• 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:
    A process for recovering propene and propene/propane mixtures from the off-gases obtained from the hydroformylation of propene involves contacting the off-gases with a liquid absorbent comprising at least one of the liquid substances formed during the hydroformylation of propene to absorb the propene and propane and thereafter desorbing these gases from said liquid substances.
    公开号:SU810076A3
    申请号:SU782680097
    申请日:1978-10-31
    公开日:1981-02-28
    发明作者:Сридхар Сринивазан
    申请人:Хемише Верке Хюльс Аг (Фирма)；
    IPC主号:
    专利说明:

    The invention relates to the processing of waste gases, in particular, to a method of processing waste gases from hydroformylation of propene, which mainly contain propene propane, carbon monoxide, methane, azo. argon and hydrogen. A known method for the processing of propene hydroformylation flue gases is that these flue gases burn fl. The purpose of the invention is to isolate unreacted components. The goal is achieved by the absorption of propene hydroforming exhaust gases by hydroformylation substances in the amount of 1-22 kg / nm of gases at a pressure of 10-60 atm and 0-50 ° C. N-butyric aldehyde, isobutyraldehyde, n-butanol or their mixtures are used as absorbent. After absorption, absorbable α-gases are separated (propene and propane by lowering the pressure and / or increasing the temperature of the absorbent. By combining desorption with fractional distillation, only propane can be separated. Propene obtained after desorption is preferably returned to hydroformylation. Then propane is then distilled by distillation from the absorbent; the free absorbent is returned to the absorption stage. The complete separation of the absorbent from the absorbable recycled material; propene is optional, as it is a product hydroformylation and therefore does not adversely affect the process of formatization. The propene hydroformylation off-gases have the following composition,% by volume: 5-40 carbon monoxide; 20-50 hydrogen; 2-20 propene; 2-20 propane; 0.5-2 C - hydrocarbons; 0.5-15 nitrogen; 0.1-0.5 carbon dioxide; 0.10, 5 argon. The exhaust gases used in examples 1-4 have the following composition, vol.%: 6 propene; 12 propane; 32 carbon monoxide; 46 hydrogen; 0.3 C4 - hydrocarbons; 2.7 nitrogen; 0.5 carbon dioxide and 0.5 argon. Exhaust gases used in Example 5, of the following composition,% by volume: 15 propene; 15 propane; 16 carbon monoxide; 43.3 hydrogen; 0.5 C hydrocarbons; 10 nitrogen; 0.1 carbon dioxide and 0.1 argon. Example 1. The hydroformylation off-gases, which are formed at two different stages of reducing the pressure from 20 to 3 atm, respectively, are combined and compressed in compressor 1 (Fig. 1) to 3.5 atm. Subsequent absorption of C - gases occurs in the absorption column 2 at elevated pressure. The incoming gas in the countercurrent is irrigated isomally with aldehyde, and for 1 it lacks Roman gas, 3.64 kg of isobutyraldehyde is used. After the final-: separation of the C-gases in the absorption column 2, the synthesis gas is returned via pipe 3 directly to the hydroformylation reactor. The absorption is carried out in co-long 2 at 35 ° C and a pressure of 35 atm. Isoaldehyde aldehyde is fed to the upper part of the column through conduit 4. A mixture of gas through conduit 5 is introduced into the middle of column 2. The reinforcing part of column 2 is used for absorption. The isobutyraldehyde used is free from C. After absorption, together with synthesis gas, only 1% of the injected propene escapes through the pipeline. When absorbed into stream 6 of isobutyraldehyde, not only drink, but also propane. C-free synthesis gas is returned to hydroformylation. About 2% of the propane remains in stream 3. Frequently, stream 3 is removed from the system to remove inert gases (.Ar). The lower part of the absorption column 2 functions as a distillation column; Here, Ci and volatile components are separated from the stream Cj / C. In the distillation part, the same pressure (35 atm) acts as in the absorption part. However, since there are almost no volatile components, only the Cj and C components are kept under pressure. The separation of propene and propane from isobutyraldehyde is carried out in the sorption column 7 by distillation at 20 atm and a top temperature of 55 ° C. The aldehyde isomalous content of the legs (C content) in the head of the product should be as low as possible to prevent undesirable loss of C. If the aldehyde enters the head product, then subsequent separation of propene and propane (column 8) in a cube will be removed in combination with propane stream (stream 9). The bottom product of column 7, in contrast, must be completely free of Cj. Only then can the aldehyde be returned to column 2 (stream 4) as an effective absorbent. In column 8, propane and propane are separated from each other by distillation. Propane leaves the system as stream 9 and can be evaporated, discharged, burned when energy is received. Propene with a purity higher than 96% (the rest is propane) is returned through conduit 10 in hydroformed oil. 99% of propene contained in the waste gas is recovered. Example 2 The crude product has the following composition, wt.%: 19., O isobutyraldehyde; 60.1 n-butyraldehyde; 4.2 Isobutanol; 7.9 n-butanol; 4.6 high boiling components and 4.2 water. The absorption is carried out at 35 atm and from 11 kg of the indicated crude product per 1 it is insoluble. gas 99% of propene is recovered. Example 3. The incoming gas contains 12% by volume of propane and 6 o6v% of propene. As the absorbent used is specified in example 1, n-butyric aldehyde. Absorption is carried out at 35 ° C, 20 atm and ratio. 7.4 kg n-butyric aldehyde to 1 nm insoluble gas. Reach prakg; tically complete absorption. 99% of propene is recovered. Example 4. The incoming gas contains 12% by volume of propane and 6% by volume of propene. Raw butanol is used as an absorbent. Absorption is carried out at 60 atm. 10 ° C and the ratio of 3.5 kg of raw butanol to 1 nm of insoluble gas. The remaining conditions are similar to Example 1. 99% of propene is recovered. Example 5. The incoming gas contains 15% by volume of propane and 15% by volume of propene. Analogously to example 1, it is washed in column 2 (Fig. 2) containing 5 -stradium units. The absorption of the CJ gas is carried out in the amplifying part at a ratio of 8.35 isobutyraldehyde to 1 nm insoluble gas, 2D atm and 35 ° C. The Cj-free gas stream 3 enters the combustion stage. The Cj-gas-loaded stream 6 of isobutyraldehyde is fed to the desorption column 7, where, at a top temperature of 50 ° C and a pressure of 20 atm, propene and propane are separated. Distillate propene in a liquid state is returned to the hydroformylation reactor. Then in column 1, propane is separated from isobutyraldehyde at a pressure of 6 atm and a top temperature of 5 ° C. In this case, propane serves as a coolant for the condensation of the head product. The C-j-free current of isobutyraldehyde (stream 4) returns. for absorption into column 2. 99% of propene is recovered. Example 6. Analogously to Example 1 with the difference that the exhaust gases of the composition are used, bb%: 5 mon carbon monoxide; 36.4 hydrogen; 20 propene; 20 propane; 2 С hydrocarbons; 15 nitrogen; 0.4 carbon dioxide and O, 2 argon. The absorption process is carried out at a pressure of 10 atm, and the absorbent is taken in an amount of 1 kg per 0.5 of the waste gases. 99.1% of propene is recovered. Example 7. Similarly to Example 1 with the difference that exhaust gases of the composition are used, vol.%: 40 carbon monoxide; 35 hydrogen; 15 propene; 8.5 propane; 0.5 C t - hydrocarbons; 0.5 nitrogen; 0.3 carbon dioxide and 0.2 argon. The absorption process is carried out at a pressure of 60 atm, and the absorbent is taken in the amount of 11 kg per 0.5 nm of flue gases. Recovery from 99.4% propene. Example Analogously to Example 1, with the difference that the exhaust gases of the composition are used, vol.%: 35 carbon monoxide; 20 hydrogen; 16 propene; 18 propane; 1.5 Sd - carbohydrate supply; 9 nitrogen; 0.2 carbon dioxide and 0.3 argon. The process is carried out at 35 ° C and a pressure of 50 atm, and the absorbent is taken in an amount of 1 kg per 1 running gas. 99% of propene is recovered. Example 9. Analogously to example 1, since that time, that I use Pei4Uflf (y t / flyefft / J npgneff
    Recycled / sontez gas
    Conclusion
    权利要求:
    Claims (2)
    [1]
    During the process, the exhaust gases of the composition,% by volume: 32.5 carbon monoxide; 50 hydrogen; 2 propene; 2 propane; 2 С hydrocarbons; 11 nitrogen; 0.4 carbon dioxide and 0.1 argon. Recover 100% propene. Claim 1. Method for treating hydroformylation flue gases of propene, characterized in that, in order to release unreacted components, flue gases are subjected to absorption of 1-22 kg / nm of gases formed during hydroformylation at a pressure of 10-60 atm at 0 -50 ° C. .
    [2]
    2. The method according to p. 1, about tl and. This is due to the fact that n-butyric, isobutyraldehydes, n-butanol, or mixtures thereof are used as the absorbent. Sources of information, rindu to take into account when SKcjnepTHSe 1. DOmbgen G., Neubaner D. Gro echnische Herstellung von Oxolkoholen aus Propylen In der BASF. hew .Ing.Technik, 1969, 41, No. 7, 976 prototype).
    Qmxodautvu
    Propane
    Phi.1
    Recyclable
    Process
    propene
    Leave gas
    Propane
    NHN
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    同族专利:
    公开号 | 公开日
    JPS5479204A|1979-06-25|
    ES474893A1|1979-03-16|
    US4210426A|1980-07-01|
    FR2407904B1|1983-08-19|
    DE2749890B2|1980-05-08|
    IT7851781D0|1978-11-06|
    AT371370B|1983-06-27|
    FR2407904A1|1979-06-01|
    DE2749890A1|1979-05-10|
    ATA795678A|1982-11-15|
    GB2009227B|1982-05-26|
    GB2009227A|1979-06-13|
    引用文献:
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    NL263403A|1961-02-08|
    US3369050A|1961-10-06|1968-02-13|Shell Oil Co|Separation, recovery and recycle of the catalyst complex in the oxo process|
    US3520937A|1966-04-05|1970-07-21|Basf Ag|Processing oxo reaction mixtures|
    US3658904A|1966-12-12|1972-04-25|Phillips Petroleum Co|Extraction process using cyano acetal solvents|DE3114147A1|1981-04-08|1982-10-28|Basf Ag, 6700 Ludwigshafen|METHOD FOR OBTAINING ALDEHYDES|
    US5001274A|1989-06-23|1991-03-19|Union Carbide Chemicals And Plastics Company Inc.|Hydroformylation process|
    US5087763A|1990-11-09|1992-02-11|Union Carbide Chemicals & Plastics Technology Corporation|Hydroformylation process|
    US5367106A|1993-09-20|1994-11-22|Hoechst Celanese Corporation|Coupled secondary oxo reaction system|
    CA2130387A1|1993-09-30|1995-03-31|Ramakrishnan Ramachandran|Process for the production of oxo products|
    US5410091A|1994-06-02|1995-04-25|Quimica Oxal C.A.|Rhodium catalyzed oxo process in tubular reactor|
    US5600017A|1995-01-18|1997-02-04|Exxon Research And Engineering Company|Direct hydroformylation of a multi-component synthesis gas containing carbon monoxide hydrogen ethylene and acetylene-|
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    GB201604608D0|2016-03-18|2016-05-04|Johnson Matthey Davy Technologies Ltd|Process|
    WO2017160956A1|2016-03-18|2017-09-21|Dow Technology Investments Llc|Hydroformylation process|
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    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    DE2749890A|DE2749890B2|1977-11-08|1977-11-08|Process for the recovery of propene or propene-propane mixtures from the exhaust gases of the hydroformylation of propene|
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