EP4004151A1 - Réacteur à lit fluidisé à phase dense pour maximiser le rendement de production de btx - Google Patents

Réacteur à lit fluidisé à phase dense pour maximiser le rendement de production de btx

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Publication number
EP4004151A1
EP4004151A1 EP20751300.3A EP20751300A EP4004151A1 EP 4004151 A1 EP4004151 A1 EP 4004151A1 EP 20751300 A EP20751300 A EP 20751300A EP 4004151 A1 EP4004151 A1 EP 4004151A1
Authority
EP
European Patent Office
Prior art keywords
catalyst
fluidized bed
reaction conditions
produce
regenerated catalyst
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
EP20751300.3A
Other languages
German (de)
English (en)
Inventor
Talal Abdullah ALDUGMAN
Ernesto UEHARA
Mao Ye
Xie PENG
Talal Khaled AL-SHAMMARI
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 EP4004151A1 publication Critical patent/EP4004151A1/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
    • C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G11/14—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts
    • C10G11/16—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts according to the "moving bed" method
    • 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
    • C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G11/14—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts
    • C10G11/18—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts according to the "fluidised-bed" technique
    • C10G11/182—Regeneration
    • 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
    • C10G2300/10—Feedstock materials
    • C10G2300/1037—Hydrocarbon fractions
    • C10G2300/104—Light gasoline having a boiling range of about 20 - 100 °C
    • 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
    • C10G2300/10—Feedstock materials
    • C10G2300/1037—Hydrocarbon fractions
    • C10G2300/1044—Heavy gasoline or naphtha having a boiling range of about 100 - 180 °C
    • 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
    • C10G2300/30—Physical properties of feedstocks or products
    • C10G2300/308—Gravity, density, e.g. API
    • 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
    • C10G2300/40—Characteristics of the process deviating from typical ways of processing
    • C10G2300/4006—Temperature
    • 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
    • C10G2300/40—Characteristics of the process deviating from typical ways of processing
    • C10G2300/4012—Pressure
    • 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
    • C10G2300/40—Characteristics of the process deviating from typical ways of processing
    • C10G2300/4018—Spatial velocity, e.g. LHSV, WHSV
    • 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
    • C10G2300/70—Catalyst aspects
    • 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
    • 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
    • C10G2400/30—Aromatics

Definitions

  • the present invention generally relates to systems and methods for producing aromatics. More specifically, the present invention relates to systems and methods of maximizing the production of benzene, toluene, and xylene via catalytic cracking of naphtha in a dense phase fluidized bed reactor.
  • BTX benzene, toluene, and xylene
  • benzene is a precursor for producing polystyrene, phenolic resins, polycarbonate, and nylon.
  • Toluene is used for producing polyurethane and as a gasoline component.
  • Xylene is feedstock for producing polyester fibers and phthalic anhydride.
  • benzene, toluene, and xylene are conventionally produced by catalytic reforming of naphtha.
  • Another conventional method for producing aromatics includes catalytic cracking of naphtha in a fluidized bed.
  • the conventional fluidized bed reactors are generally operated with low average solid volume fraction and low gas-solids contact efficiency due to the limitation of superficial gas velocities in the fluidized bed.
  • the products of the conventional methods often include a high methane content produced from thermal cracking of hydrocarbons, resulting in increased production cost for aromatics.
  • a solution to at least some of the above-mentioned problems associated with the production process for aromatics has been discovered.
  • the solution resides in a method of producing aromatics via catalytic cracking of naphtha.
  • the method includes operating a fluidized bed reactor with a solids volume fraction of 0.35 to 0.45, which can maximize the production of BTX and increase ratio of BTX to light olefins in the product stream.
  • the method includes feeding naphtha at a superficial gas velocity in the fluidized bed reactor of 0.25 to 0.5 m/s, resulting in high contact time between the naphtha and the catalyst and wide residence time distribution. This can be beneficial to at least increase the yield of BTX.
  • the method can include flowing the feed naphtha and the catalyst counter-currently, thereby further enhancing the contact between the catalyst and naphtha and increasing BTX production efficiency.
  • the fluidized bed reactor used in the method can include internals that break bubbles formed during the catalytic cracking process, leading to more effective contact between the naphtha and the catalyst. Therefore, the method of the present invention provides a technical solution to at least some of the problems associated with the conventional methods for producing aromatics mentioned above.
  • Embodiments of the invention include a method of producing aromatics.
  • the method comprises contacting a mixture of hydrocarbons having an initial boiling point of less than 250 °C with catalyst in a fluidized bed under reaction conditions effective to produce one or more aromatics.
  • the reaction conditions comprise the fluidized bed having an average solids volume fraction in a range of 0.35 to 0.45.
  • Embodiments of the invention include a method of producing aromatics.
  • the method comprises contacting naphtha comprising a mixture of hydrocarbons having an initial boiling point of less than 250 °C with catalyst in a dense phase fluidized bed under reaction conditions effective to produce one or more aromatics.
  • the reaction conditions comprise the dense phase fluidized bed having an average solids volume fraction in a range of 0.35 to 0.45 and a superficial gas velocity of 0.25 to 0.5 m/s.
  • the naphtha is flowed in a direction counter current to flow of the catalyst in the dense phase fluidized bed.
  • Embodiments of the invention include a method of producing olefins and/or aromatics.
  • the method comprises contacting naphtha comprising a mixture of hydrocarbons having an initial boiling point of less than 250 °C with catalyst in a dense phase fluidized bed under reaction conditions effective to produce one or more olefins and/or one or more aromatics.
  • the reaction conditions comprise the dense phase fluidized bed having an average solids volume fraction in a range of 0.35 to 0.45 and a superficial gas velocity of 0.25 to 0.5 m/s.
  • the naphtha is flowed through a sparger feed distributor into a reactor in a direction counter current to flow of the catalyst in the dense phase fluidized bed.
  • the catalyst is flowed into the reactor through a catalyst distributor.
  • the terms“about” or“approximately” are defined as being close to as understood by one of ordinary skill in the art. In one non-limiting embodiment the terms are defined to be within 10%, preferably, within 5%, more preferably, within 1%, and most preferably, within 0.5%.
  • the terms“wt.%”,“vol.%” or“mol.%” refer 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. In a non-limiting example, 10 moles of component in 100 moles of the material is 10 mol.% of component.
  • “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 diagram of a system for catalytically cracking a hydrocarbon mixture, according to embodiments of the invention.
  • FIG. 2 shows a schematic flowchart of a method of producing aromatics via catalytic cracking of a hydrocarbon mixture, according to embodiments of the invention.
  • aromatics, especially BTX, and light olefins can be produced by steam cracking or catalytic cracking of naphtha.
  • the overall conversion rate to BTX and/or light olefins for steam cracking naphtha is relatively low.
  • the production costs for steam cracking naphtha are high as steam cracking of naphtha produces a large amount of raffinate, which needs to be hydrogenated before it is recycled back to the steam cracking unit.
  • the large amount raffinate results in high demand for hydrogen and energy in the hydrogenation process.
  • the disclosed method includes flowing the hydrocarbon mixture and the catalyst counter- currently to ensure sufficient contact between the hydrocarbons and the catalyst and flowing the hydrocarbon mixture to generate a superficial gas velocity in the fluidized bed reactor in a range of 0.25 to 0.5 m/s for maximizing the contact time between the hydrocarbons and the catalyst, resulting in increased production efficiency for BTX, compared to conventional catalytic cracking processes.
  • a system for producing aromatics via catalytic cracking of a hydrocarbon mixture comprises a fluidized bed reactor, and a catalyst regenerator.
  • a schematic diagram is shown of system 100 that is configured to produce aromatics (e.g., BTX) with improved aromatics production efficiency and yield, compared to conventional steam cracking or conventional catalytic cracking processes.
  • system 100 include reactor 101 comprising housing 102, feed inlet 103, product outlet 104, catalyst inlet 105, and catalyst outlet 106.
  • reactor 101 is configured to catalytically crack a hydrocarbon mixture in the presence of a regenerated catalyst and/or fresh catalyst to produce (1) cracked hydrocarbons including aromatics and (2) a spent catalyst.
  • Reactor 101 may be a fluidized bed reactor.
  • the catalyst in reactor 101 includes H- ZSM-5, silica-alumina, or combinations thereof.
  • the catalyst may have an average particle size in a range of 20 to 195 pm and all ranges and values there between including ranges of 20 to 30 pm, 30 to 40 pm, 40 to 50 pm, 50 to 60 pm, 60 to 70 pm, 70 to 80 pm, 80 to 90 pm, 90 to 100 pm, 100 to 1 10 pm, 110 to 120 pm, 120 to 130 pm, 130 to 140 pm, 140 to 150 pm, 150 to 160 pm, 160 to 170 pm, 170 to 180 pm, 180 to 190 pm, and 190 to 195 pm.
  • the catalyst may include a weight ratio of active metal to support in a range of 0.7 to 0.9 and all ranges and values there between including ranges of 0.70 to 0.75, 0.75 to 0.80, 0.80 to 0.85, and 0.85 to 0.90.
  • the catalyst may have a particle density in a range of 1200 to 1600 kg/m 3 and all ranges and values there between including ranges of 1200 to 1300 kg/m 3 , 1300 to 1400 kg/m 3 , 1400 to 1500 kg/m 3 , and 1500 to 1600 kg/m 3 .
  • housing 102 is adapted to host catalytic cracking of a hydrocarbon mixture.
  • feed inlet 103 may be disposed at a lower half of housing 102 and adapted to receive feed stream 11 therein.
  • feed stream 11 includes a mixture hydrocarbons.
  • the mixture of hydrocarbons may have an initial boiling point of less than 250 °C.
  • the mixture of hydrocarbons may include full range naphtha (boiling point range of 30 to 250 °C), light naphtha (boiling range of 30 to 90 °C), or heavy naphtha (boiling range of 90 to 250 °C).
  • Catalyst inlet 105 in embodiments of the invention, is configured to receive the regenerated catalyst and/or fresh catalyst into housing 102. Catalyst inlet 105 may be disposed at upper half of housing 102. In embodiments of the invention, catalyst outlet 106 is disposed at bottom of housing 102, and configured to release a spent catalyst from housing 102. In embodiments of the invention, reactor 101 comprises one or more internals disposed in housing 102 configured to break up bubble formed in reactor 101 during catalytic cracking processes. The internals may include sieve plates, multi-orifice distributors, perforated plates, or combinations thereof.
  • product outlet 104 is configured to release product stream 12 comprising cracked hydrocarbons and/or unreacted hydrocarbons.
  • catalyst outlet 106 may be in fluid communication with spent catalyst inlet 109 of catalyst regenerator 107 such that the spent catalyst flows from reactor 101 to catalyst regenerator 107.
  • Catalyst regenerator 107 in embodiments of the invention, is configured to regenerate the spent catalyst under regeneration conditions sufficient to produce regenerated catalyst and flue gas.
  • regenerator 107 includes regenerator housing 108, spent catalyst inlet 109, flue gas inlet 110, regenerated catalyst outlet 111, and regenerating gas inlet 112.
  • spent catalyst inlet 109 is disposed at upper half of regenerator housing 108, configured to receive spent catalyst in regenerator housing 108.
  • Flue gas outlet 110 may be disposed on top of regenerator housing 108, configured to release flue gas there from.
  • regenerator gas inlet 112 is disposed at bottom of regenerator housing 108, configured to receive regenerating gas stream 13 into regenerator housing 108.
  • regenerating gas stream 113 includes steam, air, dilute oxygen in nitrogen, or combinations thereof.
  • Regenerated catalyst outlet 111 may be disposed at the bottom of regenerator housing 108, configured to release regenerated catalyst there from.
  • regenerated catalyst outlet 111 is in fluid communication with catalyst inlet 105 of reactor 101 such that regenerated catalyst flows from regenerator 107 to reactor 101.
  • Methods of catalytic cracking of hydrocarbons for producing aromatics have been discovered.
  • the methods can maximize contact between a catalyst and the hydrocarbons so that the ratio of aromatics to light olefins in the product stream is increased compared to conventional catalytic cracking processes.
  • embodiments of the invention include method 200 for producing aromatics.
  • Method 200 may be implemented by system 100, as shown in FIG. 1 and described above.
  • method 200 comprises contacting a mixture of hydrocarbons of feed stream 11 having an initial boiling point of less than 250 °C with the catalyst in the fluidized bed of reactor 101 under reaction conditions effective to produce one or more aromatics.
  • the mixture of hydrocarbons of feed stream 11 comprises heavy naphtha, light naphtha, or full range naphtha.
  • the one or more aromatics can include benzene, toluene, xylene, or combinations thereof.
  • the contacting step further produces one or more olefins including ethylene, propylene, 1 -butene, 2-butene, isobutene, or combinations.
  • contacting step at block 201 further produces spent catalyst comprising coke disposed on the catalyst.
  • the contacting at block 201 can be conducted by flowing feed stream 11 and the catalyst counter- currently to maximize contact time between the catalyst and the hydrocarbons in feed stream 11.
  • the mixture of hydrocarbons of feed stream 11 is flowed into reactor 101 through a sparger feed distributor.
  • the catalyst may be flowed into reactor 101 through a catalyst distributor.
  • the reaction conditions at block 201 include an average solids volume fraction in the fluidized bed in a range of 0.35 to 0.45 and all ranges and values there between including ranges of 0.35 to 0.36, 0.36 to 0.37, 0.37 to 0.38, 0.38 to 0.39, 0.39 to 0.40, 0.40 to 0.41, 0.41 to 0.42, 0.42 to 0.43, 0.43 to 0.44, and 0.44 to 0.45.
  • the fluidized bed includes a dense phase fluidized bed having a bed bulk density of 80 to 240 kg/m 3 and all ranges and values there between including ranges of 80 to 90 kg/m 3 , 90 to 100 kg/m 3 , 100 to 110 kg/m 3 , 110 to 120 kg/m 3 , 120 to 130 kg/m 3 , 130 to 140 kg/m 3 , 140 to 150 kg/m 3 , 150 to 160 kg/m 3 , 160 to 170 kg/m 3 , 170 to 180 kg/m 3 , 180 to 190 kg/m 3 , 190 to 200 kg/m 3 , 200 to 210 kg/m 3 , 210 to 220 kg/m 3 , 220 to 230 kg/m 3 , and 230 to 240 kg/m 3 .
  • the reaction conditions at block 201 further include a superficial gas velocity of 0.25 to 0.50 m/s and all ranges and values there between including ranges of 0.25 to 0.26 m/s, 0.26 to 0.28 m/s, 0.28 to 0.30 m/s, 0.30 to 0.32 m/s, 0.32 to 0.34 m/s, 0.34 to 0.36 m/s, 0.36 to 0.38 m/s, 0.38 to 0.40 m/s, 0.40 to 0.42 m/s, 0.42 to 0.44 m/s, 0.44 to 0.46 m/s, 0.46 to 0.48 m/s, and 0.48 to 0.50 m/s.
  • the reaction conditions at block 201 include an reaction temperature of 630 to 700 °C and all ranges and values there between including ranges of 630 to 640 °C, 640 to 650 °C, 650 to 660 °C, 660 to 670 °C, 670 to 680 °C, 680 to 690 °C, and 690 to 700 °C.
  • the reaction conditions at block 201 may further include a reaction pressure of 1 to 2 bar and all ranges and values there between including ranges of 1 to 1.1 bar, 1.1 to 1.2 bar, 1.2 to 1.3 bar, 1.3 to 1.4 bar, 1.4 to 1.5 bar, 1.5 to 1.6 bar, 1.6 to 1.7 bar, 1.7 to 1.8 bar, 1.8 to 1.9 bar, and 1.9 to 2 bar.
  • the reaction conditions at block 201 may further include a weight hourly space velocity of 1.7 to 2.1 hr 1 and all ranges and values there between including ranges of 1.7 to 1.8 hr 1 , 1.8 to 1.9 hr 1 , 1.9 to 2.0 hr 1 , and 2.0 to 2.1 hr 1 .
  • residence time distribution (RTD) in reactor 101 can be characterized that 75 to 95 % catalyst has a residence time within about 3600 seconds.
  • the benzene, toluene, and/or xylene are produced at a combined yield of 25 to 36% and all ranges and values there between including ranges of 25 to 26%, 26 to 27%, 27 to 28%, 28 to 29%, 29 to 30%, 30 to 31%, 31 to 32%, 32 to 33%, 33 to 34%, 34 to 35%, and 35 to 36%.
  • method 200 comprises, after the contacting step, regenerating the spent catalyst produced in the contacting step in catalyst regenerator 107 to produce a regenerated catalyst.
  • regenerating may be performed at a regeneration temperature in a range of 720 to 750 °C and all ranges and values there between including ranges of 720 to 725 °C, 725 to 730 °C, 730 to 735 °C, 735 to 740 °C, 740 to 745 °C, and 745 to 750 °C.
  • regenerating comprise flowing regenerating gas stream 13 through spent catalyst in catalyst regenerator 107 at a weight hourly space velocity of 10 to 40 hr 1 and all ranges and values there between including ranges of 10 to 15 hr 1 , 15 to 20 hr 1 , 20 to 25 hr 1 , 25 to 30 hr 1 , 30 to 35 hr 1 , and 35 to 40 hr 1 .
  • method 200 comprises flowing the regenerated catalyst into the fluidized bed in reactor 101 through catalyst inlet 105.
  • 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 naphtha feed was catalytically cracked in a dense phase fluidized bed reactor.
  • the naphtha feed included 23.15 wt.% normal paraffin, 28.07 wt.% iso-paraffin, 33.83 wt.% naphthenic species, 11.7 wt.% aromatics, 0.28 wt.% olefins, and 2.96 wt.% other heavier oligomeric hydrocarbon species.
  • the reaction conditions for the catalytic cracking included a reaction temperature of 680 °C, a regenerating temperature of 700 °C, and weight hourly space velocity of 1.9 hr 1 .
  • the dense phase fluidized bed reactor had a catalyst load of 1500 g.
  • the product yields (calculated based on mass; wt.%) at on-stream time of 0.5 hour, 1 hour, 2 hours, and 3 hours are shown in Table 1.
  • Embodiment l is a method of producing aromatics.
  • the method includes contacting a mixture of hydrocarbons having an initial boiling point of less than 250 °C with catalyst in a fluidized bed under reaction conditions effective to produce one or more aromatics, wherein the reaction conditions include the fluidized bed having an average solids volume fraction in a range of 0.35 to 0.45.
  • Embodiment 2 is the method of embodiment 1, wherein the fluidized bed is a dense phase fluidized bed with a bulk density of 80 to 240 kg/m 3 .
  • Embodiment 3 is the method of either of embodiments 1 or 2, wherein the reaction conditions further include a superficial gas velocity of 0.25 to 0.5 m/s.
  • Embodiment 4 is the method of any of embodiments 1 to 3, wherein the mixture of hydrocarbons include full range naphtha, light naphtha, or heavy naphtha.
  • Embodiment 5 is the method of any of embodiments 1 to 4, wherein the mixture of hydrocarbons is flowed in a direction counter current to flow of the catalyst in the fluidized bed.
  • Embodiment 6 is the method of any of embodiments 1 to 5, wherein the mixture of hydrocarbons is flowed through a sparger feed distributor into a reactor containing the fluidized bed.
  • Embodiment 7 is the method of embodiment 6, wherein the reactor includes internals including sieve plates, multi-orifice distributors, perforated plates, or combinations thereof.
  • Embodiment 8 is the method of any of embodiments 1 to 7, wherein the catalyst contains El- to ZSM-5, silica-alumina, or combinations thereof.
  • Embodiment 9 is the method of any of embodiments 1 to 8, wherein the reaction conditions further include a reaction temperature of 630 to 700 °C and a reaction pressure of 1 to 2 bar.
  • Embodiment 10 is the method of any of embodiments 1 to 9, wherein the reaction conditions further include a weight hourly space velocity in a range of 1.7 to 2.1 hr 1 .
  • Embodiment 11 is the method of any of embodiments 1 to 10, wherein the reaction conditions further include residence time distribution of 70 to 90 % within 60 minutes.
  • Embodiment 12 is the method of any of embodiments 1 to 11, wherein the method further produces one or more olefins including ethylene, propylene, 1 -butene, 2-butene, isobutene, or combinations thereof.
  • Embodiment 13 is the method of any of embodiments 1 to 12, wherein the aromatics contain benzene, toluene, xylene, or combinations thereof.
  • Embodiment 14 is the method of embodiment 13, wherein the benzene, toluene, and/or xylene are produced at a combined yield of 25 to 36%.
  • Embodiment 15 is the method of any of embodiments 1 to 14, further including, after the contacting step, regenerating the catalyst in a catalyst regenerator to produce a regenerated catalyst, and flowing the regenerated catalyst into the fluidized bed.

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  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

L'invention concerne des systèmes et des procédés de production de composés aromatiques. L'invention concerne également un mélange d'hydrocarbures ayant un point d'ébullition initial inférieur à 250 °C avec un catalyseur dans un lit fluidisé dans des conditions de réaction efficaces pour produire un ou plusieurs composés aromatiques. Les conditions de réaction comprennent une fraction volumique de solides moyenne du lit fluidisé dans une plage de 0,35 à 0,45.
EP20751300.3A 2019-07-31 2020-07-29 Réacteur à lit fluidisé à phase dense pour maximiser le rendement de production de btx Pending EP4004151A1 (fr)

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US201962881238P 2019-07-31 2019-07-31
PCT/IB2020/057163 WO2021019465A1 (fr) 2019-07-31 2020-07-29 Réacteur à lit fluidisé à phase dense pour maximiser le rendement de production de btx

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CN111718085A (zh) * 2020-06-11 2020-09-29 中石大蓝天(青岛)石油技术有限公司 一种固体废物的处理方法
WO2023101944A1 (fr) * 2021-11-30 2023-06-08 Saudi Arabian Oil Company Procédés de traitement de flux d'alimentation en hydrocarbures

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US5489732A (en) * 1994-10-14 1996-02-06 Uop Fluidized solid bed motor fuel alkylation process
US7179427B2 (en) * 2002-11-25 2007-02-20 Abb Lummus Global Inc. Apparatus for countercurrent contacting of gas and solids
KR100651418B1 (ko) * 2006-03-17 2006-11-30 에스케이 주식회사 고속유동층을 이용하여 탄화수소 원료로부터 경질 올레핀을제조하는 접촉분해 공정
CN100551883C (zh) * 2006-12-01 2009-10-21 中国化学工程股份有限公司 流化床催化裂解生产丙烯的方法及反应器
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CN102286294B (zh) * 2010-06-18 2014-05-28 中国石油化工股份有限公司 一种生产丙烯和轻芳烃的烃类催化转化方法
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CN114364454B (zh) 2023-11-07
WO2021019465A1 (fr) 2021-02-04
CN114364454A (zh) 2022-04-15
WO2021019465A8 (fr) 2021-09-23

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