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    Home > Chemicals Industry > Chemical Technology > Issue 46/2012 - Progress of propane dehydrogenation technology and analysis of project economy

    Issue 46/2012 - Progress of propane dehydrogenation technology and analysis of project economy

    • Last Update: 2022-11-12
    • Source: Internet
    • Author: User
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    Progress of propane dehydrogenation technology and project economic analysis

    Industrial applications are maturing

    Propylene is second only to ethylene important petrochemical basic raw materials, in addition to the synthesis of polypropylene (PP), propylene can also be made into acrylonitrile, isopropanol, phenol and acetone, acrylic acid and its esters and many other downstream products, is gradually replacing traditional materials such as steel, wood, cotton and cotton products, in the long run, domestic and foreign market demand is still strong, with propane dehydrogenation technology tends to mature, especially in recent years, with the development of the world's unconventional natural resources have made breakthroughs, obtaining long-term, stable, relatively low propane resources may become possible Propane dehydrogenation to propylene project has a strong competitiveness, triggering giants to invest, become a hot spot for the development of the industry, propane dehydrogenation to propylene technology has a history of more than 20 years, after continuous improvement, industrial application is becoming more and more mature, has been industrialized,
    and has become the third largest propylene production route
    。 The main processes include UOP's Oleflex process continuous moving bed process technology, Lummus-Houdry's Catofin process cycle multi-reactor process technology, Wood's Krupp Uhdewcng company's STAR process and Snamprogetti's PDH process
    jointly developed with Linde-BASF-Statoil 。 At present, the industrialized production process of propane dehydrogenation to propylene is the Oleflex process of UOP and the Catofin process
    of ABB Lummus Global of the United States.
    The two propane dehydrogenation to propylene production processes are basically the same, but only the dehydrogenation and catalyst regeneration parts
    .

    There are 14 sets of propylene dehydrogenation to propylene industrial plants in the world, of which 10 sets use UOP's Oleflex process and 4 sets are ABB Lummus' Catofin process
    .
    There are more than 20 sets of plants in production or under construction worldwide, and the production capacity will reach more than 6.
    7 million tons
    after completion.

    ●UOP's Oleflex process Oleflex process
    was developed by UOP in the 80s of the last century, first industrialized in Thailand in 1990, and in April 1997, the combined plant of 250,000 tons of propylene was put into production in South Korea using the second-generation Oleflex technology
    .
    At present, the total production capacity of Oleflex propane dehydrogenation to propylene in the world is 2.
    5 million tons
    .
    The process flow diagram of the Oleflex combined unit is shown in Figure 1
    .

    ●Lummus Catofin process
    Catofin process is the C3~C5 alkane dehydrogenation production monoolefin technology
    developed by ABB Lummus.
    Currently, 10 companies around the world use the Catofin process to produce olefins, producing more than 3.
    2 million tonnes
    .
    ABB Lummus' Catofin process flow is shown in Figure 2
    .

    ●Propane dehydrogenation process technology comparison ABB-Lummus Catofin and UOP's Oleflex propane dehydrogenation process and several other processes technology comparison
    is shown in Table 1
    .









    Table 1 Comparison of various propane dehydrogenation process technologies

    ABB-Lummus UOP Uhde Snamprogetti Linde
    Catofin Oleflex STAR FBD AG
    reactor Fixed bed Move the bed Multi-tube fixed bed Fluidized bed Multi-tube fixed bed
    Reactor structure Adiabatic Adiabatic Adiabatic Adiabatic Adiabatic
    Total reactor/pcs 5 3~4
    Material reactors/pcs 2 3~4
    Reaction temperature/°C 650 525 500~640 550~600 590
    Reaction pressure/MPa 0.
    05
    3.
    04
    0.
    1~0.
    2
    0.
    3
    ≥0.
    1
    Selectivity/% 87 84 85~93 89 /
    Conversion rate/% 90 (full) 44 (single) 35~40(Single) 30~40(Single) 40 (one way) 32~50(Single)93(Full)
    Single consumption 1.
    18
    1.
    22
    1.
    25
    / /
    catalyst Cr2O3/Al2O3 Pt ̄Sn/ Al2O3 Precious metals/Zn ̄Al2O3 Cr2O3/Al2O3 Pt/Ca ̄Zn ̄Al2O3
    Catalyst life/year 2 4~5
    Regeneration method Switch, air burns Continuous shifting switching, air combustion, Continuous removal out of the regeneration stream switching, air combustion,
    15~30min Out of regeneration Reaction 7h, regeneration 1h Bed, air burns Reaction 6h, regeneration 3h
    dilute Undiluted H2 dilution H2O dilution Undiluted Undiluted
    Production equipment/set 4 11 1 (under construction)
    ABB-LummusUOPUhdeSnamprogettiLindeCatofinOleflexSTARFBD AG reactor fixed bed mobile bed multi-tube fixed bed fluidized bed multi-tube fixed bed reactor structure thermal insulation Thermal adiabatic total reactor/5 3~4 material reactors/2 3~4 reaction temperature/°C 650 525 500~640 550~600590 Reaction pressure/MPa0.
    05 3.
    040.
    1~0.
    20.
    3≥0.
    1 selectivity/%8784 85~9389/conversion rate/%90(full)44(single)35~40(single)30~40(single)40(one-way)32~50(single)93( Full) single consumption 1.
    18 1.
    22 1.
    25//catalyst Cr2O3/Al2O3 Pt ̄Sn/ Al2O3 Precious metal/Zn ̄Al2O3 Cr2O3/Al2O3 Pt/Ca ̄Zn ̄Al2O3 catalyst life/year 24~5 Regeneration mode switching, air combustion continuous shift switching, air combustion, continuous moving out regeneration flow switching, air combustion, 15~30min out regeneration Reaction 7h, regeneration 1h bed, air combustion reaction 6h, regeneration 3h dilution undiluted H2 dilution H2O dilution undiluted undiluted Production plant/set 4111 (under construction) ABB-LummusUOP UhdeSnamprogettiLindeABB-LummusABB-LummusUOP UOPUhdeUhdeSnamprogettiSnamprogettiLindeLinde CatofinOleflexSTARFBDAGCatofinCatofin Oleflex OleflexSTARFBDFBD AGAG reactor Fixed bed mobile bed multi-tube fixed bed fluidized bed multi-tube fixed bed reactor fixed bed Fixed bedMobile bedMobile bedMultitube fixed bedMultitube fixed bedMultitube fixed bedFluidized bedMultitube fixed bedMultitube fixed bedMultitube fixed bed Reactor structureThermal insulationThermal insulationReactor structureReactor structureReactor structureInsulation Thermal insulationThermal insulationThermal insulationThermal insulation Total reactor/5 3~4 total reactor/total reactor/5 5 3~4 3~4 material reactor/2 3~4 material reactor/material reactor/2 2 3~4 3~4 Reaction temperature/°C 650 525 500~640 550~600590 Reaction temperature/°CReaction temperature/°C 650 650525525 500~640500~640 550~600 550~600 590 590 590reaction pressure/MPa 0.
    05 3.
    04 0.
    1~0.
    20.
    3 ≥0.
    1 reaction pressure/MPa reaction pressure/MPa 0.
    05 0.
    05 3.
    04 3.
    04 0.
    1~0.
    2 0.
    1~0.
    20.
    3 0.
    3≥0.
    1≥0.
    1 selective/%8784 85~93 89/selectivity/%selectivity/%87 87 848485~93 85~93 89 89//conversion rate/%90 (full) 44 (single) 35~40 (single).
    30~40 (single) 40 (one way) 32~50 (single) 93 (full) conversion rate/% conversion rate/%90 (full) 44 (single) 90 (full) 44 (single).
    35~40(single)35~40(single)30~40(single)30~40(single)40(one-way)40(one-way)32~50(single)93(full).
    32~50 (single) 93 (full) single consumption 1.
    18 1.
    22 1.
    25 // single consumption single consumption 1.
    181.
    181.
    221.
    221.
    251.
    25/// /Catalyst Cr2O3/Al2O3 Pt ̄Sn/ Al2O3 precious metal/Zn ̄Al2O3 Cr2O3/Al2O3Pt/ Ca ̄Zn ̄Al2O3 catalyst catalyst Cr2O3/Al2O3 Cr2O3/Al2O3 Pt ̄Sn/ Al2O3 Pt ̄Sn/ Al2O3 Precious metals/Zn ̄Al2O3 precious metals/Zn ̄Al2O3 Cr2O3/Al2O3 Cr2O3/Al2O3 Pt/Ca ̄Zn ̄Al2O3 Pt/Ca ̄Zn ̄Zn ̄Al2O3 Catalyst life/year24~5Catalyst life/yearCatalyst life/year2 2 4~5 4~5 regeneration mode switching, Air combustion continuous shift switching, air combustion, continuous removal regeneration flow switching, air combustion, regeneration mode regeneration mode switching, air combustion Switching, air combustion continuous shift continuous shift switching, air combustion, switching, air combustion, continuous moving out of the regeneration stream continuous moving out of the regeneration flow switching, air combustion, Switching, air combustion, 15~30min out of regeneration reaction 7h, regeneration 1h bed, air combustion reaction 6h, regeneration 3h 15~30min15~30min regeneration reaction 7h, regeneration 1h reaction 7h, regeneration 1h bed, air combustion Bed, air combustion reaction 6h, regeneration 3h reaction 6h, regeneration 3h Diluted Undiluted H2DilutionH2O Diluted Undiluted Diluted Diluted Undiluted Undiluted H2Diluted H2DiluteH2O Diluted H2O Diluted Undiluted Undiluted Undiluted Undiluted Production plant/set4 111 (under construction)Production plant/setProduction plant/set4 4 11 111 (under construction) 1 (under construction).

    The cost advantage is outstanding

    Propane accounts for about 2/3 of the total cost of propane dehydrogenation to propylene, so future propane dehydrogenation projects will be mainly concentrated in the Middle East, especially Saudi Arabia
    .

    According to statistics, in 2004~2009, the average monthly price difference of propylene and propane imports in China was 476 US dollars / ton (see Table 2), the project has a good return on investment, and it is preliminarily calculated to build a propane dehydrogenation device in East China, when the price of propane raw materials is 729 US dollars / ton (the average price of imports in January ~ April 2010), the preliminary calculation of the cost price of propylene including tax is 9381 yuan / ton (in addition to the main raw materials, other manufacturing costs and period costs 1283 yuan / ton) Compared with the imported propylene of 10249 yuan / ton in the same period of the market, it is about
    868 yuan / ton.

    At present, there are many sets of propane dehydrogenation units that have been built, are under construction or are preparing to be built in the region, and the amount of propane exported by the region will inevitably decrease year by year in the future, which will inevitably lead to an increase
    in the operating costs of propane dehydrogenation units that rely on raw material imports.

    In the long run, the demand for propylene market at home and abroad is still strong, with the maturity of propane dehydrogenation technology, especially in recent years, it is possible to obtain long-term, stable and relatively low propane resources, so that propane dehydrogenation to propylene project has strong competitiveness, triggering industry giants to invest, becoming a hot spot for industry development, it is worth noting that the project should pay attention to the production and technology of propane dehydrogenation to propylene, pay attention to the economics of propane dehydrogenation technology projects, in order to




    Table 2 Prices and spreads between imported propylene and propane in 2004~2009 USD/ton

    Year Propylene Price Propane Price Propane Price Propylene Propane Price Difference

    2004 804 376 428
    2005 995 458 537
    2006 1108 549 559
    2007 1121 619 502
    2008 1234 782 452
    2009 882 500 382
    average 1023 547 476
    2004804376428200599545853720061108549 55920071121619502200812347824522009 882500382 Average 1023547 476 2004 804376428 200420048048043763764284282005995 45853720052005995995458458537537 200611085495592006200611081108549549 559559200711216195022007200711211121 6196195025022008123478245220082008 123412347827824524522009882500382 2009 2009 882 882 500 500382382 Average 1023 547476 average average 1023 1023 547 547476 476
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