Method of producing methyl-tret-butyl and methyl-tret-amyl ethers

专利摘要:
The invention relates to ethers, in particular the preparation of methyl tert-butyl and methyl tert-amyl ethers, which are used as high-octane additives to motor fuels. The goal is to reduce energy costs. Obtaining the desired products are from methanol and a mixture of hydrocarbons containing tert-olefin at 40–70 ° C and a pressure of 10–15 mtm in the presence of a macroporous sulfonated cation-exchange resin based on a copolymer of styrene and divinylbenzene. The target products are obtained in the form of a mixture with unreacted hydrocarbons and methanol by distillation of this mixture with the separation of the target product as a cube, and a mixture of unreacted hydrocarbons and methanol as a distillate. Distillation is carried out at a pressure of 1.2-5 atm, the distillate is cooled, and from a cooled mixture containing 1.6-2.1% of methanol and unreacted hydrocarbons, methanol is passed, passing the mixture through an absorber filled with gel-like or macroporous cation exchanger at 22- 25 ° C and a pressure of 1-5 atm and a load on the absorbent of 1.2–20 kg / kg of absorbent per 1 hour. After saturation of the absorbent, methanol is desorbed with a fresh portion of the hydrocarbon mixture containing tert-olefin at 35 - 50 & ° C and a pressure of 1–20 atm and an absorbent load of 1.85–25 kg / kg asborbent per hour with the ratio of absorption and desorption rates 1: (1.23-2.5). 3 tab. i С /) i4; ib СП СП
公开号:SU1456006A3
申请号:SU823452911
申请日:1982-06-17
公开日:1989-01-30
发明作者:Гервиг Йонс；Шейф Ганс-Фолькер；Шлеппингхофф Бернгард；Михаель Ланге Петер
申请人:Эх Эрдельхеми Гмбх (Фирма)；Байер,Аг (Фирма)；
IPC主号:

专利说明:

one
The invention relates to an improved method for the preparation of methyl tert-butyl and methyl tert-amyl ethers, which are used as high-octane additives to motor fuels.
The purpose of the invention is to reduce energy costs.
The proposed method is illustrated by the examples below.
Example 1. A heated dip reactor with an internal diameter of 5-20 mm is filled with a macroporous containing sulfonic acid groups, a copolymer of styrene and divinylbenzene in the hydrogen form (crosslinked 18% divinyl
cm
1456006
benzene, total capacity-1.4 eq. / l, commercial product levatit SSCH 118 (Bayer AG, Germany), the amount of which is calculated by the amount of starting material to achieve a weight hourly loading of the catalyst equal to 1. The temperature control is carried out using - measuring instruments located along the reaction tube at a distance of 100 mm from each other. At a reaction temperature and controlled by means of an appropriate adjustment, a pressure of 15 bar passes a mixture of 100 g / h of raffinate I (see Table 1) and 26.95 g / h of methanol through the catalyst. The reaction product exiting the reactor is fed to a cooled intermediate separator.
Using gas chromatography, the composition of the initial stream and air stream is summarized in
ten
15
20
the temperature and load of the absorbent is 1.1, and the desorption of methanol-free C 4 (raffinate I) hydrocarbon stream at a pressure of 20 bar and a load of absorbent 1.85 on the methanol-absorbing resin: methanol free from methanol and switching the reactors to the appropriate cycle.
The methanol content in the absorption and desorption streams is monitored by continuous gas chromatographs. Since an absorbing gum containing methanol is used, it is first used to desorb methanol to the absorbent gum a washing stream consisting of C I refined (iso-butene, 47.2 wt.%, N-butenes 41.1 wt.%. % and butane 11.7 wt%). Desorption is carried out at a pressure of 20 bar with a supply of 1250 mp of the washing stream — At 1 h. Thus, the ratio of the absorption rates and de
sorption is 1: 2.5. Content The degree of conversion of iso-butene is soy-25 methanol in the output of desorption is 98.1% with a molar ratio of iso-butene to methanol equal to
1: 1.
840 g / h of the product stream listed in Table 1 of the composition is fed to a distillation column under pressure, in which, at a pressure of 5 bar, 351.82 g / h C is obtained as the raffinate II with a methanol content of 2.1 wt.%, and as a bottom product - 488.18 g / h of composition,%: 97.5 methyl-tert-butyl ether and 2.5 oligomers. The main stream of the distillation stage is fed to the continuous absorption of methanol to the equipment described below.
The absorption unit consists of two parallel-connected, alternately operating, heated reactors with double casings having a length of 140 cm with an internal diameter of 25 mm and each containing 680 cm of macroporous, weakly basic styrene-divinyl benzyl-resin moistened with methanol (commercial product 62 Bayer AG / HGF spherical shape (diameter 0.3-1.5 mm), both reactors are interconnected through a piping system so that the absorption of methanol from the C 4 hydrocarbon stream (pa iiat II) may be carried out at a pressure bar.
thirty
In the first reactor, the C 1 raffinate first amounts to more than 5% by weight and drops to 0.1% by weight over the first hour. After 1.5 hours (inclusive of 0.5 hours for preheating), the desorption process of the first layer of absorbent resin is over. After switching the wash stream to the second layer by absorbing resin, the product stream, into the overhead product of the distillation stage, is fed to the first absorbent layer to separate the methanol, This product stream has the following composition, wt.%:,,
iso-butene 1.6; n-butenes 74.7; butanes 21.5; methanol 2.1; the balance is 0.1.
40
45
50
55
750 ml / h of the product stream is fed to the absorbing layer of the resin at 22 ° C. and 5 bar pressure. The raffinate C d II outgoing from the absorption reactor contains less than 0.1 wt.% Of methanol for 2.5 hours and only after 3 hours the methanol content reaches 1 wt.%. absorption reactors switch. Switching continues every 3 hours for 20 days without changing the absorption effects. At the same time, the C4 II raffinate has the following composition, wt%: iso-butene 1.7; n-butenes 76.2; butanes 21.9; methanol 0.1; the balance is 0.1.
five
0
the temperature and load of the absorbent is 1.1, and the desorption of methanol free from methanol with a C 4 (raffinate I) hydrocarbon stream at a pressure of 20 bar and a load of absorbent 1.85 on the absorbing resin: methanol and switching the reactors to the appropriate cycle.
The methanol content in the absorption and desorption streams is monitored by continuous gas chromatographs. Since an absorbing gum containing methanol is used, it is first used to desorb methanol to the absorbent gum a washing stream consisting of C I refined (iso-butene, 47.2 wt.%, N-butenes 41.1 wt.%. % and butane 11.7 wt.%). Desorption is carried out at and at a pressure of 20 bar with a flow rate of 1250 mp of the rinsing flow at-1 hour. Thus, the ratio of the rates of absorption and desorption is 1: 2.5. The methanol content in the desorption effluent
In the first reactor, the C 1 raffinate first amounts to more than 5% by weight and drops to 0.1% by weight over the first hour. After 1.5 hours (inclusive of 0.5 hours for heating), the desorption process of the first layer of absorbent resin is over. After switching the wash stream to the second layer by absorbing resin, the product stream, which is the main product of the distillation stage, is fed to the first absorbent layer to separate methanol. This product stream has the following composition, wt%:,,
iso-butene 1.6; n-butenes 74.7; butanes 21.5; methanol 2.1; the balance is 0.1.
750 ml / h of the product stream is fed to the absorbing layer of the resin at 22 ° C. and 5 bar pressure. The raffinate C d II outgoing from the absorption reactor contains less than 0.1 wt.% Of methanol for 2.5 hours and only after 3 hours the methanol content reaches 1 wt.%. 0 Then the flush stream and the stream of raffinate II on both reactors switch. Switching continues every 3 hours for 20 days without any change in absorption effects. At the same time, the C4 II raffinate has the following composition, wt%: iso-butene 1.7; n-butenes 76.2; butanes 21.9; methanol 0.1; the balance is 0.1.
514560066
The consumption of steam is 0.4 t / 1t methyl tert-speeds of absorption and desorption of the c-butyl ether, the flow rate of the water 10 m 71 t is 1: 1.23. Withdrawn from stage
methyl tert-butyl ether. Electricity consumption 3.65 kW / h.
Example 2. In the apparatus described in Example 1, 100 g / l of a partially hydrogenated thermal cracking hydrocarbon C stream (gas flow) containing 20% by weight of the isamylene is reacted with 8.6 g / h of methanol per 110 g strongly acidic, containing elemental palladium, macroporous cation exchanger (0.75 g palladium per 1 liter of cation exchanger) at 70 ° С and pressure 10 bar. According to gas chromatography, the product stream (108.6 g / h) has the following composition, wt% (g / h): iso-amylenes 4.1 (4.45); tertiary amyl methyl ether 20.9 (22.70): methanol 1.2 (1.30 other hydrocarbons C 72.1 (78.30); higher esters + hydrocarbons 1.7 (1.85).
Conversion of iso-amylenes 78 wt.%.
After intermediate storage, the product stream of the specified composition is fed to the distillation column, operating at a pressure of 1.2 bar and temperature desorption, the product contains methanol through: 1 h 6.1 g / h (1.62%), 2 h - 2.0 g / h ( 0.54%), 3 hours - 0.2 g / h
: (0.05%),
The cycle of absorption - desorption is repeated 5 times, and the degree of absorption and
10 desorption of methanol during this time is not reduced.
The steam consumption is 0.29 tons, the water consumption is 12 m per 1 ton of methyl tert-amyl ether. Electricity consumption 15 3.9 kW / h.
An example of a C3K-1KB absorption apparatus described in Example 1 is a stream of hydrocarbons C, obtained as the main product of
20 races according to example 2 are passed through absorbent resins to remove methanol. For desorption, an initial stream of hydrocarbons Cj is used, having a composition similar to that of
25 ku in example 2.
Absorption and desorption effects obtained with gas chromatography on various absorbers Absorption and desorption effects obtained with gas chromatography on various absorbers35
in the upper part of 40 ° С, in the middle of the absorbing resins are given in table 3, parts of 86 ° С and cubed. At the same time, tert-amyl ether (TAMG) with a purity of 95%, containing 5% by weight of higher esters and hydrocarbons, is taken as a side stream. Unreacted hydrocarbons Cj and 1.6 May / methanol are taken as the head product. This is the head product (300 g / h) at 25 ° C and a pressure of 1 bar is passed through 15 g of the ion exchanger used in Example 1. In this case, the absorbent load is 20. The apparatus is the same as in Example 1. The composition of the overhead distillation stream at the outlet of the absorber is RESINS analyzed by GLC at regular intervals.
The results obtained when the absorbent is operated for 3 and 3.5 hours are given in Table 2.
40
45
50
Examples 3-11 use the following ion exchangers:
Example 3 - SC 102, gel stitched and styrene-divinylbenzene to a resin with sul phonic acid groups, strongly acidic in the form
example 4 - CNP 80, macroporous,
slightly acid crosslinked acrylic acid cation cation;
Example 5 - DN H, condensate based on phenol and formaldehyde with sulfonic acid groups
Example 6 - SPC 118, as SC 102, but macroporous;
Example 7 - MP 62, macroporous, synthetic styrene-divinyl benzene resin with dimethylbenzylamine groups;
Then the head stream is fed to the second output of the absorbent resin. The desorption of methanol from the first layer of absorbent resin is carried out at 50 ° C, a pressure of 5 bar and an absorbent load of 25, using the starting C5 hydrocarbon mixture as a wash stream of 370 g / h. So the ratio
Desorption the product contains methanol through: 1 h 6.1 g / h (1.62%), 2 h - 2.0 g / h (0.54%), 3 h - 0.2 g / h
(0.05%),
The cycle of absorption - desorption is repeated 5 times, and the degree of absorption and
desorption of methanol during this time is not reduced.
The steam consumption is 0.29 tons, the water consumption is 12 m per 1 ton of methyl tert-amyl ether. Electricity consumption 3, 9 kW / h.
An example of a C3K-1KB absorption apparatus described in Example 1 is a stream of hydrocarbons C, obtained as the main product of
The races according to Example 2 are passed through absorbent resins to remove methanol. For desorption, an initial stream of hydrocarbons Cj, having a composition similar to that in Example 2, is used.
The absorption and desorption effects obtained using gas chromatography on various absorbent resins are given in Table 3,
five
on the accessing resins are given in table 3,
0
five
0
five
In examples 3-11, the following ion exchangers are used:
example 3 - SC 102, a gel-like crosslinked styrene-divinylbenzene-resin with sulfonic acid groups, strongly acidic, in the form
example 4 - CNP 80, macroporous,
slightly acid crosslinked acrylic acid cation;
Example 5 - DN H, condensate based on phenol and formaldehyde with sulfonic acid groups;
Example 6 — SPC 118, as SC 102, but macroporus;
Example 7 - MP 62, macroporosity, scandinated styrene-divinylbenzene resin with dimethylbenzylamine groups;
Example 8 - MP 500, strongly based
macroporos styrene divininbenzene resin type
I;
Example 9 - MP 504, strongly based
gel type styrene-divinylbenzene resin type I;
Example 10-M 600, with a basic helium styrene-divinyl benzene type II resin; Example 11 - XAD 12, styrenedivinyl benzene ion exchanger with N-oxide groups.
The resins of examples 3-11 are commercial products.
porous sulfonated cation-exchange resin based on a copolymer of styrene and divinylbenzene, to obtain the target products as a mixture with unreacted hydrocarbons and methanol by distillation of the mixture with the separation of the target product in the form of a cube
In examples 3-11, steam consumption is 0.29 tons of Hydrocarbons and methanol in
and water consumption of 10 m per 1 ton of the target product. Electricity consumption 3.8 kW / Che
. So in the proposed
The form of distillate, characterized in that, in order to reduce energy costs, the distillation is carried out at a pressure of the process, the steam consumption is 0.29-15. The distillate is cooled and from ox20
A mixture containing 1.6–2.1% of methanol and unreacted hydrocarbons is saturated with methanol, passes the mixture through an absorber filled with gel-like or macroporous cation exchanger at 22–25 ° C and a pressure of 1–5 atm and the load on the absorbent 1, t -20 kg / kg of absorbent per 1 hour, and after saturation of the absorbent, 25 inventions are desorbed in fresh portion of methanol
hydrocarbon mixture containing tert-olefin, at 35-50 C and a pressure of 1-20 atm and the load on the absorbent 1.85-25 kg / kg of absorbent per 1 hour with a ratio of the rates of absorption and desorption 1: (1.23-2, five).
About 4 tons, and water consumption - 10-12 m per 1 ton of the target product, whereas in the known method per 1 ton of the target product spend 0.55 tons of steam and 21 mm of water. Electricity consumption in the proposed method is 3.65 -; 3.8kW / h, whereas in the known
4.9kW / h, /
Formula
The method of producing methyl tert-butyl and methyl tert-amine ethers by reacting methanol with a mixture of hydrocarbons containing tert-olefin 5 at 40-70 ° C and pressure, 10-15 atm in the presence of macro30
Composition
iso-butene n-butenes butane methanol
Methyl tert-bu ether (MTBE)
Oligomers and others
a distillate, characterized in that, in order to reduce energy costs, the distillation is carried out at a pressure. The composition of the overhead stream of the product (300 g / h)
Hydrocarbons With Methanol Tertiaryamyl Ether
absorbent load 5. 3) Number of streams; A - 630 g; B - 1260 g; B - J890
Editor M.Kelemes
Tehred L. Oliynyk Proofreader SoShekmar
Order 7460/58 Circulation 352, Subscription
VNShPI State Committee for Inventions and Discoveries at the State Committee on Science and Technology of the USSR 113035, Moscow, Zh-35, 4/5 Raushsk nab.
Table 2
15
TablncvZ

权利要求:
Claims (3)
[1]
Claims 25 A method for producing methyl tert-butyl methyl tert-amyl esters by reacting methanol with a mixture of hydrocarbons containing a tert-olefin C ₄ -C ₅ at 40-70 ° C and a pressure of 10-15 atm in the presence of macroporous sulfonated cation exchange resins based on a copolymer of styrene and divinylbenzene, to obtain the target products in the form of a mixture with unreacted hydrocarbons and methanol by distillation of the mixture with separation of the target product in the form of a cube, and a mixture of unreacted hydrocarbons and methanol in the form of dis tillates, characterized in that, in order to reduce energy costs, the distillation is carried out at a pressure of 1.25 atm, the distillate is cooled and methanol is isolated from the cooled mixture containing 1.6, 2.1% methanol and unreacted hydrocarbons, passing the mixture through an absorber filled with gel or macroporous cation exchange resin at 22-25 ° C and a pressure of 1-5 atm and an absorbent load of 1.1-20 kg / kg of absorbent per 1 h, and after saturation of the absorbent, methanol is desorbed with a fresh portion of the hydrocarbon mixture containing tretolefin, at 35-50 ^ 0 and pressure 1 20 atm and an absorbent load of 1.8525 kg / kg of absorbent per 1 h with a ratio of ₃₀ absorption and desorption rates of 1: (1.23-2.5).
T a b l and c Composition Source stream Flow product g / h McLC "% I I I!1 1 1eleven1 liter111 May. % iso butene 47.22 37,2 0.89 0.7 n-buteny 41.12 32 ^ 4 40.51 31.9 Bhutan 11.66 9.2 11.66 9.2 Methanol 26.95 21,2 1.14 0.9 Methyl — tert-butyl ether (MTBE) - - 70.85 55.8 Oligomers and others. -1.90 1,5
I about
Table 2
The composition of the head stream of the product (300 g / h)
Content, wt.%, Through, h
3,5
Hydrocarbons 97.9293 , 7 293.7 Methanol 1,60.3 (= 0.1%) 0.6 (= 0 , 2%) Tertiary amyl ether 0.51,51,5 fifteen T a b l and c and 3 Absorbent MeOH concentration 1 eluate following the example 3 4 5 1 ⁶ί ⁷i ⁸L .9 I1 10 . - (SC 102) (CNP 80) (DNH ⁺ ) I (SPC 118) I (MP 62) ί (mr 500); (MP 504); (M 600) (KAD 12) MeOH eluate concentration g / h G / h g / h g / h g / h g / hg / h g / h g / h - Absorption B 0.63 2,52 3.15 4.41 0.63 1.892,52 5.04 0.63 Desorption A 26.46 ‘17.64 11.97 13.23 21.42 17.0115.12 10.71 17.64 IN 17.01 10.00 7.56 5.67 11.97 5.675.67 5.04 8.19 in 3.15 1.87 1.26 0.63 3.15 1.851.26 1.89 2,52 Absorption A 0.63 2,52 1.89 2.52 0.63 0.631.26 2,52 0.63 IN 0.63 3.70 3.15 3.78 0.63 2,522,52 4.61 0.63 IN 2.52 5.04 4.41 6.3 0.63 6.35.67 7.56 0.63 Absorption A 25.83 23.31 12.60 11.34 23.94 10.915.75 8.82 17.64 IN 15.12 9.45 6.93 3.70 16.30 10.75.04 3.15 6.30 IN 4.41 2,52 1.89 1.89 3.15 1.891.26 3.15 • Absorption A 0.63 3.15 2,52 3.78 0.63 0.631.26 2.52 0.63 IN 2,52 5.04 5.67 5.04 0.63 3.154.41 6.30 0.63 IN 3.78; 6.3 6.93 7.56 1.26 5.046.30. 7.56 1.89
Π R name. 1)
Absorption :, then! C ₅ hydrocarbons containing 2Z methanol; temperature 25 ° C; Pressure 1 bar; absorbent load 5.
Desorption: the feed stream of hydrocarbons S., temperature 35 * C, a pressure of 1 bar, the load 5. The absorbent ¹
Number of threads: A 630 g; B - 1260 g; B - J890
[2]
2)
[3]
3)

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法律状态:

优先权:

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