• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
  • 同族专利
  • 引用文献
  • 法律状态
  • 优先权
    • 专利摘要:
    Pure dimethyl ether is prepared by catalytic dehydration of methanol over a gamma -Al2O3 catalyst which preferably contains small amounts of SiO2 and purification of the dehydration product by addition thereof to a distillation column to obtain pure dimethyl ether on certain plates of this column and taking off the pure dimethyl ether and impurities above certain plates of the same column.
    公开号:SU1602392A3
    申请号:SU874203754
    申请日:1987-11-17
    公开日:1990-10-23
    发明作者:Дорнхаген Хорст；Хаммер Хартмут；Майзенбург Эвальд；Хаас Бернд
    申请人:Унион Райнише Браунколен Крафтштофф, Аг (Фирма)；
    IPC主号:
    专利说明:

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    31602392
    The invention relates to chemical technology, in particular to the catalytic dehydration of methanol with the preparation of a high-purity, odorless, dimethyl ether, suitable for use as a spraying agent for cosmetic and household use aerosols.
    The aim of the invention is to improve the quality of dimethyl eLire.
    On league. Figure 1 shows a diagram of an installation for the preparation and purification of dimethyl ether; in fig. 2 - distillation column to obtain a pure one. dimethyl ether; in fig. 3 - the same, with the selection of the side stream.
    According to FIG. 1, fresh methanol is fed through pipe 3 and heat exchangers 4 and 5 into the dehydration reactor 1 by pump 2. The distillation column 6 for obtaining pure dimethyl ether operates in the pressure range corresponding to the pressure in the factor: 1 synthesis /, usually at a slightly lower pressure (it is preferable to work at a pressure difference O t - 10 kg / cm). Limethyl ether is taken from the top of the column 6 as a side fraction 7 in its pure form. Gas from the head of the column 6 enters via line 8 to condenser 9. Reflux into the column: 6 is fed through line 10. The offgas enters through line 11 to the scrubber 12, in which the gas is washed with methanol 13. Flushing is carried out a coil or counter current, however it is preferable to use a counter current. Raw methanol or a bottom product can also be used as a washing liquid. In the latter case, the washing liquid containing dimethyl E11) ir is again supplied to column 6. A small amount. in dimethyl ether enters the reactor 1 through line 14 together with methanol after washing. The exhaust gas is removed through line 15. From the reactor 1, the synthesis product is fed through line 16 through heat exchanger 4 to column 6. Impurities boiling from the column between the boiling point of methanol and dimethyl ether are removed from line 17 which are sent for incineration. The bottom product of column 6, containing mainly methanol and water, enters the separator through line 18. However, as if the pressure was below the pressure of the column. Through line 20, methanol is withdrawn from column 19 and returned to the synthesis reactor. From the bottom of the column, wastewater is piped along line 21. At line 22, impurities with higher boiling points than: methanol are removed from the tea.
    FIG. Figure 2 shows the distillation on column 23 to obtain pure dimethyl ether. The raw material stream from the reactor enters via line 24. Lnsty dimethyl ether selects n lines 25, and impurities are removed along line 26. Gas from the head of column 27 enters condenser 2 Reflux into column 23 is fed via line
    29. The waste gases are removed by line.
    30. The cubed temperature of the column is maintained with the help of 1Schrkl 1:; ionic reboiler 31, and along line 32 the distillation residue is taken from the distillation.
    FIG. Figure 3 shows the distillation on column 33. Food is fed through line 34, and distillate containing impurities comes through line 35 to lake 36, which is equipped with a circulating reboiler 37.
    Limethyl ether from tank 36 of line 38 is returned to column 33. Pure dimethyl ether is taken off
    JJ lines 39. The impurities freed from dimethyl ether are removed from the syst through line 40. The gaseous products of the top of column 33 are fed through line 41 to the condenser 42. The leg 33 is fed through line 43. Exhaust gas is removed through line 44 .
    Example 1. Synthesis was carried out at 270-290 s and a pressure of 10 kg / cm using J 45 catalyst, which contains 0.018 May L SiO. From the product leaving the reactor, almost no-odor pure dimethyl ether is obtained.
    The product coming from the reactor in the amount of 3000 kg / h and containing 65% by weight of dimetylated ether is distilled in two serially connected continuously operating distillation columns, from which the first is equipped with 50 valve trays.
    thirty
    40
    50
    Food - in the first column comes
    .-. 27th plate. (From the head of
    this column 19, working with normal columns). Impurities are taken from the 22nd
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    . or at a slightly elevated or reduced pressure, however, as a rule, the pressure is lower than the pressure of column 6. Through line 20, methanol is withdrawn from column 19 and returned to the synthesis reactor. Wastewater is removed from the bottom of the column via line 21. In line 22, if necessary, remove impurities with higher boiling points than: methanol.
    FIG. 2 shows a distillation column 23 for the preparation of pure dimethyl ether. The feed stream from the reactor enters via line 24. Lime dimethyl ether is withdrawn through line 25, and impurities are removed through line 26. Gas from the head of the column via line 27 enters condenser 28. Reflux into column 23 is fed through line
    29. The waste gases are removed through the line.
    30. The cubed temperature of the column is maintained by means of Shchrkl 1:; ionic reboiler 31, and along the line 32 the bottom residue from the distillation is removed.
    FIG. Figure 3 shows the distillation column 33. Power is supplied via line 34, and distillate containing impurities is fed through line 35 to tank 36, which is equipped with a circulating reboiler 37.
    Limethyl ether from tank 36 through line 38 is returned to column 33. Pure dimethyl ether is taken along
    J lines 39. The impurities freed from dimethyl ether are removed from the system through line 40. Gaseous products from the top of column 33 through line 41 enter condenser 42. The leg is fed to column 33 through line 43. Exhaust gas is removed through line 44.
    Example 1. The synthesis was carried out at 270-290 s and a pressure of 10 kg / cm using J 5 catalyst, which contains 0.018 May L SiO. From the product leaving the reactor, pure, odorless dimethyl ether is obtained almost quantitatively.
    The product, coming from the reactor in the amount of 3000 kg / h and containing 65% by weight of dimetide ether, is distilled in two serially connected continuously operating distillation columns, from which the first is equipped with 50 valve trays.
    0
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     one
    plates. Pure dimethyl ether in the first column is obtained at 7 atm from the 12th plate of the head of the columns with a reflux ratio of 1: 2. In the second clone, filled with Raschig rings, unreacted methanol is regenerated. The methanol conversion in the synthesis reactor is 92%. The yield of pure dimethyl ether, calculated on the methanol reacted, was 99.7%.
    Odor determination is carried out mainly by the sensory method with the help of an experimental commission.
    In cases where the odor threshold lies in the area recorded with instruments, the odor threshold or load threshold can also be determined by measuring methods such as chromatography J electrical conductivity, photometry or fluorescence measurement (Rrdol und Kohle - Erdgas Petrochemip, 1972 , 32, No. 2, s. 86J.
    L p and M e p 2. The process is carried out under the conditions of example 1 with a dietary content of 80 wt.% Dimethyl ether using a catalyst - Alj O which contains 0.005 wt.% SiO, but with an Allegm number of 1: 0.4. As in example 1, receive the odorless dimethyl ether. Conversion of methanol 92%, the yield of the ester 99.7%.
    PRI me R 3. According to example 1, however, use the catalyst J-,
    which contains 0.4 wt.% SiO. As in Examples 1 and 2, odorless dimethyl ether is obtained quantitatively, yield 99.7%.
    PRI me R 4. In the conditions:; of Example 1, a V-catalyst is used, which has a content-iT of 0.025 mass% Si. 0.02 wt.% Fe20. At the indicated conditions, distillates r1; and odorless dimethyl ether are obtained practically quantitatively. Conversion of methanol 92%, the yield of the ester 99.7%.
    Example 5. The process is carried out under the conditions of Example 4, however, the dimethyl ether column is filled with wire cloth. The starting material is introduced into the clones for the calculated in accordance with the invention, and the dimethyl ether and impurities are taken from the calculated tray. Pure, odorless pure dimethyl ether is obtained. The content of the main vegetation 99.7 wt.%
    PRI me R 6 (comparative). Under the conditions of Prira 1, 1 gtroness is carried out with a catalyst.) - 0.020 wt.%
    2392
    SiOg, Impurities are selected at the head of the second column. Almost odorless dimethyl ether is obtained. The output of the ether 97,0%.
    PRI me R 7 (comparative). The process is conducted according to example 6, however, with a catalyst that contains 6 wt.% SiOj. Dimethyl d ester is almost odorless, yield 97%.
    Froze Under the conditions of Example 1, U-, Koczyc contains 6 wt.% Si02 as a catalyst. The product from the reactor is fed to j 30th (gaseous) and 36th (liquid) plates from the head of the column. In the first column at 7 kg / cm from the 3rd plate (from the head of the column) at a reflux ratio of 1: 3, 20 chistL dimethyl ether is obtained.
    Impurities are taken from the 18th plate from the head of the column. Conversion of methanol in the synthesis reactor 91%. The output of dimethyl ether 99,2%. 25 get odorless dimethyl ether.
    EXAMPLE 9 The process is carried out under the conditions of Example B, but with a reflux ratio of 1: 4. The alumino-silicate rtf OQ catalyst is used as the catalyst. Methanol conversion 83%.
    Pure, odorless pure dimethyl ether is obtained, yield 99.3% based on the converted methanol.
    Example 10. R column for distilling off dimethyl ether with 65 valve 35 plates to the 49th plate from the head of the column serves 4000 kg / h of a mixture consisting of | 2400 kg of dimethyl ether, 580 kg of methanol, 910 kg
    water and 110 kg of impurities. 40
    The column operates at a pressure of about kg / cm and a reflux ratio of 1: 1.9.
    From the head of the column, 30 off-gases are taken, consisting mainly of CO, N. hydrocarbons and a small amount of dimethyl ether.
    From the 6th plate of the column (from the head), 2385 kg / h of pure di- 0 methyl ether with methanol content are taken.
    From the 33rd plate (from the head section) 90 kg / h of impurities are taken. 10 kg / h more high boiling point; their, than methanol, components, 580 kg / h of methanol and
    910 kg / h of water are taken from a cube and fed to a column in which methanol is distilled off. An odorless dimethyl ester is obtained.
    P p and m ep 11. The process is carried out as in Example 10, however, a frakidyu is taken out through a lateral discharge, which is between the boiling point of diethyl and methanol. 2395 kg / h of pure dimethyl ether 80 kg / h of fractions containing impurities were obtained. in the form of a side stream, which is stripped in a side tank equipped with a reboiler (FIG. 3).
    Highly pure, odorless dimethyl ether is obtained.
    Example 12. In the first distillation column with 100 valve trays, 61,000 kg / h of mixture, which contains 55000 kg of methanol, 2000 kg of dimethyl ether, 3500 kg of water and 500 kg of impurities are fed, the reflux ratio is 1: 7.
    The feed is carried out on the 35th plate from the head of the column. From the 9th plate, 5 counting from the top of the column, 1996 kg / h of dimethyl ether are removed. From the 30th plate, from the head portion, the olonnas take 302 kg / h of impurities through a side outlet. 55000 kg / h of methanol, 3500 kg / h of water and 190 kg / h of impurities, which consist mainly of higher alcohols, are taken from the bottom of the column.
    Pressure in the column kg / cm. The flue gas (12 kg) that is withdrawn through the head is washed with methiol counterflow. An odorless, high-purity dimethyl ether is obtained.
    Example 13, In the first distillation column with 70 cap plates and a plate (o: t head portion), 4000 kg / h of a mixture consisting of 800 kg of dimethyl ether, 2825 kg of methanol, 300 kg of water and 75 kg of boiling water are served. between methanol and dimethyl ether of impurities. Reflux number 1: 2. With the 4th plate (from the head) taken 796 kg /; h of high-purity odorless dimethyl ether, from the 40th plate (from the head) taken 77 kg / h of impurities,
    2825 kg / h of methano: la and 300 kg / h of water are taken from the cube.
    An odorless, high-purity dimethyl ether is obtained.
    Example 14 A first distillation column with 45 cap trays is fed to the 34th plate (from a g of tin) 2000 kg / h of a mixture consisting of 1750 kg of dimethyl ether, 100 kg of methanol and 100 kg of water, and
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    (also 50 kg of impurities. The column operates at reflux ratio 1: 0-, 5.
    From the 3rd plate (from the head section) 1745 kg / h of dimethyl ether are taken from the 29th plate (from the head section) 48 kg / h of impurities are removed. 100 kg / h of water, 100 kg / h of methanol and 5 kg / h of high-boiling impurities are taken from the cube.
    An odorless, high-purity dimethyl ether is obtained.
    PRI me R 15 (comparative). Example 13 is repeated, but dimethyl ether is taken from the 18th plate (from the head). Impurities are taken from the 45th plate.
    Receive dimethyl ether with a smell,. .
    Example 16 Dehydration of methanol is carried out at a contact load on the feed of 0.2 l / ldh over catalyst g - containing 0.02 wt.% SiO, at and at a pressure of 3 kg / cm. The methanol conversion is 35%. - The yield of dimethyl ether, based on the converted methanol, is 99.7%.
    Etc. and measure 17; Dehydration is cast in methanol with a contact load on the raw material of 16 L / L1CH at and at a pressure of 50 kg / cm over the catalyst Y, containing 0.1 wt.% SiOj., The regeneration of methanol is 98%. The yield of dimethyl ether, calculated on converted methanol, is 99.5%.
    Example 18. In the first distillation column with 26 cap trays, one plate was transferred to the lowest plate of the 4000 kg / h mixture, which consists of 2400 kg of dimethyl ether, 580 kg of methanol, 910 kg of water and 110 kg of impurities.
    The pressure in the column 10 kg / cm. The reflux ratio is 1:20. From the top of the column, 30 exhaust gas is withdrawn, mainly consisting of CO2, Hg, hydrocarbons and a small fraction of dimethyl ether.
    From the third plate of the column (from the head of the column), 2374 kg / h of pure dimethyl ether with a methanol content of 3 ppm are taken, C 18-71 plates (from the head of the column) are taken 101 kg / h of impurities, and 10 kg / h more than HIGHSCAPE components than methanol. At the same time, .580 kg / h of methanol and 910 kg / h of water are sent to a column in which methanol is distilled off.
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    91602392
    Example 19. In the reactor, which srder sieve as a catalyst Y-AljO with 0.018 mass% SiOg, is fed 6261 kg / h of pure methanol. Of these, 1046 kg / h of recirculated methanol from a distillation methanol column.
    The reactor operates under a pressure of 11 kg / cm and a temperature in the catalyst bed of 260–300 ° C with a contact load on the catalyst of 2.4 l / l; h.
    The reaction product exiting the reactor consists of 1046 kg / h of unreacted methanol, 1442 kg / h of reactant water and 3773 kg / h of dimethyl ether.
    This mixture is fed at the first istil, for example, to the paddle column on the 53rd plate.
    In the column, the total number of valve plates is 61. The reflux ratio is 1: 3.
    From the 40th plate, 64 kg / h of impurities are taken. It should be noted that about 56 kg of this stream is dimethyl ether.
    From the 7th plate, 3709 kg / h of raw dimethyl eLire without stock are taken.
    A small amount of inert ga15
    20
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    p and
    in si
    d gr
    di
    in ra
    with
    chi ku no me
    pr. relo 99 Di de si Co 99 with go not from but to your co
    A call (H, COg 5 light hydrocarbons) is retracted through the head of the column. The bottom product 2488 kg / h is sent for separation into a methanol column equipped with 40 valve plates. As a result of separation, 1046 kg / h of methanol from the head of the column and 1442 kg / h of water, which is taken from the cube, are obtained.
    The head product from the methanol column is returned to the synthesis reactor.
    Example 20. The process is carried out as in Example 19, however, the synthesis is carried out at a pressure of 3 kg / cm, a temperature of 160-200 ° C and a catalyst contact load of 0.3 l / l h of raw materials.
    The resulting reaction product consists of 5879 kg / h of unreacted methanol, 79 kg / h of reaction water and 203 kg / h of dimethyl ether.
    The mixture is fed to the 45th plate in a bowl for distilling the dimethylbpgo ether. The reflux number is 1:15.
    From the 8th plate, 11 kg / h of impurities are taken, and they contain 10–10 dimethyl ether.
    From the 2nd plate from ro ioBHoii, parts of the column take 193 kg / h of pure
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    dimethyl ether. The distillation of the bottom product in the cattle condition of 6057 kg / h is carried out in a methanol column, and thus 5978 kg / h of methanol and 79 kg / h of water are obtained.
    Example 21 The process is carried out in accordance with Example 19, however, the synthesis is carried out at 430-450 ° C.
    the pressure of 48 kg / cm and the contact load on the catalyst 15,
    The reaction products consist of 188 kg / h of unreacted methanol, 1708 kg / h of reaction water, and 4365 kg / h of dimethyl ether.
    The mixture is directed to the 26th burner to the dimethyl ether recovery columns. Reflux 1: 0.4.
    From the 20th plate the columns take 91 kg / h of impurities. Of these, 79 kg / h is dimethyl ether.
    From the 14th plate 4286 kg / h of pure dimethyl ether are taken. 1884 kg of bottom product is distilled in a methanol column and 176 kg / h of methanol and 1708 kg / h of reaction water are recovered.
    Thus, from the presented examples, it follows that according to the invention, dimethyl ether is quantitatively isolated in a first distillation column with a yield of 99.5- 99.7%. Dimethyl ether is odorless, contains less than 10 ppm of methanol and a maximum of 0.1 May. hydrocarbons. The content of the main component of 99.9 wt.%. Crawling The dimethyl ether according to the invention is suitable for any AZ application. When carrying out the process according to the invention, the methanol conversion increases by one stage dehydration to 92%. compared with 83% by a known method. In this case, compared with the known method, only one column with a high separation capacity is needed, while the second column for separating methanol from water can be less than the separation capacity compared to the first
    COLONNOSIS.
    The proposed method allows in the second column to additionally also separate impurities, respectively, between the temperature of boiling and methanol and dimethyl ether, as a result, the wastewater depleted of impurities can be further easily processed. Operation and additional columns is possible, but this reduces the efficiency of the process.
    权利要求:
    Claims (3)
    [1]
    1. Method for the continuous preparation of dimethyl ether by catalytic dehydration of methanol over a catalyst, U-alumina, which contains silica, at a temperature of 200-450 s and a pressure of 3 GP, kg / cm, to obtain the product of dehydration and its separation into two rectification columns with the selection in the first column on top of the gaseous products, which contain COj, H,
    and light hydrocarbons mixed with dimethyl ether, as a side fraction from the intermediate section of the dimethyl ether column and from the bottom of the bottom product column, sent to the second column, in which
    the methanol not entering the reaction is distilled off and then it is returned to the dehydration stage, and the reaction water is obtained as the bottom product of the second column, while
    in the first column, the fraction of dithyl is separated, which contains impurities boiling away at the boiling point temperature of dimethyl eLir, but lower than methanol, which, in order to improve the quality of dimethyl ether,
    methanol hydration is carried out over a catalyst - containing 0.005-0.5 wt.% SiOj, at a flow rate of methanol of 0.2-16 l / l.
    about
    five
    catalyst per hour and the dehydration product is fed to the plate of the first pL of the recirculation column below the 25th plate from the head of the column and the dimethyl ether is taken from the plate above the 15th plate from the head of the column and at least 5 plates higher from the feed plate, and the fraction containing impurities is removed from the plate, which is 5-37 plates higher than the feed to the column, but below the 15th plate from the head of the column, while the reflux number is maintained in the range 1: 1 - 1:15 when the content of dimethyl ether in Recreatives Products dehydration 1-5 wt%, or equal to 1: 0.4 - 1: 5. dimethylether at a concentration of 20-80 wt.%.
    [2]
    2. The method according to claim 1, wherein the gaseous products1 1 from the top of the first column are washed with methanol in countercurrent mode.
    [3]
    3. Method according to paragraphs. 1 and 2, that is, the flow rate of HZ and that the fraction containing the impurities and taken from the first column is stripped to the side stripping section 11 1I and the separated dimethyl ether is returned to the same one. Col- Uprioritet on items and signs: 11/18/86 on PP. 2 and 3 - distillate purification of dimethyl ether. 12/16/86 per liter 1 - methanol dehydration catalyst.
    (Pu2.f
    Figg
    Compiled by G.Stepanov Editor S.Pekar Tehred L.Serdyukova Proofreader O. Tsiple
    Order 3280
    Circulation
    VNIIPI State Committee for Inventions and Discoveries at the State Committee on Science and Technology of the USSR 113035, Moscow, Zh-35, Raushsk nab. D. 4/5
    Production and Publishing Combine Patent, Uzhgorod, st. Gagarin, 101
    Fig.d
    Subscription
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    同族专利:
    公开号 | 公开日
    ES2003076A4|1988-10-16|
    AT71354T|1992-01-15|
    IN168048B|1991-01-26|
    DD270901A1|1989-08-16|
    NO874787D0|1987-11-17|
    CN1036199A|1989-10-11|
    YU208087A|1988-10-31|
    DK603187A|1988-05-19|
    DK603187D0|1987-11-17|
    AU6550686A|1988-05-19|
    BR8606293A|1988-07-05|
    CA1322767C|1993-10-05|
    NO874787L|1988-05-19|
    HUT45956A|1988-09-28|
    NZ222597A|1990-09-26|
    FI875046A0|1987-11-16|
    AU603070B2|1990-11-08|
    EP0455004A1|1991-11-06|
    ES2003076T3|1992-07-01|
    DE3775902D1|1992-02-20|
    GR880300102T1|1989-06-22|
    JPS63208546A|1988-08-30|
    PL268856A1|1988-10-13|
    EP0270852A2|1988-06-15|
    EP0270852B1|1992-01-08|
    FI875046A|1988-05-19|
    NO165914B|1991-01-21|
    NO165914C|1991-05-02|
    EP0270852A3|1988-12-28|
    引用文献:
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    法律状态:
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    申请号 | 申请日 | 专利标题
    AU65506/86A|AU603070B2|1986-11-18|1986-11-18|Process for the purification of dimethylether|
    DE19863642845|DE3642845C2|1986-12-16|1986-12-16|
    BR8606293A|BR8606293A|1986-11-18|1986-12-19|PROCESS FOR PURIFICATION OF DIMETHYL ETER|
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