• 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 separating carbon dioxide from a gaseous recycle system containing ethylene unconverted in the catalytic oxidation of ethylene to ethylene oxide comprises (a) contacting at least a portion of the total recycle stream with an aqueous absorbant for carbon dioxide thereby producing a hydrocarbon rich overhead and a carbon dioxide-fat absorbate, (b) flashing the fat absorbate to produce a hydrocarbon-rich inert vapor stream and a hydrocarbon-lean, carbon dioxide-fat absorbate and (c) stripping the hydrocarbon-lean, carbon dioxide-fat absorbate to produce a carbon dioxide overhead substantially free of hydrocarbon.
    公开号:SU845771A3
    申请号:SU742046362
    申请日:1974-07-15
    公开日:1981-07-07
    发明作者:Гордон Фостер Элтон；Феликс Рассел Поль；Джорж Фандерватер Роберт
    申请人:Шелл Интернэшнл Рисерч Маатсхаппийб.B.(Фирма)；
    IPC主号:
    专利说明:

    The cauldron) is connected to the recycle liquid gases passing through conduit 2 and mixed with oxygen-containing (e.g. oxygen, air, or their mixture stream 3 from a source (not shown) and in contact with the oxidation catalyst of the usual structure for example, a silver-containing catalyst. The gaseous hydrocarbon stream 1 should not contain acetylene even as traces (acetylene is harmful and dangerous during the oxidation process), the reaction zone can consist of many reactors arranged in series or parallel. In zone 4, part of ethylene is partially oxidized to ethylene oxide. The effluent from zone 4 usually has the composition, mol.%: 0.5-3 ethylene oxide, up to 35 ethylene, up to 8 oxygen, 0.5-20 carbon dioxide gas and hydrocarbons C | -C ,, as well as inert gases such as nitrogen and argon. The stream leaving zone 4 passes through pipe 5 at a temperature of 200-300 ° C, mainly at a pressure of 10-25 atm and is cooled to 35-100 ° C using heat exchangers 6 The cooled reaction product passes through line 7 to the primary absorption zone 8, where it is in contact with This stream 9 at 15-50 ° C and atm pressure for absorbing and separating ethylene oxide from unreacted ethylene and other hydrocarbons, carbon dioxide and oxygen, as well as most other gaseous components. The water absorber containing diluted ethylene oxide is passed through conduit 10 for further processing. Unreacted gaseous materials are passed through Pipeline 11 to the compressor 12 and through line 13 for further processing and ultimately to return to the reaction zone 4. The compressor 12 can be placed in the recycle of the recycler, for example, line 7 or 2. At least part of the unabsorbed gaseous materials from pipeline 13, they are passed through pipelines 4 and 15 to washing zone 16, where they come into contact with the regenerated carbon dioxide absorbent introduced through pipe 17. The number of returned gas different materials held in the washing zone 16 can be controlled by any conventional valve means 18, the amount is usually 10-50 wt.% of gaseous materials Recycle. Typical absorbents for carbon dioxide are aqueous solutions of alkali metal carbonates, such as potassium carbonate, conditions of absorption in the washing zone 16 vary depending on the absorbent used; however, absorption is usually carried out at 35-f25 C and a pressure of 10-25 atm. After the washing zone (carbon dioxide absorption) 16, the gaseous stream is fed as overhead through conduits 19 and 2 to reaction zone 4. The carbon dioxide enriched sorbet containing small amounts of entrained and / or dissolved hydrocarbons is transferred from the wash zone 16 through a pipeline 20 to the distillation zone 21. Hydrocarbons contained in the absorber, obo-. carbonated gas is distilled off at COI 21 at 95-120 ° C and a pressure of 2-8 atm. The gaseous overhead stream is directed through conduit 22. I The drawing shows a preferred scheme in which the head fraction of the distant zone is returned to the gaseous raw material of the recycle pipe running in conduit 2 through conduit 22, compressor 23, conduits 24 and 15, washing zone 16 and conduit 19 However, the amount of overhead of the distant zone is usually very small and can be returned to the gaseous raw material of the recycler at any desired location, for example, in the primary absorption zone 8 through a pipeline (not shown); or through a pipeline (not locally) directly into pipeline 2, through which the main gaseous raw material of the recycler is returned to reaction zone 4. The head fraction of the distant zone can also be used as fuel gas, the remaining carbon absorbed liquid absorber enriched from the distant zone 21 through conduit 25 to the main stripping zone 26. In addition, the drawing also shows a variant of the scheme in which the enriched absorber leaving the distant zone 21 through conduit 25 is brought into contact with stripping gas into the zones intermediate distillate 27 in order to separate virtually all carbonaceous substances that may remain in the absorber. According to this scheme, valves 28, located on line 29, and valves 30, located on line 25, are installed with the aim of directing at least a part, and preferably of total fatty absorbate enriched with carbon dioxide, through line 31 to the intermediate distillate 27 where it is brought into contact with an inert distant gas, such as nitrogen, carbon dioxide or water vapor, is introduced through conduit 32. Air can also be used as the distant gas, since it is usually necessary to use only very low temperatures. small amounts of stripping gas. The pressure in the intermediate distillate zone 27- can vary from 2 to 5.5 atm, however, it is usually maintained at a pressure slightly lower than the pressure in the distant zone 21. In the extracted head fraction of the intermediate distillate there are essentially all yrn hydrogens that can remain in the fat absorber enriched with carbon dioxide introduced into the specified zone 27. The head - the fraction of the intermediate distillate zone 27 removed through the pipeline can be combined with the gaseous raw material of the recycler by means not shown in the drawing, however leash and generally contains a minor amount hydrocarbons. Absorbate enriched with carbon dioxide from zone 27 is directed through pipelines 34 and 29 to zone 26, where carbon dioxide is stripped from water absorbate at pressures up to 2 atm. Steam can be introduced into zone 26 through pipeline 35 to facilitate distillation. When using stripping steam, the overhead stream passing from zone 26 through conduit 36 is cooled using heat exchangers to condense at least part of the vapors contained in it to recover and possibly reuse the condensate. Carbon dioxide, which is evaporated from the water sorbent, is essentially free of hydrocarbons and can be used as a scavenger and used by itself or removed through conduit 36 without adversely affecting the surrounding river. gas, is sent to pipeline 17 to the secondary sorption zone (carbon dioxide gas flushing zone) 16 for contact with gaseous gas from the raw material of the recycler entering the pipeline wire 15. Using a carbon fiber for stripping carbon dioxide from adsorbate gas reduces the content of hydrocarbons in carbon dioxide to 0.005%. Example 2. A gaseous stream of oxide and ethylene of a normal concentration and amount, as described in the previous section, containing (wt.%) 5-15 carbon dioxide, 653-8 oxygen, j, the rest of the hydrocarbons are inert gases, such as nitrogen and argon, as well as water vapor. About 25 vol.% Of the outgoing gaseous stream is subjected to a contacting aqueous solution of calcium carbonate taken as an absorbent for carbon dioxide. Approximate pressure and temperature maintained in the indicated. zones, you will bring to tab. 1. Table 1 Rinsing 16 11 o of the distillate 21 107.2 Main Stripping 26110 Composition of various streams of lead; us in the table. 2
    Flow, per unit of time in terms of 100 g. Mol of recycled stream 13
    Composition, wt.%: Hydrocarbons
    Oh .05 35 C -Cj.
    COM 40
    98.5 20 98.5 98.5 T l
    权利要求:
    Claims (1)
    [1]
    The composition will differ depending on the degree of condensation created to recover the distant vapor. Claims The method of hydrocarbon separation from the products of ethylene oxidation to ethylene oxide by successive absorption of ethylene oxide with water, and then with an aqueous alkaline solution of carbon dioxide and recycling of unabsorbed hydrocarbons, is characterized in that, in order to increase the degree of hydrocarbon emission.
    0.07 140 145 1.7
    Contains less than 10% of total flow 20
    92
    one
    1.5 Traces of alkaline absorber are heated at 95-120s and a pressure of 2-8 atm. The hydrocarbons lost in this process are recycled, followed by release of carbon dioxide by treating the residue with steam. Sources of information taken into account during the examination 1. USSR Author's Certificate No. 436491, cl. C 07 D 1/14,) publ. 1974 (prototype).
    类似技术:
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    US1936570A|1933-11-28|Gas purification
    US2134507A|1938-10-25|Purifying gases
    同族专利:
    公开号 | 公开日
    BE817532A|1975-01-13|
    US3867113A|1975-02-18|
    FR2237896A1|1975-02-14|
    CA1035780A|1978-08-01|
    DE2433423A1|1975-02-06|
    GB1476201A|1977-06-10|
    FR2237896B1|1978-11-10|
    JPS5040508A|1975-04-14|
    PL100734B1|1978-11-30|
    DD113219A5|1975-05-20|
    RO69201A2|1981-08-30|
    NL7409244A|1975-01-20|
    ES428262A1|1976-07-16|
    CS183745B2|1978-07-31|
    NL189259C|1993-02-16|
    DE2433423C2|1987-05-27|
    IT1017162B|1977-07-20|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    US3375639A|1962-12-27|1968-04-02|Union Oil Co|Extraction of acidic constituents from gas mixtures with gammabutyrolactone|
    US3362133A|1965-10-25|1968-01-09|Allied Chem|Process for hydrogen sulfide removal from gas mixtures containing h2s and co2|
    US3463603A|1967-03-17|1969-08-26|Shell Oil Co|Method of separating acidic gases from gaseous mixture|
    US3770622A|1970-12-28|1973-11-06|Fluor Corp|Treatment of wet natural gas mixtures to recover liquid hydrocarbons|
    US3710546A|1971-09-16|1973-01-16|Metallgesellschaft Ag|Process for the removal of hydrogen sulfide and carbon dioxide from fuel gases and synthesis gases|
    BE789308A|1971-10-04|1973-03-27|Shell Int Research|TERIGE OPLOSSINGEN VAN ETHEENOXYDE WERKWIJZE VOOR HET CONCENTREREN IN ZUIVEREN VAN WA|US4493715A|1982-12-20|1985-01-15|Phillips Petroleum Company|Removal of carbon dioxide from olefin containing streams|
    GB8431597D0|1984-12-14|1985-01-30|Ici Plc|Treatment of gas mixtures|
    GB8432657D0|1984-12-27|1985-02-06|Ici Plc|Separation process|
    US4769047A|1987-06-29|1988-09-06|Shell Oil Company|Process for the production of ethylene oxide|
    US5177225A|1990-07-09|1993-01-05|The Boc Group, Inc.|Process for the production of alkylene oxide|
    US5233060A|1992-08-13|1993-08-03|The Dow Chemical Company|Ethylene recovery in direct-oxidation ethylene oxide processes|
    US6168769B1|1993-12-06|2001-01-02|Phillips Petroleum Company|Olefin purification|
    US5972303A|1994-01-18|1999-10-26|Phillips Petroleum Company|Olefin purification|
    US6495609B1|2000-11-03|2002-12-17|Exxonmobil Chemical Patents Inc.|Carbon dioxide recovery in an ethylene to ethylene oxide production process|
    US6533843B2|2001-06-05|2003-03-18|Scientific Design Company, Inc.|Two stage flash for hydrocarbon removal|
    US8049044B2|2002-12-23|2011-11-01|Shell Oil Company|Remediation process and apparatus|
    US20050277778A1|2004-06-10|2005-12-15|Krishnan Viswanathan|Carbon dioxide production|
    EP2154521B1|2007-04-17|2012-08-22|ARKRAY, Inc.|Method and apparatus for measuring substrate concentration|
    US8183400B2|2008-07-31|2012-05-22|Dow Technology Investments Llc|Alkylene oxide recovery systems|
    ES2458224T3|2010-05-18|2014-04-30|Basf Se|Procedure for the removal of carbon dioxidefrom a circulating gas system|
    US8814989B2|2010-05-18|2014-08-26|Basf Se|Process for removing carbon dioxidefrom a cycle gas system|
    EP3788027A4|2018-04-30|2022-03-09|Scient Design Co|Recirculating process for preparing ethylene glycol|
    TW201945071A|2018-04-30|2019-12-01|美商科學設計有限公司|Epoxidation process with concentrated ethylene oxide solutions|
    TW201945328A|2018-04-30|2019-12-01|美商科學設計有限公司|Method for improving the manufacture of ethylene glycol|
    WO2019213029A1|2018-04-30|2019-11-07|Scientific Design Company, Inc.|Process for preparing ethylene glycol|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    US379276A|US3867113A|1973-07-16|1973-07-16|Ethylene oxide process|
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