EP4259750A1 - Procédé de vapocraquage d' une charge contenant du chlore - Google Patents

Procédé de vapocraquage d' une charge contenant du chlore

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Publication number
EP4259750A1
EP4259750A1 EP21794979.1A EP21794979A EP4259750A1 EP 4259750 A1 EP4259750 A1 EP 4259750A1 EP 21794979 A EP21794979 A EP 21794979A EP 4259750 A1 EP4259750 A1 EP 4259750A1
Authority
EP
European Patent Office
Prior art keywords
stream
steam
chlorine
hydrocarbon
ppm
Prior art date
Legal status (The legal status 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 status listed.)
Pending
Application number
EP21794979.1A
Other languages
German (de)
English (en)
Inventor
Safa FARAJZADEH BIBALAN
Laura Bini
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
SABIC Global Technologies BV
Original Assignee
SABIC Global Technologies BV
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 SABIC Global Technologies BV filed Critical SABIC Global Technologies BV
Publication of EP4259750A1 publication Critical patent/EP4259750A1/fr
Pending legal-status Critical Current

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
    • C10G1/10—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal from rubber or rubber waste
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
    • C10G1/002—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal in combination with oil conversion- or refining processes
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G9/34—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by direct contact with inert preheated fluids, e.g. with molten metals or salts
    • C10G9/36—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by direct contact with inert preheated fluids, e.g. with molten metals or salts with heated gases or vapours
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/20—Characteristics of the feedstock or the products
    • C10G2300/201—Impurities
    • C10G2300/202—Heteroatoms content, i.e. S, N, O, P
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
    • C10G2400/20—C2-C4 olefins

Definitions

  • the present invention generally relates to steam cracking processes. More specifically, the present invention relates to a method of processing a plastic derived pyrolysis oil (“pyoil”) to produce a feed stream for a steam cracker.
  • plyoil plastic derived pyrolysis oil
  • a solution to at least the above mentioned problem associated with methods for lowering heteroatom contaminants content is discovered.
  • the solution resides in a method for processing pyoil that includes mixing pyoil with naphtha and steam. This can be beneficial for diluting the contaminants in the pyoil without using a large amount of naphtha, thereby reducing production cost compared to conventional methods.
  • the disclosed method can further include constructing a numerical model for correlation between steam to hydrocarbon ratios and chlorine contents such that an optimized steam to hydrocarbon ratio can be determined to minimize the effect of the contaminants in a steam cracking unit while maintaining a low production cost for steam cracking the pyoil, compared to conventional methods. Therefore, the methods of the present invention provide a technical solution to the problem associated with the conventional methods for lowering contaminants in plastic derived pyoil.
  • Embodiments of the invention include a method of processing pyoil.
  • the method comprises mixing a pyoil obtained via pyrolysis of plastics with naphtha to produce a hydrocarbon stream having a chlorine (element) content lower than a chlorine (element) content of the pyoil.
  • the method includes mixing the hydrocarbon stream with steam to form a feed stream.
  • the method includes steam cracking the feed stream under reaction conditions sufficient to produce olefins.
  • Embodiments of the invention include a method of processing pyoil.
  • the method comprises mixing a pyoil obtained via pyrolysis of plastics with naphtha to produce a hydrocarbon stream comprising 1 to 3 ppm chlorine.
  • the pyoil comprises more than 60 ppm chlorine.
  • the method comprises mixing the hydrocarbon stream with steam at a steam to hydrocarbon mass ratio of greater than 0.35 to form a feed stream having a chlorine (element) content less than a chlorine content of the hydrocarbon stream.
  • the method comprises steam cracking the feed stream under reaction conditions sufficient to produce olefins.
  • Embodiments of the invention include a method of processing plastics.
  • the method comprises (a) processing plastics under pyrolysis conditions sufficient to produce a pyoil comprising hydrocarbons and more than 60 ppm chlorine.
  • the method comprises (b) mixing the pyoil with naphtha to produce a hydrocarbon stream comprising 1 to 3 ppm chlorine.
  • the method comprises (c) mixing the hydrocarbon stream with steam at a first steam to hydrocarbon ratio to produce a first feed stream.
  • the method comprises (d) steam cracking, in a steam cracker, the feed stream under reaction conditions sufficient to produce an effluent stream comprising olefins, aromatics and steam.
  • the method comprises (e) separating the effluent stream in a separation unit to produce one or more product streams comprising an ethylene stream, a propylene stream, a C4 stream, and a pyrolysis gas stream.
  • the method comprises (f) determining chlorine content of one or more process streams produced during steps (d) and (e).
  • the method comprises (g) repeating steps (c) to (f) but with a second steam to hydrocarbon ratio in step (c) to obtain data for steam to hydrocarbon ratios and chlorine contents of the one or more process streams.
  • the method comprises (h) constructing a numerical model for correlation between steam to hydrocarbon ratios and chlorine contents of the one or more process streams.
  • the method comprises (i) determining a final steam to hydrocarbon ratio using the numerical model such that the chlorine contents for the one or more process streams are each below 3 ppm.
  • the method comprises (j) operating the steam cracker using the final steam to hydrocarbon ratio to process the hydrocarbon stream.
  • wt.% refers to a weight, volume, or molar percentage of a component, respectively, based on the total weight, the total volume, or the total moles of material that includes the component.
  • 10 moles of component in 100 moles of the material is 10 mol.% of component.
  • circular polymer means a polymer made from ethylene or propylene, which is produced by steam cracking pyrolysis oil.
  • chlorine content means concentration of chlorine element.
  • the chlorine element exist in molecular structure(s) of chlorinated compound(s).
  • primarily means greater than any of 50 wt.%, 50 mol.%, and 50 vol.%.
  • “primarily” may include 50.1 wt.% to 100 wt.% and all values and ranges there between, 50.1 mol.% to 100 mol.% and all values and ranges there between, or 50.1 vol.% to 100 vol.% and all values and ranges there between.
  • FIG. 1 shows a schematic flowchart for a method of processing a plastic, according to embodiments of the invention
  • FIG. 2 shows a schematic diagram of a cracking unit, according to embodiments of the invention
  • FIG. 3 shows a schematic flowchart for a method of processing a pyoil, according to embodiments of the invention
  • FIG. 4 shows comparison of measured chlorine levels with model predicted chlorine levels in process water of a steam cracking unit
  • FIG. 5 shows comparison of measured chlorine levels with model predicted chlorine levels in a steam/liquid water separator bottom stream of a steam cracking unit
  • FIG. 6 shows predicted chlorine concentration in process water as a function of steam to oil (hydrocarbon) ratio.
  • plastic derived pyoil which contains a high level of heteroatom contaminants including chlorine, is processed by blending the pyoil with a large amount of naphtha at a pyoil to naphtha mass ratio up to 1 : 167.
  • This can be costly due to the high cost of naphtha, resulting in low financial feasibility of the whole process.
  • the present invention provides a solution to this problem. The solution is premised on a method of processing pyoil.
  • the disclosed method of processing pyoil includes blending the pyoil with naphtha to form a hydrocarbon stream and further diluting the hydrocarbon stream with steam to produce a feed stream for steam crackers that has a chlorine level that is safe for the steam cracking units. This can significantly reduce the amount of naphtha needed for blending with pyoil, thereby reducing the overall cost for lowering chlorine level in pyoil.
  • the disclosed method can include constructing a numerical model correlating hydrocarbon stream to steam mass ratio and chlorine contents of one or more process streams in a steam cracking unit.
  • the numerical model can be used to obtained an optimized hydrocarbon to steam mass ratio that can ensure production efficiency and low chlorine level in the steam cracking unit, resulting in improved production efficiency from pyoil and increased safety level of processing pyoil.
  • the method for processing plastics comprises constructing a numerical model that correlates hydrocarbon to steam ratio with chlorine levels in process streams in steam cracking units.
  • a flow chart is shown for method 100 of processing plastics.
  • method 100 includes processing plastics under pyrolysis conditions sufficient to produce a pyoil comprising hydrocarbons and more than 60 ppm chlorine.
  • the plastics comprise polyolefins, polyethylene terephthalate (PET), polyamide (PA) and polyvinyl chloride (PVC), polystyrene (PS), acrylonitrile butadiene styrene (ABS), or combinations thereof.
  • the pyrolysis conditions include a pyrolysis temperature of 300 to 700 °C and all ranges and values there between including ranges of 300 to 350 °C, 350 to 400 °C, 400 to 450 °C, 450 to 500 °C, 500 to 550 °C, 550 to 600 °C, 600 to 650 °C, and 650 to 700 °C.
  • the pyrolysis conditions further include a pyrolysis pressure of 1 to 5 bar.
  • the pyoil comprises 60 to 600 ppm chlorine and all ranges and values there between including ranges of 60 to 120 ppm, 120 to 180 ppm, 180 to 240 ppm, 240 to 300 ppm, 300 to 360 ppm, 360 to 420 ppm, 420 to 480 ppm, 480 to 540 ppm, and 540 to 600 ppm.
  • method 100 includes mixing the pyoil with naphtha to produce a hydrocarbon stream.
  • the hydrocarbon stream can comprise 1 to 3 ppm chlorine and all ranges and values there between including ranges of 0.1 to 0.3 ppm, 0.3 to 0.6 ppm, 0.6 to 0.9 ppm, 0.9 to 1.2 ppm, 1.2 to 1.5 ppm, 1.5 to 1.8 ppm, 1.8 to 2.1 ppm, 2.1 to 2.4 ppm, 2.4 to 2.7 ppm, and 2.7 to 3.0 ppm..
  • the pyoil and the naphtha are mixed at a pyoil to naphtha mass ratio of 1 :400 to 1:60 and all ranges and values there between.
  • the naphtha includes light virgin naphtha, and/or full range naphtha.
  • naphtha can include C4 to C10 hydrocarbons.
  • method 100 includes mixing the hydrocarbon stream with steam at a first steam to hydrocarbon ratio to produce a first feed stream.
  • the steam is at a temperature of 180 to 300 °C.
  • the first steam to hydrocarbon ratio can be in a range of 0.35 to 1.0 and all ranges and values there between including ranges of 0.35 to 0.40, 0.40 to 0.45, 0.45 to 0.50, 0.50 to 0.55, 0.55 to 0.60, 0.60 to 0.65, 0.65 to 0.70, 0.70 to 0.75, 0.75 to 0.80, 0.80 to 0.85, 0.85 to 0.90, 0.90 to 0.95, 0.90 to 0.95, and 0.95 to 1.0.
  • method 200 includes steam-cracking, in a steam cracker, the first the feed stream under reaction conditions sufficient to produce an effluent stream comprising olefins, aromatics, and steam.
  • the reaction conditions can include a cracking temperature of 780 to 870 °C and a residence time of the steam cracker of 10 to 700 ms.
  • method 100 includes separating the effluent stream in a separation unit to produce one or more product streams comprising an ethylene stream comprising primarily ethylene, a propylene stream comprising primarily propylene, a C4 stream comprising primarily C4 hydrocarbons, and a pyrolysis gas stream comprising pyrolysis gas.
  • the steam cracking at block 104 and separating at block 105 are implemented in steam cracking unit 200, as shown in FIG. 2.
  • Cracking unit 200 can include steam cracker 201 configured to receive feed stream 11 obtained at block 103 and crack feed stream 11 to produce effluent stream 12 comprising olefins, aromatics, and steam.
  • Cracking unit 200 can include primarily fractionator 202 configured to separate effluent stream 12 to form first top stream 13 comprising olefins, aromatics, and steam, carbon black oil stream 14 comprising primarily carbon black oil, and cracked distillate stream 15 comprising primarily naphthalenes.
  • Cracking unit 200 can further include water quench column 203 configured to quench first top stream 13 to produce quench water stream 16 comprising primarily water and 0.1 to 20 ppm chlorine, quench effluent stream 18 comprising primarily Ci to Cs hydrocarbons, and pygas stream 17 comprising Cs+ pyrolysis gasoline.
  • an outlet of water quench column 203 is in fluid communication with an inlet of steam/liquid water separator 220 such that quench water stream 16 flows from water quench column 203 to steam/liquid water separator 220.
  • Steam liquid water separator 220 can be configured to separate quench water stream 16 to produce (1) purge stream 42 comprising water and contaminants including chlorine, and (2) recycle stream 41 comprising steam. Recycle stream 41 can be flowed back to steam cracker 201.
  • Cracking unit 200 can include compressor 204 configured to compress quench effluent stream 18 to produced compressed effluent stream 19 and additional pygas stream 20. Additional pygas stream 20 can include a liquid fraction of quench effluent stream 18. In embodiments of the invention, pygas stream 17 and additional pygas stream 20 can form combined pygas stream 38. In embodiments of the invention, combined pygas stream 38 comprises 0.1 to 1 ppm chlorine element. According to embodiments of the invention, cracking unit 200 can include acid removal unit 205 configured to remove acid from compressed effluent stream 19 to produce acid stream 21 comprising one or more acids and acid-free effluent stream 22.
  • Acid-free effluent stream 22 can be compressed in second compressor 206 and then cooled down in cold box 207 to form light stream 23 comprising primarily methane and hydrogen, collectively, and demethanizer feed stream 24.
  • Cracking unit 200 can further comprise demethanizer 208 configured to remove methane from demethanizer feed stream 24 to form methane stream 25 and deethanizer feed stream 26.
  • methane stream 25 is recycled back to cold box 207.
  • Deethanizer feed stream 26 can be further processed in deethanizer 209 to produce C2 stream 27 comprising primarily C2 hydrocarbons and depropanizer feed stream 28.
  • C2 stream 27 may be further processed in acetylene extraction unit 210 to remove acetylene stream 29 comprising primarily acetylene, and then in C2 splitter 211 to produce ethylene stream 30 comprising primarily ethylene, and ethane stream 31 comprising primarily ethane.
  • Cracking unit 200 can further comprise depropanizer 212 configured to separate depropanizer feed stream 28 to form C3 stream 32 comprising primarily C3 hydrocarbons, and debutanizer feed stream 33.
  • C3 stream 32 may be further processed in MAPD reactor 213 and C3 splitter 214 to produce propylene stream 34 comprising primarily propylene, and propane stream 35 comprising propane.
  • MAPD reactor 213 can be configured to remove methyl acetylene and propadiene (MAPD) prior to entering C3 splitter.
  • cracking unit 200 can further include debutanizer 215 configured to separate debutanizer feed stream 33 to produce C4 stream 36 comprising C4 hydrocarbons, and C5+ stream 37 comprising primarily C5+ hydrocarbons.
  • each of demethanizer 208, deethanizer 209, C2 splitter 211, depropanizer 212, C3 splitter 214, and debutanizer 215 includes a distillation column.
  • method 100 comprises determining chlorine content of one or more process streams produced at blocks 104 and 105.
  • the process streams at block 106 can include cracked distillate stream 15, feed stream 11, quench water stream 16, acid stream 21, combined pygas stream 38, debutanizer feed stream 33, final pygas stream 39, or combinations thereof.
  • the determining of chlorine content at block 106 is conducted by sampling of inlet and downstream of the plant according to Cl mass balance. In embodiments of the invention, about 80% of the chlorine intake is in the process water (quench water stream 16).
  • method 100 comprises repeating blocks 103 to 106 but with a second steam to hydrocarbon ratio at block 103 to obtain data for steam to hydrocarbon ratios and chlorine contents of the one or more process streams in cracking unit 200.
  • the steam to hydrocarbon ratios are controlled in a range of 0.35 to 1.0 and all ranges and values there between including ranges of 0.35 to 0.40, 0.40 to 0.45, 0.45 to 0.50, 0.50 to 0.55, 0.55 to 0.60, 0.60 to 0.65, 0.65 to 0.70, 0.70 to 0.75, 0.75 to 0.80, 0.80 to 0.85, 0.85 to 0.90, 0.90 to 0.95, 0.90 to 0.95, and 0.95 to 1.0.
  • method 100 comprises constructing a numerical model for correlation between steam to hydrocarbon ratios and chlorine contents of the one or more process streams.
  • the numerical model is constructed using sampling of inlet and downstream of the plant according to mass balance of Cl.
  • a conversion rate of 88% was obtained for Cl in feed stream to end up in the process water (quench water stream 16).
  • the numerical model is configured to predict chlorine content in the one or more process streams of cracking unit 200 using steam to hydrocarbon ratios as inputs.
  • method 100 comprises determining a final steam to hydrocarbon ratio using the numerical model constructed at block 108 such that the chlorine contents for the one or more process streams of cracking unit 200 are each below a pre-determined level.
  • the pre-determined level is configured to minimize corrosion rate in cracking unit 200.
  • the pre-determined level can be 3 ppm.
  • the determining includes plug in a target chlorine level by using a calculated value of conversion rate for Cl (e.g., 88%) from feed stream 11 to the process water (quench water stream 16).
  • the target chlorine level is obtained at block 108.
  • method 100 can include operating the steam cracker (steam cracker 201 of cracking unit 200) using the final steam to hydrocarbon ratio obtained in block 109 to process the hydrocarbon stream.
  • embodiments of the invention include method 300 of processing pyoil.
  • method 300 includes mixing a pyoil obtained via pyrolysis of plastics with naphtha to produce a hydrocarbon stream having a chlorine (element) content lower than a chlorine (element) content of the pyoil.
  • the plastics include polyolefins, polyethylene terephthalate (PET), polyamide (PA) and polyvinyl chloride (PVC), polystyrene (PS), acrylonitrile butadiene styrene (ABS), or combinations thereof.
  • the pyoil can comprise more than 60 ppm elemental chlorines.
  • naphtha and pyoil are mixed at a mass ratio of up to 167: 1, preferably 50: 1.
  • the naphtha includes hydrocarbons having a boiling range of 35 to 200 °C.
  • the pyoil includes hydrocarbons having a boiling range of 35 to 390 °C.
  • the pyoil comprises more than 60 ppm chlorine element, preferably 60 to 600 ppm chlorine and all ranges and values there between including ranges of 60 to 120 ppm, 120 to 180 ppm, 180 to 240 ppm, 240 to 300 ppm, 300 to 360 ppm, 360 to 420 ppm, 420 to 480 ppm, 480 to 540 ppm, and 540 to 600 ppm.
  • the hydrocarbon stream comprises 1 to 3 ppm of chlorine element and all ranges and values there between including ranges of 1 to 1.2 ppm, 1.2 to 1.4 ppm, 1.4 to 1.6 ppm, 1.6 to 1.8 ppm, 1.8 to 2.0 ppm, 2.0 to 2.2 ppm, 2.2 to 2.4 ppm, 2.4 to 2.6 ppm, 2.6 to 2.8 ppm, and 2.8 to 3 ppm.
  • method 300 includes mixing the hydrocarbon stream with steam to form a feed stream.
  • the hydrocarbon stream is mixed with steam at a steam to hydrocarbon mass ratio of greater than 0.35, preferably 0.35 to 1 and all ranges and values there between including ranges of 0.35 to 0.40, 0.40 to 0.45, 0.45 to 0.50, 0.50 to 0.55, 0.55 to 0.60, 0.60 to 0.65, 0.65 to 0.70, 0.70 to 0.75, 0.75 to 0.80, 0.80 to 0.85, 0.85 to 0.90, 0.90 to 0.95, and 0.95 to 1.
  • the feed stream comprises 0.2 to 1.6 ppm chlorine (element), preferably 0.2 to 0.8 ppm and all ranges and values there between including ranges of 0.2 to 0.3 ppm, 0.3 to 0.4 ppm, 0.4 to 0.5 ppm, 0.5 to 0.6 ppm, 0.6 to 0.7 ppm, and 0.7 to 0.8 ppm.
  • the steam is at a temperature of 180 to 300 °C and all ranges and values there between including ranges of 180 to 190 °C, 190 to 200 °C, 200 to 210 °C, 210 to 220 °C, 220 to 230 °C, 230 to 240 °C, 240 to 250 °C, 250 to 260 °C, 260 to 270 °C, 270 to 280 °C, 280 to 290 °C, and 290 to 300 °C.
  • method 300 includes steam cracking the feed stream under reaction conditions sufficient to produce olefins.
  • the steam-cracking at block 303 is conducted in cracking unit 200.
  • the olefins produced at block 303 include ethylene, propylene, C4 olefins, or combinations thereof.
  • Steam-cracking at block 303 can be conducted at a cracking temperature of 780 to 870 °C and all ranges and values there between including ranges of 780 to 790 °C, 790 to 800 °C, 800 to 810 °C, 810 to 820 °C, 820 to 830 °C, 830 to 840 °C, 840 to 850 °C, 850 to 860 °C, and 860 to 870 °C.
  • Steam-cracking at block 303 is conducted at a residence time in a range of 10 to 700 ms and all ranges and values there between including ranges of 10 to 50 ms, 50 to 100 ms, 100 to 150 ms, 150 to 200 ms, 200 to 250 ms, 250 to 300 ms, 300 to 350 ms, 350 to 400 ms, 400 to 450 ms, 450 to 500 ms, 500 to 550 ms, 550 to 600 ms, 600 to 650 ms, and 650 to 700 ms.
  • the systems and processes described herein can also include various equipment that is not shown and is known to one of skill in the art of chemical processing. For example, some controllers, piping, computers, valves, pumps, heaters, thermocouples, pressure indicators, mixers, heat exchangers, and the like may not be shown.
  • a pyoil comprising 50 to 226 ppm chlorine is blended with naphtha to reduce the chlorine concentration in the blend to 1 to 3 ppm.
  • Regular steam cracker feedstocks such as gas condensate and naphtha contain chlorine at level of less than 0.1 to 1.0 ppm.
  • FIG. 6 shows the predicted chlorine concentration in the process water as a function of steam-to-oil ratio.
  • Embodiment 1 is a method of processing pyoil.
  • the method includes mixing a pyoil obtained via pyrolysis of plastics with naphtha to produce a hydrocarbon stream having a chlorine content lower than a chlorine content of the pyoil.
  • the method further includes mixing the hydrocarbon stream with steam to form a feed stream.
  • the method still further includes steam cracking the feed stream under reaction conditions sufficient to produce olefins.
  • Embodiment 2 is the method of embodiment 1, wherein the pyoil contains more than 60 ppm chlorine.
  • Embodiment 3 is the method of any of embodiments 1 and 2, wherein the hydrocarbon stream contains 1 to 3 ppm elemental chlorine.
  • Embodiment 4 is the method of any of embodiments 1 to 3, wherein the feed stream has a chlorine content less than a chlorine content of the hydrocarbon stream.
  • Embodiment 5 is the method of any of embodiments 1 to 4, wherein the hydrocarbon stream is mixed with steam at a mass ratio greater than 0.35.
  • Embodiment 6 is the method of any of embodiments 1 to 5, wherein the plastic includes polyolefins, polyethylene terephthalate (PET), polyamide (PA) and polyvinyl chloride (PVC), polystyrene (PS), acrylonitrile butadiene styrene (ABS), or combinations thereof.
  • Embodiment 7 is the method of any of embodiments 1 to 6, wherein the naphtha and the pyoil are mixed at a mass ratio of up to 167: 1, preferably 50: 1.
  • Embodiment 8 is a method of processing plastics.
  • the method includes: (a) processing plastics under pyrolysis conditions sufficient to produce a pyoil containing hydrocarbons and more than 60 ppm chlorine; (b) mixing the pyoil with naphtha to produce a hydrocarbon stream containing 1 to 3 ppm chlorine; (c) mixing the hydrocarbon stream with steam at a first steam to hydrocarbon ratio to produce a first feed stream; (d) steam cracking, in a steam cracker, the first feed stream under reaction conditions sufficient to produce an effluent stream containing olefins, aromatics and steam; (e) separating the effluent stream in a separation unit to produce one or more product streams containing an ethylene stream, a propylene stream, a C4 stream, and a pyrolysis gas stream; (f) determining chlorine content of one or more process streams produced during steps (d) and (e); (g) repeating steps (c) to (f) but with a second
  • Embodiment 9 is the method of embodiment 8, wherein the separating at step (e) can include separating effluent stream from the steam cracker to produce a top stream containing Ci-Cs hydrocarbons and steam, a cracked distillate containing C9-C12 hydrocarbons, and carbon black oil containing C12+ hydrocarbons.
  • Embodiment 10 is the method of any of embodiment 8 and 9, wherein step (e) further includes quenching the top stream to produce a quench water stream containing 0.1 to 20 ppm chlorine, a quench effluent stream containing ethylene, propylene, C4 hydrocarbons, C5+ hydrocarbons, and a pygas stream containing C5+ hydrocarbons.
  • Embodiment 11 is the method of any of embodiments 8 to 9, wherein the pygas stream is combined with a compressed liquid fraction of the quench effluent stream to form a combined pyrolysis gas stream.
  • Embodiment 12 is the method of any embodiments 8 to 10, wherein the combined pyrolysis gas stream contains 0.1 to 1 ppm chlorine. All embodiments described above and herein can be combined in any manner unless expressly excluded.

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Abstract

L'invention concerne un procédé de mise en œuvre d'un plastique et un procédé de traitement d'une huile de pyrolyse provenant d'un plastique. L'invention permet de construire un modèle numérique d'une corrélation entre la teneur en chlore d'un ou plusieurs courants de procédé d'une unité de vapocraquage et un rapport hydrocarbure/vapeur dans un courant de charge de l'unité de vapocraquage. Un mélange d'huile de pyrolyse et de naphta est mélangé à de la vapeur, selon un rapport hydrocarbure/vapeur obtenu à partir du modèle, dans le but de produire le courant de charge d'une unité de vapocraquage. Le courant de charge est traité dans l'unité de vapocraquage pour produire des oléfines.
EP21794979.1A 2020-12-10 2021-10-12 Procédé de vapocraquage d' une charge contenant du chlore Pending EP4259750A1 (fr)

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US202063123998P 2020-12-10 2020-12-10
PCT/IB2021/059340 WO2022123338A1 (fr) 2020-12-10 2021-10-12 Procédé de vapocraquage d'une charge contenant du chlore

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EP4259750A1 true EP4259750A1 (fr) 2023-10-18

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US (1) US20240010918A1 (fr)
EP (1) EP4259750A1 (fr)
JP (1) JP2023552612A (fr)
CN (1) CN116635504A (fr)
WO (1) WO2022123338A1 (fr)

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WO2024115058A1 (fr) * 2022-11-28 2024-06-06 Sabic Global Technologies B.V. Procédé et composition de recyclage chimique de polymères à teneur réduite en chlore

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JP6378368B2 (ja) * 2014-02-25 2018-08-22 サウジ ベーシック インダストリーズ コーポレイションＳａｕｄｉ Ｂａｓｉｃ Ｉｎｄｕｓｔｒｉｅｓ Ｃｏｒｐｏｒａｉｔｏｎ 混合廃プラスチック類（ｍｗｐ）を有益な石油化学製品に変換する方法
WO2016142806A1 (fr) * 2015-03-10 2016-09-15 Sabic Global Technologies, B.V. Procédé d'hydrocraquage de flux d'hydrocarbures et d'huiles de pyrolyse
WO2016142808A1 (fr) * 2015-03-10 2016-09-15 Sabic Global Technologies, B.V. Processus intégré de conversion de déchets plastiques en produits pétrochimiques finaux

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US20240010918A1 (en) 2024-01-11
CN116635504A (zh) 2023-08-22
WO2022123338A1 (fr) 2022-06-16
JP2023552612A (ja) 2023-12-18

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