WO2000053548A1 - Process for the production of olefins - Google Patents

Process for the production of olefins Download PDF

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Publication number
WO2000053548A1
WO2000053548A1 PCT/GB2000/000637 GB0000637W WO0053548A1 WO 2000053548 A1 WO2000053548 A1 WO 2000053548A1 GB 0000637 W GB0000637 W GB 0000637W WO 0053548 A1 WO0053548 A1 WO 0053548A1
Authority
WO
WIPO (PCT)
Prior art keywords
metallic salt
light olefins
salt
olefins
solution
Prior art date
Application number
PCT/GB2000/000637
Other languages
French (fr)
Inventor
Andrew Lindsay Burns
Barry Martin Maunders
Original Assignee
Bp Chemicals Limited
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Bp Chemicals Limited filed Critical Bp Chemicals Limited
Priority to AU26822/00A priority Critical patent/AU2682200A/en
Publication of WO2000053548A1 publication Critical patent/WO2000053548A1/en

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C11/00—Aliphatic unsaturated hydrocarbons
    • C07C11/02—Alkenes
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2529/00—Catalysts comprising molecular sieves
    • C07C2529/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites, pillared clays

Definitions

  • the present invention relates to a process for the production and isolation of low molecular weight olefins, and in particular to the production and isolation of ethylene and propylene.
  • a well known process is the steam cracking of paraffinic hydrocarbons containing two or more carbon atoms. Such processes, involve the pyrolysis of the hydrocarbon at high temperature. The heat required for the pyrolysis is provided by indirect heat transfer from a radiant furnace.
  • An alternative process is the production of olefins from an oxygenated feed such as methanol.
  • the oxygenate feed is contacted with a suitable catalyst which is typically a molecular sieve.
  • a suitable catalyst typically a molecular sieve.
  • This process is disclosed in US 5744680, US 4912281 and US 5028400. This process has the advantage that the olefin can be obtained from a feed containing one carbon atom, the selectivity to ethylene and propylene is greater than the conventional steam cracking process and the operating temperature is significantly less.
  • cryogenic distillation which is a multi-stage process comprising (1) a first step of separating and removing methane, carbon monoxide, and hydrogen via a demethaniser; (2) a second step of separating C 2 /C 3 hydrocarbons from the heavier hydrocarbons; (3) a third step of hydrogenating the C 2 /C 3 acetylenic compounds to ethylene and propylene; and (4) a fourth step of separating ethylene from ethane and of separating propylene from propane.
  • the present invention provides a process for the production and recovery of light olefins, said process comprising the steps of
  • the present invention provides an effective, efficient and inexpensive means of producing and isolating the highly desirable light olefins.
  • the feedstock of the present process is an oxygenated feedstock.
  • Suitable examples of an oxygenated feedstock include alcohols, ethers, aldehydes, ketones and mixtures thereof.
  • the oxygenate feed may comprise 1 to 10 carbon atoms, preferably 1 to 4 carbon atoms.
  • the preferred oxygenate feed is methanol.
  • the feedstock may be diluted with a diluent such as steam, hydrogen, nitrogen, carbon monoxide, carbon dioxide, methane and other light paraffinic hydrocarbons.
  • a diluent such as steam, hydrogen, nitrogen, carbon monoxide, carbon dioxide, methane and other light paraffinic hydrocarbons.
  • the feedstock and optional diluent is contacted with a catalyst capable of converting the oxygenate feed to olefins.
  • the catalyst is a molecular sieve. Suitable catalysts include silico alumino phosphates, for example SAPO 34 and SAPO 17, zeolites for example ZSM-5 and ZSM-11.
  • the conversion process is carried out under conditions suitable for the production of olefins. Suitably, the process is carried out in the liquid or vapour phase. It is preferred to carry out the process in the vapour phase.
  • the process is carried out at a temperature of from 200 to 700°C, preferably from 300 to 500°C and under a pressure of from 0.001 to 1000 atmospheres, preferably from 0.01 to 100 atmospheres.
  • the conversion process may be carried out in any suitable reactor, for example a fixed bed, fluid bed or spouted bed reactor.
  • the products of the process comprise light olefins, e.g. ethylene and propylene in addition to butyl enes and small amounts of hydrogen, carbon oxides, methane, acetylenes, ethane, propane, butanes and higher hydrocarbons.
  • the products may also comprise water, which should be removed, preferably, prior to the olefin recovery step b).
  • the products of the conversion process are contacted with a solution of a metallic salt.
  • the product stream is pre-treated prior to contact with the metallic salt.
  • the pre-treatment step may comprise one or more of amine scrubbing, catalytic oxidation and/or reduction and other steps, known to those skilled in the art, to remove components such as carbon dioxide, oxygen, hydrogen, oxygenates and the like which may be present in small amounts.
  • C 4 and heavier hydrocarbons may also be removed in a like manner.
  • the product stream is contacted with a solution of a metallic salt which is capable of chemically absorbing the light olefinic products.
  • Suitable metallic salts include salts of chromium, copper (1), manganese, nickel, iron, mercury, silver, gold, palladium, rhodium, ruthenium, osmium, molybdenum, tungsten and rhenium.
  • the preferred metallic salt is a copper (1) salt or a silver salt.
  • the salt may be an acetate, nitrate, sulphate, carboxylate and borates.
  • the preferred salt is a nitrate e.g. copper (1) nitrate, silver nitrate. Equally preferred is silver fluoroborate.
  • the solution of metallic salt is suitably an aqueous solution and may comprise an organic nitrogen-containing compound such as pyridine, piperidene, hydroxy- propionitrile, diethylene triamine, acetonitrile, formamide, acetamide and derivatives thereof.
  • organic nitrogen-containing compound such as pyridine, piperidene, hydroxy- propionitrile, diethylene triamine, acetonitrile, formamide, acetamide and derivatives thereof.
  • the concentration of metal salt to nitrogen-containing compound in the aqueous solution is in the range from 1 : 1 to 1 :6, preferably 1 :2.
  • the concentration of metal salt in the solution is suitably at least 0.5 moles of salt per litre of solvent, preferably at least 2 moles of salt per litre of solvent.
  • the process for isolating the ethylene and propylene comprises contacting the product stream obtained from the oxygenate conversion process with a metal complex which is capable of complexing or absorbing ethylene and/or propylene.
  • the separation process may be carried out by any suitable means known to the person skilled in the art.
  • the first stage of the separation process can be carried out in an absorber column designed to provide efficient contacting between the gas mixture and the complexing solution.
  • the absorption stage of the process can utilise a hydrophobic hollow fibre membrane.
  • the complexing reaction is carried out at a temperature of from -10 to 300°C, preferably from 5 to 70°C.
  • the reaction is carried out under a pressure of from 1 to 70 barg preferably 3 to 20 barg.
  • a second step in the separation process is the removal of dissolved gases from the complex solution. This may be carried out by degassing at a temperature of from 0 to 80°C, preferably 15 to 35°C above the temperature of formation of the complex. Alternatively this step may be carried out under pressure of 2 to 98% of the absolute pressure used to form the complex, preferably 10 to 80% of the absolute pressure used to form the complex. Alternatively, a combination of reduced pressure and increased temperature may be used.
  • the third step is recovery of ethylene and/or propylene by dissociation of these gases from the metal complex.
  • this dissociation may be carried out at a temperature of from 0 to 80°C, preferably 15 to 35°C above the temperature used to remove dissolved gases.
  • this step may be carried out under pressure at 2 to 98% of the absolute pressure used to remove the dissolved gases, preferably 10 to 80% of the absolute pressure used to remove the dissolved gases.
  • a combination of reduced pressure and increased temperature may be used.
  • the regenerated olefin-free solution is then returned to the absorber column to complex more olefins.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

This invention relates to a proces comprising the steps of (a) contacting an oxygenated feedstock with a catalyst selective for the conversion of the feedstock into light olefins under conditions to produce a product stream comprising light olefins; (b) contacting said product stream with a solution of a metallic salt, said metallic salt being capable of selectively chemically absorbing the light olefins to produce a chemically absorbed olefin rich liquid stream; and (c) recovering said light olefins from the metallic salt.

Description

PROCESS FOR THE PRODUCTION OF OLEFINS
The present invention relates to a process for the production and isolation of low molecular weight olefins, and in particular to the production and isolation of ethylene and propylene.
Various processes for the production of olefins are known. A well known process is the steam cracking of paraffinic hydrocarbons containing two or more carbon atoms. Such processes, involve the pyrolysis of the hydrocarbon at high temperature. The heat required for the pyrolysis is provided by indirect heat transfer from a radiant furnace.
An alternative process is the production of olefins from an oxygenated feed such as methanol. In this process, the oxygenate feed is contacted with a suitable catalyst which is typically a molecular sieve. This process is disclosed in US 5744680, US 4912281 and US 5028400. This process has the advantage that the olefin can be obtained from a feed containing one carbon atom, the selectivity to ethylene and propylene is greater than the conventional steam cracking process and the operating temperature is significantly less.
A problem associated with the process, however, is that whilst the product stream is rich in C2/C3 olefins, also present are methane, other paraffins higher olefins and small amounts of C2/C3 acetylenic compounds, hydrogen and carbon monoxide. Ethylene and propylene are the most desired products and there is therefore a need to separate these from the product stream. Conventionally, such separation has been accomplished through the use of cryogenic distillation which is a multi-stage process comprising (1) a first step of separating and removing methane, carbon monoxide, and hydrogen via a demethaniser; (2) a second step of separating C2/C3 hydrocarbons from the heavier hydrocarbons; (3) a third step of hydrogenating the C2/C3 acetylenic compounds to ethylene and propylene; and (4) a fourth step of separating ethylene from ethane and of separating propylene from propane.
Whilst the above mentioned process is efficient, it is expensive. We have developed a means of separating and isolating the C2/C3 olefins from the product stream which is integral with the oxygenate conversion process and which avoids the use of the most expensive and energy intensive cryogenic stages as required in the conventional art.
Accordingly, the present invention provides a process for the production and recovery of light olefins, said process comprising the steps of
(a) contacting an oxygenated feedstock with a catalyst selective for the conversion of the feedstock into light olefins under conditions to produce a product stream comprising light olefins;
(b) contacting said product stream with a solution of a metallic salt, said metallic salt being capable of selectively chemically absorbing the light olefins to produce a chemically absorbed olefin rich liquid stream; and (c) recovering said light olefins from the metallic salt.
The present invention provides an effective, efficient and inexpensive means of producing and isolating the highly desirable light olefins.
For the purpose of the present invention, by light olefins is meant ethylene and propylene. The feedstock of the present process is an oxygenated feedstock. Suitable examples of an oxygenated feedstock include alcohols, ethers, aldehydes, ketones and mixtures thereof. Typically, the oxygenate feed may comprise 1 to 10 carbon atoms, preferably 1 to 4 carbon atoms. The preferred oxygenate feed is methanol.
The feedstock may be diluted with a diluent such as steam, hydrogen, nitrogen, carbon monoxide, carbon dioxide, methane and other light paraffinic hydrocarbons. The feedstock and optional diluent is contacted with a catalyst capable of converting the oxygenate feed to olefins. The catalyst is a molecular sieve. Suitable catalysts include silico alumino phosphates, for example SAPO 34 and SAPO 17, zeolites for example ZSM-5 and ZSM-11. The conversion process is carried out under conditions suitable for the production of olefins. Suitably, the process is carried out in the liquid or vapour phase. It is preferred to carry out the process in the vapour phase. Suitably the process is carried out at a temperature of from 200 to 700°C, preferably from 300 to 500°C and under a pressure of from 0.001 to 1000 atmospheres, preferably from 0.01 to 100 atmospheres. The conversion process may be carried out in any suitable reactor, for example a fixed bed, fluid bed or spouted bed reactor. The products of the process comprise light olefins, e.g. ethylene and propylene in addition to butyl enes and small amounts of hydrogen, carbon oxides, methane, acetylenes, ethane, propane, butanes and higher hydrocarbons. The products may also comprise water, which should be removed, preferably, prior to the olefin recovery step b). The products of the conversion process are contacted with a solution of a metallic salt. Optionally, but preferably, the product stream is pre-treated prior to contact with the metallic salt. The pre-treatment step may comprise one or more of amine scrubbing, catalytic oxidation and/or reduction and other steps, known to those skilled in the art, to remove components such as carbon dioxide, oxygen, hydrogen, oxygenates and the like which may be present in small amounts. Optionally, C4 and heavier hydrocarbons may also be removed in a like manner.
The product stream is contacted with a solution of a metallic salt which is capable of chemically absorbing the light olefinic products. Suitable metallic salts include salts of chromium, copper (1), manganese, nickel, iron, mercury, silver, gold, palladium, rhodium, ruthenium, osmium, molybdenum, tungsten and rhenium. The preferred metallic salt is a copper (1) salt or a silver salt. The salt may be an acetate, nitrate, sulphate, carboxylate and borates. The preferred salt is a nitrate e.g. copper (1) nitrate, silver nitrate. Equally preferred is silver fluoroborate.
The solution of metallic salt is suitably an aqueous solution and may comprise an organic nitrogen-containing compound such as pyridine, piperidene, hydroxy- propionitrile, diethylene triamine, acetonitrile, formamide, acetamide and derivatives thereof.
Suitably the concentration of metal salt to nitrogen-containing compound in the aqueous solution is in the range from 1 : 1 to 1 :6, preferably 1 :2. The concentration of metal salt in the solution is suitably at least 0.5 moles of salt per litre of solvent, preferably at least 2 moles of salt per litre of solvent.
The process for isolating the ethylene and propylene comprises contacting the product stream obtained from the oxygenate conversion process with a metal complex which is capable of complexing or absorbing ethylene and/or propylene. The separation process may be carried out by any suitable means known to the person skilled in the art. For example, the first stage of the separation process can be carried out in an absorber column designed to provide efficient contacting between the gas mixture and the complexing solution. Optionally, the absorption stage of the process can utilise a hydrophobic hollow fibre membrane. Suitably the complexing reaction is carried out at a temperature of from -10 to 300°C, preferably from 5 to 70°C. Suitably, the reaction is carried out under a pressure of from 1 to 70 barg preferably 3 to 20 barg. A second step in the separation process is the removal of dissolved gases from the complex solution. This may be carried out by degassing at a temperature of from 0 to 80°C, preferably 15 to 35°C above the temperature of formation of the complex. Alternatively this step may be carried out under pressure of 2 to 98% of the absolute pressure used to form the complex, preferably 10 to 80% of the absolute pressure used to form the complex. Alternatively, a combination of reduced pressure and increased temperature may be used.
The third step is recovery of ethylene and/or propylene by dissociation of these gases from the metal complex. Typically this dissociation may be carried out at a temperature of from 0 to 80°C, preferably 15 to 35°C above the temperature used to remove dissolved gases. Alternatively, this step may be carried out under pressure at 2 to 98% of the absolute pressure used to remove the dissolved gases, preferably 10 to 80% of the absolute pressure used to remove the dissolved gases. Alternatively, a combination of reduced pressure and increased temperature may be used.
The regenerated olefin-free solution is then returned to the absorber column to complex more olefins.

Claims

Claims
1. A process comprising the steps of
(a) contacting an oxygenated feedstock with a catalyst selective for the conversion of the feedstock into light olefins under conditions to produce a product stream comprising light olefins; (b) contacting said product stream with a solution of a metallic salt, said metallic salt being capable of selectively chemically absorbing the light olefins to produce a chemically absorbed olefin rich liquid stream; and (c) recovering said light olefins from the metallic salt.
2. A process as claimed in claim 1, wherein the oxygenated feedstock comprises compounds selected from the group consisting of: alcohols, ethers, aldehydes and ketones.
3. A process as claimed in claim 1 or 2, wherein the oxygenate feed comprises 1 to 10 carbon atoms.
4. A process as claimed in any preceding claim, wherein the catalyst capable of converting the oxygenate feed to olefins is a molecular sieve.
5. A process as claimed in any preceding claim, wherein the metallic salt is salt of chromium, copper (1), manganese, nickel, iron, mercury, silver, gold, palladium, rhodium, ruthenium, osmium, molybdenum, tungsten and/or rhenium.
6. A process as claimed in claim 5, wherein the metallic salt is selected from the group consisting of copper (1) nitrate, silver nitrate, and silver fluoroborate.
7. A process as claimed in any preceding claim, wherein the solution of metallic salt comprises an organic nitrogen-containing compound selected from the group consisting of: pyridine, piperidene, hydroxy-propionitrile, diethylene triamine, acetonitrile, formamide, acetamide and derivatives thereof.
8. A process as claimed in any preceding claim, wherein the concentration of metal salt to nitrogen-containing compound in said solution of metallic salt is in the range from 1:1 to 1:6.
9. A process as claimed in any preceding claim, wherein prior to step c), dissolved gases are removed from the chemically absorbed olefin rich liquid stream.
10. A process as claimed in any preceding claim, where the products from step a) are pre-treated prior to contact with the metallic salt in step b).
11. A process as claimed in claim 10, wherein said pre-treatment step comprises one or more of amine scrubbing, catalytic oxidation, catalytic reduction and the removal of at least one of the components selected from the group consisting of oxides of carbon, oxygen, hydrogen and oxygenates.
12. A process as claimed in claim 10 or 11, wherein the products from step a) are pre- treated to remove C4 and heavier hydrocarbons therefrom.
PCT/GB2000/000637 1999-03-09 2000-02-23 Process for the production of olefins WO2000053548A1 (en)

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GB9905422.3 1999-03-09

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Cited By (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN106478336A (en) * 2015-08-28 2017-03-08 中国石油化工股份有限公司 The separation of alcohol and/or ether olefin product and the method for by-product process
CN106478347A (en) * 2015-08-28 2017-03-08 中国石油化工股份有限公司 Alcohol and/or ether olefin product separate and the method using by-product volume increase alkene
CN106478349A (en) * 2015-08-28 2017-03-08 中国石油化工股份有限公司 Alcohol and/or ether propylene product processing method
CN106478348A (en) * 2015-08-28 2017-03-08 中国石油化工股份有限公司 Alcohol and/or the separation method of ether propylene product
CN106478344A (en) * 2015-08-28 2017-03-08 中国石油化工股份有限公司 Alcohol and/or ether propylene product separation method
CN106478343A (en) * 2015-08-28 2017-03-08 中国石油化工股份有限公司 Alcohol and/or ether propylene product separate the method utilizing
CN106478350A (en) * 2015-08-28 2017-03-08 中国石油化工股份有限公司 Alcohol and/or ether propylene product separate and the method using by-product propylene enhancing
CN106478335A (en) * 2015-08-28 2017-03-08 中国石油化工股份有限公司 The separation of alcohol and/or ether olefin product and the method for coproduction ethylbenzene
CN106478333A (en) * 2015-08-28 2017-03-08 中国石油化工股份有限公司 Alcohol and/or the separation method of ether olefin product
CN106478334A (en) * 2015-08-28 2017-03-08 中国石油化工股份有限公司 The separation of alcohol and/or ether olefin product and the method using by-product coproduction ethylbenzene
CN106478346A (en) * 2015-08-28 2017-03-08 中国石油化工股份有限公司 Alcohol and/or ether propylene product separate and the method using lighter hydrocarbons propylene enhancing
WO2023059738A1 (en) * 2021-10-06 2023-04-13 W.R. Grace & Co.-Conn. Catalytic pyrolysis of plastics to produce petrochemical feedstock

Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5744680A (en) * 1995-08-10 1998-04-28 Uop Process for producing light olefins

Patent Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5744680A (en) * 1995-08-10 1998-04-28 Uop Process for producing light olefins

Cited By (23)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN106478336A (en) * 2015-08-28 2017-03-08 中国石油化工股份有限公司 The separation of alcohol and/or ether olefin product and the method for by-product process
CN106478347A (en) * 2015-08-28 2017-03-08 中国石油化工股份有限公司 Alcohol and/or ether olefin product separate and the method using by-product volume increase alkene
CN106478349A (en) * 2015-08-28 2017-03-08 中国石油化工股份有限公司 Alcohol and/or ether propylene product processing method
CN106478348A (en) * 2015-08-28 2017-03-08 中国石油化工股份有限公司 Alcohol and/or the separation method of ether propylene product
CN106478344A (en) * 2015-08-28 2017-03-08 中国石油化工股份有限公司 Alcohol and/or ether propylene product separation method
CN106478343A (en) * 2015-08-28 2017-03-08 中国石油化工股份有限公司 Alcohol and/or ether propylene product separate the method utilizing
CN106478350A (en) * 2015-08-28 2017-03-08 中国石油化工股份有限公司 Alcohol and/or ether propylene product separate and the method using by-product propylene enhancing
CN106478335A (en) * 2015-08-28 2017-03-08 中国石油化工股份有限公司 The separation of alcohol and/or ether olefin product and the method for coproduction ethylbenzene
CN106478333A (en) * 2015-08-28 2017-03-08 中国石油化工股份有限公司 Alcohol and/or the separation method of ether olefin product
CN106478334A (en) * 2015-08-28 2017-03-08 中国石油化工股份有限公司 The separation of alcohol and/or ether olefin product and the method using by-product coproduction ethylbenzene
CN106478346A (en) * 2015-08-28 2017-03-08 中国石油化工股份有限公司 Alcohol and/or ether propylene product separate and the method using lighter hydrocarbons propylene enhancing
CN106478343B (en) * 2015-08-28 2018-10-23 中国石油化工股份有限公司 Alcohol and/or ether propylene product detach the method utilized
CN106478344B (en) * 2015-08-28 2018-10-23 中国石油化工股份有限公司 Alcohol and/or ether propylene product separation method
CN106478346B (en) * 2015-08-28 2018-10-23 中国石油化工股份有限公司 Alcohol and/or the separation of ether propylene product and the method using lighter hydrocarbons propylene enhancing
CN106478347B (en) * 2015-08-28 2018-10-23 中国石油化工股份有限公司 Alcohol and/or the separation of ether olefin product and the method for increasing production alkene using by-product
CN106478350B (en) * 2015-08-28 2018-10-23 中国石油化工股份有限公司 Alcohol and/or the separation of ether propylene product and the method using by-product propylene enhancing
CN106478333B (en) * 2015-08-28 2018-10-23 中国石油化工股份有限公司 The separation method of alcohol and/or ether olefin product
CN106478348B (en) * 2015-08-28 2018-11-20 中国石油化工股份有限公司 The separation method of alcohol and/or ether propylene product
CN106478349B (en) * 2015-08-28 2018-11-20 中国石油化工股份有限公司 Alcohol and/or ether propylene product processing method
CN106478336B (en) * 2015-08-28 2019-04-12 中国石油化工股份有限公司 The method of the separation of alcohol and/or ether olefin product and by-product processing
CN106478335B (en) * 2015-08-28 2019-05-14 中国石油化工股份有限公司 The method of the separation and coproduction ethylbenzene of alcohol and/or ether olefin product
CN106478334B (en) * 2015-08-28 2019-05-14 中国石油化工股份有限公司 The separation of alcohol and/or ether olefin product and the method for utilizing by-product coproduction ethylbenzene
WO2023059738A1 (en) * 2021-10-06 2023-04-13 W.R. Grace & Co.-Conn. Catalytic pyrolysis of plastics to produce petrochemical feedstock

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GB9905422D0 (en) 1999-05-05

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