WO2012008947A1 - Lits fluidisés comprenant des parois membranaires et procédés de fluidisation - Google Patents

Lits fluidisés comprenant des parois membranaires et procédés de fluidisation Download PDF

Info

Publication number
WO2012008947A1
WO2012008947A1 PCT/US2010/041758 US2010041758W WO2012008947A1 WO 2012008947 A1 WO2012008947 A1 WO 2012008947A1 US 2010041758 W US2010041758 W US 2010041758W WO 2012008947 A1 WO2012008947 A1 WO 2012008947A1
Authority
WO
WIPO (PCT)
Prior art keywords
para
fluidizing
fluidized bed
particles
gas
Prior art date
Application number
PCT/US2010/041758
Other languages
English (en)
Inventor
Timohthy E. Vail
Original Assignee
Synthesis Energy Systems, Inc.
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 Synthesis Energy Systems, Inc. filed Critical Synthesis Energy Systems, Inc.
Priority to PCT/US2010/041758 priority Critical patent/WO2012008947A1/fr
Publication of WO2012008947A1 publication Critical patent/WO2012008947A1/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
    • C10J3/482—Gasifiers with stationary fluidised bed
    • 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
    • C10J3/52—Ash-removing devices
    • C10J3/523—Ash-removing devices for gasifiers with stationary fluidised bed
    • 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
    • C10J2300/093—Coal
    • 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
    • C10J2300/0956—Air or oxygen enriched air
    • 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
    • C10J2300/0976—Water as steam
    • 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

Definitions

  • the present invention relates to fluidized beds, and methods of fluidizing.
  • the present invention relates to fluidized bed reactors and to methods of gasification.
  • the present invention relates to fluidized bed reactors having membrane walls, and to methods of gasification.
  • the present invention relates to fluidized bed coal gasification and to methods of coal gasification.
  • Fluidization is commonly defined as an operation by which particulate fine solids are transformed into a fluid-like state through contact with a gas or liquid. Fluidized beds are known for their high heat and mass transfer coefficients, due to the high surface area-to-volume ratio of fine particles. Fluidized beds are used in a wide variety of industrial processes such reaction, drying, mixing, granulation, coating, heating and cooling.
  • a fluidized bed consists of a vertically- oriented column filled with granular material, and a fluid (gas or liquid) is pumped upward through a distributor at the bottom of the bed. When the drag force of flowing fluid exceeds gravity, particles are lifted and fluidization occurs.
  • a vessel is provided for a fluidized bed.
  • a gas distribution grid is usually positioned in the vessel and defines the bottom surface of the fluidized bed.
  • the central portion of the grid may be conical or cylindrical in shape and comprises a passage.
  • a constriction is provided at the bottom of the passage having a fixed opening defining a venturi of fixed throat size to provide a uniform upward gas velocity into the vessel and thus into the fluidized bed. Directing a stream of high velocity gas through the venturi or passage into the reaction vessel causes ash particles in the vessel to agglomerate and eventually discharge through the passage and venturi throat.
  • a venturi is utilized to serve as a passage for withdrawing the agglomerated solids from the fluidized bed.
  • Spiral or other descending ridges are positioned on the interior surface of the constricted cylindrical opening of the venturi to permit variable and increased rates of agglomerate discharge with improved separation and classification of the solid materials.
  • gas recirculation means is used to supplement combustion air flow to maintain gas velocity in the circulation loop sufficient to entrain and sustain particle mass flow rate at a level required to limit furnace gas temperature to a predetermined value as 1 550 F. and wherein gas recirculation mass flow apportions heat transfer from the gas and recirculated particles among the respective portions of the steam generator fluid heat absorption circuits, gas and circulating particle mass flow rates being
  • Means are provided for collecting hig h temperature bed solid particles downstream of the furnace.
  • the dense pack heat exchanger directs the hot collected particles down over heat transfer surface, such surface being a portion of the steam generator flu id circuits. Flow is induced by gravity means. The dense compaction of the solid particles around the fluid heat exchange circuits results in hig h heat transfer rates as the flu id cools the compacted solid material.
  • the heat exchange surface is arranged to facilitate flow of the solid particles throug h the heat exchanger.
  • a steam generator having a circulating fluidized bed combustion system whereby there is provision to admit air flow incrementally along the gas path to control combustion rate and firing temperature in a manner to maintain differential temperatures along the gas path.
  • the initial portion of the gas path where combustion is initiated can be held in one temperature range as 1 550F which is optimum for sulphur retention and the final portion of the combustion zone can be elevated in temperature as to 1 800F to produce a greater degree of heat transfer through the gas to fluid heat exchange surface downstream of the combustion zone.
  • U. S. Patent No. 4,745 ,884, May 24, 1 988, Coulthard discloses a fluidized bed steam generating system includes an upstanding combustion vessel, a gas/solids separator, a convection pass boiler and a heat exchanger positioned directly below the boiler and all of the above elements except the gas/solids separator are enclosed within a waterwall structure having outside waterwalls and a central waterwall common to the reactor vessel on one hand and the convection pass boiler and heat exchanger on the other hand.
  • the close proximity of the components of the system eliminate numerous problems present in conventional multi-solid fluidized bed steam generators.
  • the particle separator has a serpentine configuration which includes a first turn which is capable of causing the solid particles in the flue gas to move toward the rear membrane wall and a second turn which is capable of causing smaller sized solid particles and the flue gas to be disposed between the front membrane wall and the larger sized solid particles wherein the flue gas passes through the solid particles to a discharge conduit which is disposed within the rear membrane wall and wherein the smaller sized solid particles are retained between the front membrane wall and the larger sized solid particles.
  • the particle separator also includes a means for recycling the solid particles from the particle separator to the reactor chamber.
  • U. S. Patent No. 5,391 ,21 1 , issued February 21 , 1 995, to Alliston discloses an integral cylindrical cyclone and loopseal.
  • the cyclone separator for a solids-laden process gas from a reactor also provides a pressure seal for the reactor.
  • the cyclone includes a main housing with a longitudinal axis.
  • the housing is made of a membrane wall construction having a plurality of tubes arranged around the axis and encased within membrane wall panels. A portion of the tubes are bent outwardly to form an inlet which communicates with the main housing for receiving the solids-laden process gas from the boiler. Solids are separated from the solids-laden process gas as they swirl together in the main housing of the cyclone separator.
  • a partition wall is disposed at the lower section of the main housing around the longitudinal axis for defining an outer chamber and an inner chamber adjacent to the outer chamber. Gas is provided to the outer and inner chambers for creating fluidized beds of the solids in the outer and inner chambers. Solids are passed from the inner chamber to the outer chamber through an underflow port in the partition wall. Solids exit the main housing from an overflow port which communicates with the reactor.
  • a fluidized bed apparatus includes a vessel having a top and bottom, and defining a fluidized bed region.
  • the vessel further comprises a membrane wall.
  • a method of fluidizing includes fluidizing while heat is being provided through a membrane wall of the fluidizing vessel.
  • a method of fluidizing includes introducing particles into a fluidizing bed region of a vessel.
  • the method further includes providing heating through a membrane wall of the fluidizing vessel.
  • FIG. 1 is a schematic representation of one non-limiting example of a fluidized bed of the present invention.
  • FIG. 2 is a cutaway side view of a portion of vessel 1 0 of FIG. 1 , showing wall 1 1 0 and grid 1 8 as comprising tubes 202 arranged to from membrane walls 200.
  • FIG. 1 shows a schematic drawing of a fluidized bed gasifying apparatus or device 1 00 that includes means for agglomerating ash or particulate in the fluidized bed.
  • device 1 00 includes a vessel 1 0 within which a fluidized bed 1 2 is retained.
  • Vessel 1 00 further comprises outer wall 1 1 0.
  • Pulverized fresh feed coal enters via line 1 4 and is contained within the bottom portion of the vessel or reactor 1 0 as a fluid bed 1 2 having a bed density of about 1 5 to 30 pounds per cubic foot.
  • the coal within bed 1 0 is converted by reaction with steam and air to gaseous fuel components. These gaseous fuel components pass from the vessel 1 0 through a discharge line 1 6.
  • a shaped sloped grid 1 8 is provided within vessel 1 0 at the bottom of bed 1 2. Air and steam enter through a line 20 and pass through ports in grid 1 8 to assist in maintenance of bed 1 2 in a fluidized state.
  • the ash contained in the feed coal within bed 1 2 generally settles near the bottom of fluid bed 1 2 due to its greater density. Thus, the ash particles flow down the sides of the generally conical grid 1 8 and pass into or enter a withdrawal chamber or particle exit passage 22 that is formed as part of the grid 1 8.
  • FIG. 29 Referring additionally to FIG. 2 there is shown cutaway side view of a portion of vessel 1 0 of FIG. 1 , showing wall 1 1 0 and grid 1 8 as comprising tubes 202 arranged to from membrane walls 200.
  • the tubes of the membrane wall form a spiral flow path for the heat transfer fluid.
  • the membrane walls comprise tubes that are generally arranged in large panels or banks of parallel tu bes wh ich are connected together with a metal mem brane or web continuously interposed between each pair of adjacent tubes in the bank to form a tube wall. It shou ld be understood, that the d imensions for the membrane wall may be any suitable dimensions as desired and appropriate. It should also be u nderstood that the membrane walls may be made of any suitable material by any suitable method .
  • the tubes may generally have an outer d iameter which can range from about 1 inch up to about 3 inches, with a wall thickness which can be u p to about 0.5 inch.
  • the web or membrane connecting adjacent tubes to each other general ly has a thickness about equal to the wall thickness of the tubes, with the width of the webbing generally rang ing from about 0.25 inch to about 0.75 inch .
  • the webs or membranes can be welded to the outer walls of adjacent tubes to form the tube banks; however, the tube and connecting membranes can be, and preferably are, formed together in a single casting operation.
  • any part or all of device 1 00 may com prise one or more membrane wal ls.
  • part or all of wall 1 1 0 may comprise one or more membrane walls, and/or part or all of grid 1 8 may comprise one or more membrane walls.
  • FIG.3 there is shown a schematic of membrane wall 210 as forming wall 110 and grid 18.
  • membrane wall 210 comprises ports 211 and 212 for circulation of a heat transfer fluid.
  • membrane wall 220 As forming grid 18.
  • membrane wall 220 comprises ports 221 and 222 for circulation of a heat transfer fluid.
  • each of membrane walls 230, 240, 250 and 260 comprise ports 231 and 232 for circulation of a heat transfer fluid. It should be understood that membrane walls 230, 240, 250 and 260 may be operated independently to provide different heating/cooling zones as desired.
  • any single circulation loop may be provided with more than just a pair of ports, and may be provided with any suitable number of ports to vary/control the circulation as desired.
  • membrane walls may be utilized for other parts of system 100 other than just for wall 110 and grid 1 8.
  • one or more membrane walls may be utilized to form part or all of coal inlet stream 1 4, part or all of inlet stream 20, and/or part or all of inlet stream 28. Use of membrane walls at these streams may assist in preheating any reactants.
  • a membrane wall could also be utilized to cool outlet streams 1 6 and 30, or even to recover heat from outlet streams 1 6 and 30.
  • Various methods of the present invention for fluidizing particles include providing heating/cooling to the particles by circulating heat transfer fluid through one or more membrane walls.
  • a non-limiting example of a method of fluidizing is as follows. It should be understood that velocities, percentages, diameters, flow rates, temperatures, reactant compositions, output gas, and any other operating parameter, may be varied according to the operation desired. The following operating conditions are merely specific to this non-limiting example, and are not meant to limit the claimed invention in any way, shape or form.
  • the ash particles are contacted within passage 22 by a high velocity air-steam stream having a velocity in the range of about 50 to about 200 feet per second.
  • This high velocity air-steam stream enters the chamber or passage 22 by passing from line 28 and through the narrow throat or orifice 24 of the passage or venturi tube 22.
  • the ash particles may be admixed with a considerable amount of finely divided coal particles and form a semi-fixed bed in the passage 22.
  • this semi-fixed bed may have a density generally in the range of about 40 to about 60 pounds per cubic foot.
  • the air-steam stream represented by input throug h passage 22 may constitute in the range of approximately 20-40% of the total ai r and steam to the bed 1 2. The remainder enters by way of line 20 and grid 1 8.
  • the flu id bed has a temperature of 1 800F-2000F and the temperature in the region of the passage is about 2000F-2200F.
  • the velocity of the inlet gases through the venturi throat 24 may be high compared to the gas velocity at distribution grid 1 8.
  • This high velocity stream forms a jet or a spout giving rise to a violent and rapid circulation of solids in the zone of the passage 22.
  • the gases passing through the orifice 24 may also contain a higher percentage of the oxident than those gases passing through the distribution grid 1 8. Thereby, as previously explained, a higher temperature is generated in the zone of the passage 22 and in the middle, but not entirely through the fluidized bed 1 2.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)

Abstract

La présente invention concerne un appareil à lit fluidisé, au moins une partie de l'appareil comprenant une paroi membranaire.
PCT/US2010/041758 2010-07-13 2010-07-13 Lits fluidisés comprenant des parois membranaires et procédés de fluidisation WO2012008947A1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
PCT/US2010/041758 WO2012008947A1 (fr) 2010-07-13 2010-07-13 Lits fluidisés comprenant des parois membranaires et procédés de fluidisation

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
PCT/US2010/041758 WO2012008947A1 (fr) 2010-07-13 2010-07-13 Lits fluidisés comprenant des parois membranaires et procédés de fluidisation

Publications (1)

Publication Number Publication Date
WO2012008947A1 true WO2012008947A1 (fr) 2012-01-19

Family

ID=45469720

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/US2010/041758 WO2012008947A1 (fr) 2010-07-13 2010-07-13 Lits fluidisés comprenant des parois membranaires et procédés de fluidisation

Country Status (1)

Country Link
WO (1) WO2012008947A1 (fr)

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4466202A (en) * 1983-03-07 1984-08-21 Bend Research, Inc. Energy-efficient evaporation process with means for vapor recovery
US6699444B1 (en) * 1997-07-07 2004-03-02 Foster Wheeler Energia Oy Fluidized bed reactor
US20050036940A1 (en) * 2003-08-11 2005-02-17 Membrane Reactor Technologies Ltd. Internally circulating fluidized bed membrane reactor system
US20060013762A1 (en) * 2004-07-16 2006-01-19 Kuipers Johannes Alfonsius Mar Process and reactor for the production of hydrogen and carbon dioxide

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4466202A (en) * 1983-03-07 1984-08-21 Bend Research, Inc. Energy-efficient evaporation process with means for vapor recovery
US6699444B1 (en) * 1997-07-07 2004-03-02 Foster Wheeler Energia Oy Fluidized bed reactor
US20050036940A1 (en) * 2003-08-11 2005-02-17 Membrane Reactor Technologies Ltd. Internally circulating fluidized bed membrane reactor system
US20060013762A1 (en) * 2004-07-16 2006-01-19 Kuipers Johannes Alfonsius Mar Process and reactor for the production of hydrogen and carbon dioxide

Similar Documents

Publication Publication Date Title
EP0247798B1 (fr) Réacteur à lit fluidisé et procédé d'opération d'un tel réacteur
US4684375A (en) Method for gasifying a material using a circulating fluidized bed
EP0092622B1 (fr) Réacteur à lit fluidisé et sa méthode d'opération
EP0103613B2 (fr) Chaudiere rapide a lit fluidifie
US5033413A (en) Fluidized bed combustion system and method utilizing capped dual-sided contact units
US20100242361A1 (en) Fluidized beds having membrane walls and methods of fluidizing
AU2008298732B2 (en) Fluidized beds and methods of fluidizing
KR100289287B1 (ko) 유동층반응기시스템및그작동방법
US4947803A (en) Fludized bed reactor using capped dual-sided contact units and methods for use
CA3124409C (fr) Reacteur de gazeification et procede de gazeification
US5634516A (en) Method and apparatus for treating or utilizing a hot gas flow
US20090064580A1 (en) Venturi inserts, interchangeable venturis, and methods of fluidizing
US5005528A (en) Bubbling fluid bed boiler with recycle
US7803268B2 (en) Method and plant for producing low-temperature coke
CN103339442A (zh) 增强循环质量反应器操作的方法以及执行该方法的反应器
JPH0391602A (ja) 燃焼装置、特に、渦流層式燃焼装置
JPH0343524B2 (fr)
WO2012008947A1 (fr) Lits fluidisés comprenant des parois membranaires et procédés de fluidisation
US4945656A (en) Circulating fluidised bed apparatus
JPS6240601B2 (fr)
KR20100009098A (ko) 사각 형태의 이단 순환 유동층 반응기
WO1993000553A1 (fr) Procede et appareil de regulation de temperature dans un reacteur a lit fluidise
CA1280272C (fr) Reacteur a lit fluidise circulatoire bi-etage, et son fonctionnement
CS253584B2 (en) Device for heat and/or substance transfer

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 10854816

Country of ref document: EP

Kind code of ref document: A1

NENP Non-entry into the national phase

Ref country code: DE

122 Ep: pct application non-entry in european phase

Ref document number: 10854816

Country of ref document: EP

Kind code of ref document: A1