WO2010024792A1 - Reformeur pour transformer une biomasse en gaz de synthèse - Google Patents

Reformeur pour transformer une biomasse en gaz de synthèse Download PDF

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Publication number
WO2010024792A1
WO2010024792A1 PCT/US2007/025147 US2007025147W WO2010024792A1 WO 2010024792 A1 WO2010024792 A1 WO 2010024792A1 US 2007025147 W US2007025147 W US 2007025147W WO 2010024792 A1 WO2010024792 A1 WO 2010024792A1
Authority
WO
WIPO (PCT)
Prior art keywords
reformer
biomass
section
tubular reactor
synthesis gas
Prior art date
Application number
PCT/US2007/025147
Other languages
English (en)
Inventor
William L. Manning
Michael J. Goff
Original Assignee
Black & Veatch Corporation
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 Black & Veatch Corporation filed Critical Black & Veatch Corporation
Priority to PCT/US2007/025147 priority Critical patent/WO2010024792A1/fr
Publication of WO2010024792A1 publication Critical patent/WO2010024792A1/fr

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/48—Apparatus; Plants
    • C10J3/485—Entrained flow gasifiers
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/002—Removal of contaminants
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/002—Removal of contaminants
    • C10K1/003—Removal of contaminants of acid contaminants, e.g. acid gas removal
    • C10K1/004—Sulfur containing contaminants, e.g. hydrogen sulfide
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0913—Carbonaceous raw material
    • C10J2300/0916—Biomass
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0953—Gasifying agents
    • C10J2300/0973—Water
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/12—Heating the gasifier
    • C10J2300/1215—Heating the gasifier using synthesis gas as fuel
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/12—Heating the gasifier
    • C10J2300/1246—Heating the gasifier by external or indirect heating
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C10J2300/164—Integration of gasification processes with another plant or parts within the plant with conversion of synthesis gas
    • C10J2300/1656—Conversion of synthesis gas to chemicals
    • C10J2300/1659—Conversion of synthesis gas to chemicals to liquid hydrocarbons
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/1853—Steam reforming, i.e. injection of steam only
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/141—Feedstock
    • Y02P20/145—Feedstock the feedstock being materials of biological origin

Definitions

  • the present invention relates to a tubular reformer wherein biomass is treated in the presence of steam in the tubular reformer at elevated temperatures to convert the biomass and steam into synthesis gas comprising primarily carbon monoxide, hydrogen, and carbon dioxide.
  • WO2005/021474A1 discloses a process, including a biomass feed- treating process, a reformer process for converting biomass to synthesis gas, and a process for converting a synthesis gas into ethanol. A similar process is disclosed in
  • a reformer for converting biomass into synthesis gas comprising primarily of carbon monoxide, hydrogen, and carbon dioxide by reaction with steam.
  • the reformer consists of a cylindrical vessel with an outer wall having an inside and an outside, a bottom and a top, a biomass inlet, and a synthesis gas outlet.
  • tubular reactor in the cylindrical vessel, the tubular reactor being in fluid communication with the biomass inlet and the synthesis gas outlet; a radiant section extending upward from the bottom of the cylindrical vessel; a burner centrally positioned in the bottom of the cylindrical vessel; at least one outer section having an inside, a top, and a bottom and positioned on the cylindrical vessel outer wall over an opening in the cylindrical vessel outer wall along at least a portion of the axial length of the tubular reactor, along a central axis of the cylindrical vessel; and at least one burner positioned in the bottom of at least one outer section.
  • FIG 1 is a schematic view of the reactor of the present invention
  • FIG 2 is a top view of the reactor taken at lines AA on FIG 1 ; and;
  • FIG 3 is a schematic diagram of a system for the production of a suitable biomass feed for the reactor of the present invention.
  • biomass reformer 10 is shown and consists of a cylinder 12, including a stack 16 and a transition section 14 for the discharge of combustion gases from the reformer; it also includes a tapered section 15, stack 16, and dimension lines defining a height 14 of the transition and stack section, as shown. The height of this section can vary widely.
  • stack 16 also includes a flow controller, shown as a damper 17. This flow controller provides a desired back pressure in the reactor and regulates the amount of combustion gas discharged from the reactor.
  • Convection section 20 having a height 20' is shown above a radiant section
  • a tubular reactor consisting of multiple tube coils 50 is shown.
  • the tubular reactor can be fabricated of any suitable material and is used to receive a feed of biomass entrained in a stream of steam via a line 44.
  • the mixture of biomass and steam is passed rapidly through the tubular reactor and is discharged at a synthesis gas outlet 52.
  • This gas stream is subsequently passed to cooling, scrubbing, or solids separation units (as required) to remove the nonreactive materials of the biomass from the synthesis gas.
  • the hydrogen to carbon monoxide ratio of the synthesis gas may be adjusted by the use of, for example, the water gas shift reaction.
  • the technology for performing this change is well known, as is the technology for converting synthesis gas into a wide range of products utilizing, for example, the Fischer-Tropsch process.
  • the tubes in the radiant portion of the biomass reformer should be fabricated of materials that can withstand temperatures in excess of about 1900 0 F and may include materials such as B407UNSN8810 alloy steel or equivalent.
  • the tubes in the convection section of the reformer should be fabricated of carbon steel and high temperature alloy steel such as A312TP310 alloy or equivalent. A variety of alloy steels are available for use in the hottest portions of the reformer.
  • the tubular reactor may also consist of multiple tube coils 50, which may have numerous inlets and outlets. Such variations are well known in the industry and do not require further elaboration.
  • the tubes may be arranged in other configurations that are effective for heating by a central burner 22, as shown.
  • the bottom 27 of the outer sections is at essentially at the same level as the bottom of radiant section 18.
  • Burner 24 is basically at the same level as burner 22, so that the gases produced from the burners effectively contact the tubular reactor along the entire length of opening 54 to increase the heat provided to the tubular reactor.
  • FIG 2 is a top view of the reactor shown in FIG 1 taken at line A-A.
  • FIG 2 shows the inner diameter of the coil, the outer sections and the inner diameter of the reactor cylinder. The outer sections are shown with insulation 28.
  • the feed stream may be introduced through a line 44a into a feed preheat coiled tube reactor 46 in convection section 20, so that the biomass feed and steam stream are passed through preheating coil section 46 to preheat the biomass/steam mixture in the convection section, with the combined streams being passed via a line 48 from the convection section into the radiant section for reaction.
  • steam production coil 40 with water inlet 30 for the production of steam through line 32 and a steam coil 42 for introducing steam through line 36 for the production of superheated steam through line 34, is included in the convection section.
  • the convection section includes steam generator coil 40 to reduce the temperature of the flue gases passed to stack 16.
  • the super-heating of steam and the preheating of the biomass/steam is adjusted as required to produce the desired inlet temperature for the biomass/steam stream passed into the radiant section. This temperature ranges from about 950 0 F to about 1250 0 F.
  • the amount of steam produced is sufficient to cool the combustion gases that pass into transition section 15 to a temperature below about 600 0 F and preferably below about 550 0 F.
  • the residence time of the biomass/steam - synthesis gas mixture in the tubular reactor, i.e., coils 50 can vary significantly and is typically from about 0.6 second to 2 seconds, with the outlet temperature from the reactor being from about 1500 0 F to 1800 0 F. Variations of temperature and time in the reactor can result in the production of synthesis gas having different hydrogen/carbon monoxide ratios.
  • the amount of preheating of the feed stream achieved in convection section 20 can vary widely. The amount of water in the biomass, for instance, may be insignificant if the biomass has been adequately dried previously and is charged with superheated steam that will continue to reduce the amount of water in the biomass stream. Typically, the water concentration of the biomass stream is reduced to a level of about 20 weight percent or less and, preferably, to a level of about 15 weight percent or less, prior to charging to the convection section.
  • the biomass may simply be passed into a stream of flowing superheated steam for transportation to and through the tubular reactor.
  • No reactor is shown in detail in WO/2005/021474, and certainly no reactor with the efficiency and longevity provided by the structure of the reformer described herein.
  • biomass feed is introduced into a hopper 102 (as shown by arrow 100), passed downward through hopper 102 to a grinder 104, which grinds the biomass feed to a fine consistency and drops it onto a screen 106.
  • Biomass from grinder 104 that is not sufficiently fine is recycled by a line 110 back to hopper 102.
  • the finely divided particles from screen 106 are routed through line 108 and passed to dryer 112, with exhaust gases being filtered and vented through line 114.
  • the dried biomass material is then passed via a line 116 and a lock valve 118 to storage in a hopper 120, from which it is passed via a second lock valve and a metering system 122 through a line 124 to be combined with a superheated steam by entraining it in a steam stream supplied through a line 126.
  • the resulting mixture passes through line 130 to the reformer of the present invention through feed inlet 44.
  • the fuel for burners 22 and 24 is supplied as shown via a line 138 and may comprise a fuel gas, synthesis gas, or any combustible gas or liquid fuel stream. [0022]
  • the resulting synthesis gas is routed via line 52 to treatment in a facility
  • the present invention consists of a reactor that is particularly effective and efficient in supplying heat to the radiant section and to the convection section of a tubular reactor.
  • the reformer of the present invention receives a feedstock at temperatures from about 250 0 F to about 450 0 F at inlet 44a.
  • the temperature of the synthesis gas leaving the reactor is typically between about 1500 0 F and 1800 0 F.
  • a preferable temperature is about 1650 0 F up to about 1750 0 F.
  • the pressure in reformer 10 can vary widely, as long as the pressure in the tubular reformer is sufficient to move the biomass through the tubular reformer at the desired rate.
  • the temperature and pressure conditions, as well as the steam to biomass ratios will vary dependent on the particular feedstock available to obtain the desired hydrogen to carbon monoxide ratio. Individuals familiar with these processes can readily determine the operating conditions for a particular feed stream. Contact times in the tubular reactor vary from about 0.4 second to
  • the amount of superheated steam used is a function of the nature of the feedstock. Skilled technicians can readily determine the hydrogen and carbon content of the feedstock, as well as the amount of water contained in the feedstock, for the purposes of determining the proper ratio of superheated steam to be combined with the biomass feedstock. As indicated previously, the product synthesis gas stream can be treated for the removal of undesirable materials such as oils, solids, or acidic components.
  • the reformer sections i.e., radiant section 18, convection section 20, and stack and transition section 14, are shown as separate sections connected at 62 and 64. The reformer could also be fabricated as a single unit or in sections to be assembled to produce the reformer.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Hydrogen, Water And Hydrids (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

L'invention concerne un reformeur tubulaire dans lequel une biomasse est traitée en présence de vapeur dans un réacteur tubulaire à températures élevées pour transformer cette biomasse et cette vapeur en gaz de synthèse, comprenant principalement du monoxyde de carbone, de l'hydrogène et du dioxyde de carbone.
PCT/US2007/025147 2008-08-18 2008-08-18 Reformeur pour transformer une biomasse en gaz de synthèse WO2010024792A1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
PCT/US2007/025147 WO2010024792A1 (fr) 2008-08-18 2008-08-18 Reformeur pour transformer une biomasse en gaz de synthèse

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
PCT/US2007/025147 WO2010024792A1 (fr) 2008-08-18 2008-08-18 Reformeur pour transformer une biomasse en gaz de synthèse

Publications (1)

Publication Number Publication Date
WO2010024792A1 true WO2010024792A1 (fr) 2010-03-04

Family

ID=41721750

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/US2007/025147 WO2010024792A1 (fr) 2008-08-18 2008-08-18 Reformeur pour transformer une biomasse en gaz de synthèse

Country Status (1)

Country Link
WO (1) WO2010024792A1 (fr)

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3129065A (en) * 1960-09-14 1964-04-14 Chemical Construction Corp Upright fluid heating furnace with integral heat recovery means
US3512506A (en) * 1968-04-22 1970-05-19 Peter Von Wiesenthal Compact multipath process heater
US6685893B2 (en) * 2001-04-24 2004-02-03 Abb Lummus Global Inc. Pyrolysis heater
US6767375B1 (en) * 1999-08-25 2004-07-27 Larry E. Pearson Biomass reactor for producing gas
US20060045828A1 (en) * 2004-09-01 2006-03-02 Aaron Timothy M Catalytic reactor

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3129065A (en) * 1960-09-14 1964-04-14 Chemical Construction Corp Upright fluid heating furnace with integral heat recovery means
US3512506A (en) * 1968-04-22 1970-05-19 Peter Von Wiesenthal Compact multipath process heater
US6767375B1 (en) * 1999-08-25 2004-07-27 Larry E. Pearson Biomass reactor for producing gas
US6685893B2 (en) * 2001-04-24 2004-02-03 Abb Lummus Global Inc. Pyrolysis heater
US20060045828A1 (en) * 2004-09-01 2006-03-02 Aaron Timothy M Catalytic reactor

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