenes-2, section isomerization contact for the purpose of conversion of CIS - and TRANS-isomers of butene-2 to butene-1;

vi) the return flow of isomerized products in the selective hydrogenation section (i) after mixing with fresh stream C4of hydrocarbons.

In an alternative embodiment, the separation of butene-1 by way of fractional distillation, the position of the columns may be reversed. With this arrangement of the downloadable product from the bottom of the first, get butene-1 of high purity, and from the upper part of the display isobutane (pair isobutane). With this arrangement, an integrated method of producing butene-1 may include the following stage of the process:

I) fresh stream C4hydrocarbons consisting mainly of linear butenes, butane and possibly butadiene, along with possible traces of acetylene compounds, together with return back into the cycle the product stream rich in butene-1 and contains probable traces of butadiene, in the section selective hydrogenation of butadiene and acetylene possible connections:

II) flow hydrogenated hydrocarbons or their fractions in the vapor phase in a separating section with molecular sieves for the separation of paraffins (consisting mainly of butane) from olefins (consisting mainly of butene-1 and butenes-2), regeneration of olefins and blowing paraffins;

III) flow of hydrocarbons containing the separated olefins, together with possible faction is not loaded on the stage (II) in the first column section for separating butene-1, and this section consists of two distillation columns mounted in series;

IV) flow of product from the bottom of the first column of stage (III) in butene-1, while the flow of product from the upper part comes in the second distillation column;

V) removal of the lower part of the second column of the product flow, consisting of butene-1 of high purity (> 99%), and the direction of flow of the product from the top of the second column, consisting mainly of isobutene and butene-1, a separating section with molecular sieves (II);

VI) the return flow of isomerized products in the selective hydrogenation section (I) after mixing with fresh stream C4of hydrocarbons.

A comprehensive method of producing butene-1 of the present invention can be better understood by referring to the block diagrams shown in Fig. 1 to 4, which are illustrative but not restrictive of his ways, and to the block diagram of Fig. 5, which separately represents an illustrative version separating sections with molecular sieves.

In Fig. 1 by the letters A, B, C and D, respectively designated section for separating butene-1 A, section of molecular sieve separating the hydrocarbon-B, section isomerization connection C and the selective hydrogenation section D. the product Stream (3), consisting of the sum of fractions of C4hydrocarbons (1) and fraction (16), out of a facility for the isomerization of C and . arereasonably hydrogen, if present, are blown off with a stream of the product (5).

Stream is hydrogenated product (4) refer to the section for separating butene-1 A. After the separation of butene-1 (8) using well-known methods (not shown), for example, the method described in U.S. patent 4718986, the remaining fraction of hydrocarbons (10) send (entirely or partially) in a separating section B with molecular sieves. Partial separation of part of the above fraction remaining hydrocarbons pass from the separating section B, dashed line (11).

Paraffins (13) and the product stream (14), consisting mainly of butene-1, CIS - and TRANS-isomers of butene-2 and the remaining butane, is removed from the separating section B. the product Stream (14), combined with the possibly existing thread (11), passed section B, form a product stream (15), which comes in isomerization section C. Stream (16), rich in butene-1, deduce from it, and return back to the selective hydrogenation section D.

Any C3-and C5+the hydrocarbons formed by isomerization or present in the loading of C4(1), deduce, by (17) and (18).

In Fig. 2 the separating section B is located in front of semisonic illustrates the details of the section A. Section A consists of two distillation columns A' and A". In the first column A' enter product flow (4) arising from the selective hydrogenation section, and in its upper part to receive a flow of product, consisting mainly of isobutane. The second column is A" serves the flow of product (7) from the bottom of column A', receiving in the upper part of the column A stream (8) of butene-1 of high purity (>99%), and in the lower part of the stream (9), consisting mainly of butenes-2 and n-butane.

Streams (6) and (9) are combined into stream (10) and serves in a separating section B with molecular sieves.

Fig. 4 is an expanded diagram of the above-described Fig. 2 option section A. in fact, at this location, the remaining fraction of hydrocarbons that come out of the section A, is not fully served in section isomerization C. Specifically, the flow of isobutane (6) extending from the upper part of the column A', return back to the separating section B with molecular sieves, while the flow of the product (9) exiting the bottom of column A, serves in section isomerization C.

A separating section B in Fig. 5 includes adsorption/desorption installation D and two distillation columns E and F.

For continuous operation it is also possible to have two at the output two streams D1 and D2.

In the phase of adsorption obtained product flow D1 contains almost no olefins, it is sent to a distillation column E to branch Stripping agent E2, which is put back into the cycle, from exhaust butane fraction E1.

In the desorption phase olefin fraction D2 is separated and sent to a distillation column F for the Department of butene fraction F1 (which let back into the cycle) from the Stripping agent F2, which is returned back to D.

In the complex process of obtaining butene-1 the method of the present invention provides the ability to blow out a stream of paraffins, containing no olefin. This in turn allows almost full use of the available olefins, maximizing thus the production of butene-1. In addition, it reduces the concentration of paraffins in the cycle, thus reducing capital and energy costs.

For a better understanding of the present invention and its possible embodiments below are some illustrated, but not restrictive examples.

Example 1.

Please refer to the enclosed chart of Fig. 3 and the corresponding table. 1 with quantitative data for the performance of butene-1 primer the massive job %

C3- 0,03

isobutan - 0,06

butene-1 - 37,61

butene-2-TRANS - 20,70

butene-2-CIS - 16,77

isobutane - 4,89

n-butane - 17,78

butadiene - 1,71

acetylene products - 0,45

This stream is combined with the return back to the loop flow (16) having a flow rate of about 2930 g/h flow (3) serves in section hydrogenation of butadiene D, in which butadiene is almost completely transformed into a linear butenes, while a small portion is converted to n-butane. Acetylene compounds mainly hydronaut in this section. Stream is hydrogenated products (4) served in a partition for separating butene-1 (A). With this arrangement of the blocks, as indicated in Fig. 3, the flow of the product (4) is fed to the first distillation column A', the top of which is formed isobutane (6) with a capacity of about 240 g/h, the flow of isobutane consists mainly just isobutane, all C3hydrocarbons contained in the stream (4), and butene-1, along with natural and low content of n-butane and butenes-2.

The product stream (7), practically does not contain isobutane, served in column A, from the upper part of which receive about 730 g/h of butene-1 with a degree of purity higher than 99% (8). Product flow (9) are combined into stream (the lo 20 weight % paraffins. About 30% of this thread away, bypassing the section B, while the remaining part (12) enters the section B, which operates at 130oC and a pressure of 4 bars. As molecular sieves used about 4000 cm3zeolite X pellets of 1/16 inch extrudate, as a Stripping agent for the adsorbed olefins using n-hexane in the vapor phase (about 5000 g/h). After separation of the Stripping agent by distillation product flow (13), consisting mainly of 288 g/h aliphatic hydrocarbons, blow these paraffins in the number of 96.6 percent. In the stream (15) the content of aliphatic hydrocarbons is reduced to about 13 weight %. This stream is then fed to the section isomerization connection, which is the conversion of the butenes-2 to butene-1 and other products belonging to groups C3-and C5+. These by-products are removed (17) and (18), and the obtained fraction (16) is recycled back into the section hydrogenation D.

Example 2.

Carry out a procedure similar to that of example 1, but corresponding to the diagram of figure 4, and the quantitative data presented in the table. 2.

1. A comprehensive method of producing butene-1 by filing the original thread C4uglevodorov is of butadiene and acetylene possible connections and flow hydrogenated products almost not containing butadiene and acetylene compounds, in the section for the separation of butene-1 to obtain the product stream consisting of butene-1 with a degree of purity higher than 99%, and the remaining hydrocarbons consisting primarily of paraffins and olefins butene-1 and butenes-2, characterized in that the remaining hydrocarbons or part of them served in the vapor phase section of the separation on a molecular sieve (b') for separating paraffins, consisting mainly of butane, from olefins, consisting mainly of butene-1 and butenes-2, obtaining separated olefins and output process paraffins separated olefins together with possible part of the remaining hydrocarbons are not included in the section separation on a molecular sieve, serves in section isomerization to convert CIS - and TRANS-butenes in the butene-1 and the flow of isomerized products return in section selective hydrogenation after mixing with the original thread C4of hydrocarbons.

2. The method according to p. 1, characterized in that section selective hydrogenation to remove acetylenic compounds possibly present in the feedstock, and butadiene transform in linear butenes.

3. The method according to p. 1 or 2, characterized in that the separation of butene-1 in CE is I, that fractional distillation is carried out using two successive distillation columns, at the top of the first one separate stream of isobutane, consisting mainly of isobutane, and the bottom product of this column serves the second distillation column, getting at the top of the second column a product stream comprising butene-1 with a degree of purity higher than 99%, and in its lower part butenova stream enriched in the remaining n-butane, CIS - and TRANS butenes-2 and containing butene-1.

5. The method according to p. 3, wherein the fractional distillation is carried out using two successive distillation columns, from the bottom of the first receive butenova stream enriched in the remaining n-butane, CIS-, TRANS-butenes-2 and containing butene-1, and the top product of this column serves the second distillation column, receiving from the upper part of the stream of isobutane, and in the lower part of the discharge product, consisting of butene-1 with a degree of purity greater than 99%.

6. The method according to any of the preceding paragraphs, characterized in that section of the separation of the molecular sieve serves the remaining hydrocarbons in the amount of more than 5% wt. from their common thread.

7. The method according to any of the firm in relation to the olefinic double bond.

8. The method according to p. 7, characterized in that the molecular sieve has a General formula

(Cat2/nO)xMe2O3(SiO2)y,

where Cat represents a cation with a valency of n, which can be exchanged for calcium, such as sodium, lithium, potassium, magnesium and other; x is a number from 0.7 to 1.5; Me is boron or aluminum; y is a number from 0.8 to 200, preferably from 1.3 to 4.

9. The method according to any of paragraphs.1 to 8, characterized in that the molecular sieve is a zeolite of type X and Y with a particle size of from 0.1 to 3 mm

10. The method according to any of paragraphs.1 to 9, characterized in that the coefficient of the selectivity of olefins/paraffins zeolite has a value of from 3 to 12.

11. The method according to any of paragraphs.1 to 10, characterized in that the separation of the molecular sieve is carried out at a temperature of from 20 to 180oC and an absolute pressure of from 1 to 10 bar.

12. The method according to any of paragraphs. 1 - 11, characterized in that the separation of olefins in the partition separating the molecular sieve is carried out by elution of molecular sieves desorbers agent in the vapor phase, followed by distillation thus obtained mixture.

13. The method according to p. 12, characterized in that section for separation of butene-1 includes a CLASS="ptx2">

14. The method according to p. 12 or 13, characterized in that it comprises the following stages: serves stream of hydrocarbons containing the separated olefins, together with possible faction is not loaded at the stage b' in the first column section for separating butene-1, consisting of two distillation columns mounted in series; serves the flow of product from the top of the first column, consisting mainly of isobutene and butene-1 in a separating section with molecular sieves b', while the flow of product from the lower portion flows into the second distillation column; divert flow from the top of the second column, consisting mainly of butene-1 of high purity (> 99%), and serves the flow of product from the bottom of the second column, consisting mainly of butenes-2, section isomerization contact for the purpose of conversion of CIS - and TRANS-isomers of butene-2 to butene-1.

15. The method according to p. 14, characterized in that the swap column fractionated distillation.

16. The method according to p. 15, characterized in that it comprises the following stages: serves stream of hydrocarbons containing the separated olefins, together with possible faction is not loaded at the stage b' in the first column section for separating butene-1, consisting of two who, ostoja mainly from butenes-2, section isomerization due to conversion of CIS - and TRANS-isomers of butene-2 to butene-1, where the flow of product from the top of the second distillation column, and removing a product stream from the bottom of the second column, consisting of butene-1 of high purity (> 99%), and serves the flow of product from the top of the second column, consisting mainly of isobutane and butene-1, a separating section with molecular sieves b'.

 

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11 cl, 5 dwg

FIELD: chemistry.

SUBSTANCE: invention relates to a method of producing butene-1 via dimerisation of ethylene at pressure 0.5-4 MPa and temperature 50-95°C in the medium of a hydrocarbon solvent in the presence of a catalyst system consisting of trialkyl aluminium - AlR3, in which R is a hydrocarbon radical containing 1-6 carbon atoms, titanium etherate - Ti(OR)4, in which R is a hydrocarbon radical containing 2-6 carbon atoms, in the presence or absence of a modifier - ether. At the end of the dimerisation reaction, a catalyst deactivator is fed into the reactor or into the reaction mass when the reaction mass comes out of the reactor, where the catalyst deactivator used is monoalkyl ethers of ethylene glycol.

EFFECT: use of the method increases selectivity of the process and purity of butene-1, lowers the probability of secondary reactions such as isomerisation of butene-1 into cis- or trans-butene-2, reduces the degree of polymerisation, improves working conditions and improves economic performance of the process.

3 cl, 11 ex, 2 tbl

FIELD: chemistry.

SUBSTANCE: invention relates to a method of producing propylene and butene-1 from ethylene at high temperature in a continuous or periodic mode in the presence of a catalyst deposited on a support. The method is characterised by that the process is carried out at temperature 75-110°C in the presence of a catalyst containing the following in wt %: Re - 5-15, B2O3 - 3-10, γ-Al2O3 - the balance.

EFFECT: use of the present method simplifies the process and increases selectivity thereof during formation of propylene, and also enables to obtain a mixture of propylene and butene-1 as the end product.

2 cl, 6 ex, 2 tbl

FIELD: chemistry.

SUBSTANCE: invention relates to a method of producing 1-butene and isobutene and/or compound(s) thereof with alcohol(s), water, or products of di- and trimerisation of isobutene from a mixture of C4-hydrocarbons, primarily containing 2-butenes, using skeletal and positional isomerisation of 2-butenes and at least rectification, characterised by that catalysed isomerisation of 2-butenes is carried out at temperature ranging from 100°C to 500°C in a common reaction zone where positional and skeletal isomerisation to 1-butene and isobutene take place, or in separate reaction zones, in one of which there is positional isomerisation to 1-butene and in the other there is simultaneous skeletal and positional isomerisation to isobutene and 1-butene; the isobutene formed is extracted from the mixture initially in form of alkyl-tert-butyl ester(s) and/or tert-butanol and/or isobutene dimers and trimers and, optionally, said compound(s) is(are) subjected to catalysed decomposition with release of isobutene, and from the stream(s) in which 1-butene and 2-butenes are predominant, a stream primarily containing 1-butene is separated by rectification and the residue, which primarily contains 2-butenes, is at least partially recycled into the zone where there is skeletal isomerisation.

EFFECT: method enables to obtain 1-butene and isobutene in a common process, which enables to cut the size of the necessary equipment and more rationally organise flow.

11 cl, 8 ex, 3 tbl, 2 dwg

FIELD: chemistry.

SUBSTANCE: method is characterised by contacting a gas stream containing at least one of said hydrocarbons with a dehydrogenation catalyst containing gallium and platinum and deposited on a support made of aluminium oxide or aluminium oxide and silicon dioxide, at reaction temperature in a direct-flow, upward stream with weight ratio of catalyst to hydrocarbon of 5 to 100 in a dehydrogenation reactor, wherein the average contact time of the hydrocarbon with the catalyst in the zone of the dehydrogenation reactor ranges from 1 s to 4 s, and temperature and pressure in the dehydrogenation reactor range from 570 to 750°C and from 41.4 (6.0) to 308 (44.7) kPa (psia); and moving the hydrocarbon and the catalyst from the dehydrogenation reactor into a separation device, wherein the average contact time of the hydrocarbon with the catalyst at reaction temperature in the separation device is less than 5 s, and the full average contact time between the hydrocarbon, catalyst and the formed hydrocarbons is less than 10 s; and moving the catalyst from the separation device into a regenerator, where the catalyst is brought into contact with an oxygen-containing regenerating stream and additional fuel.

EFFECT: method has short contact time between the hydrocarbon and the catalyst.

7 cl, 5 dwg

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