WO1999051917A1 - Lit fluidise circulant - Google Patents

Lit fluidise circulant Download PDF

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Publication number
WO1999051917A1
WO1999051917A1 PCT/JP1999/001663 JP9901663W WO9951917A1 WO 1999051917 A1 WO1999051917 A1 WO 1999051917A1 JP 9901663 W JP9901663 W JP 9901663W WO 9951917 A1 WO9951917 A1 WO 9951917A1
Authority
WO
WIPO (PCT)
Prior art keywords
fluidized bed
combustion
gas
circulating
bed
Prior art date
Application number
PCT/JP1999/001663
Other languages
English (en)
Japanese (ja)
Inventor
Kanichi Ito
Original Assignee
Ebara 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 Ebara Corporation filed Critical Ebara Corporation
Priority to JP2000542609A priority Critical patent/JP3497822B2/ja
Priority to AU30538/99A priority patent/AU3053899A/en
Publication of WO1999051917A1 publication Critical patent/WO1999051917A1/fr

Links

Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN  A CARRIER GAS OR AIR 
    • F23C10/00—Fluidised bed combustion apparatus
    • F23C10/005—Fluidised bed combustion apparatus comprising two or more beds
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN  A CARRIER GAS OR AIR 
    • F23C10/00—Fluidised bed combustion apparatus
    • F23C10/02—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/30—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having a fluidised bed
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2203/00—Furnace arrangements
    • F23G2203/50—Fluidised bed furnace
    • F23G2203/503—Fluidised bed furnace with two or more fluidised beds

Definitions

  • the present invention relates to a fluidized bed used for heat treatment of solid waste such as garbage and waste plastic.
  • the temperature inside the furnace becomes as high as 130 to 140 ° C in order to melt and drop ash on the inner wall as described above.
  • Heat dissipation ⁇ It is necessary to prevent heat loss, so the construction of the furnace wall is expensive. There was a title.
  • FIG. 10 and 11 are views showing a conventional two-tower circulation type fluidized bed, wherein FIG. 10 is a schematic sectional view, and FIG. 11 is a view taken in the direction of arrow Z in FIG.
  • the two-column circulating fluidized bed is composed of a pyrolysis gasification fluidized bed 51 and a combustion fluidized bed 52 of the first class, which are connected by a pair of pipes 53, 54.
  • the amount of heat required for pyrolysis is supplied by circulating the heat medium in two towers.
  • the pyrolysis gas is taken out separately from the combustion exhaust gas.
  • the heat medium in the fluidized bed has a property that it is difficult to move in the horizontal direction, in this configuration, the heat medium is locally supplied by piping and tends to flow short-circuited as indicated by arrows 55 and 56.
  • it was necessary to increase the height H of the fluidized bed in order to cause a sufficient reaction in the fluidized bed, it was necessary to increase the height H of the fluidized bed, and there was a problem that not only the power loss of fluidization was increased but also the size of the apparatus was increased.
  • the generated HC1 is included in the pyrolysis gas.
  • High temperature corrosion occurs due to HC 1 gas in the equipment.
  • complicated pre-treatment was required, such as mechanical removal of vinyl chloride in advance or thermal decomposition separately after heating and melting to remove chlorine. Disclosure of the invention
  • the present invention solves the above-mentioned problems, that is, (1) a high calorie gas capable of rapidly heating a cycle-opening combustion melting furnace even with a low calorie and high moisture content refuse raw material can be obtained. (2)
  • the construction of a cyclone combustion and melting furnace with a high furnace temperature does not require expensive furnace walls. There is no danger of short-circuiting in the circulation of the heat medium as in the two-tower circulation system described in (1), and the equipment is small and compact with small motive power.
  • Waste plastic raw materials containing vinyl chloride etc. The purpose is to obtain a gas applicable to the cycling furnace and to avoid high-temperature corrosion of HC1 by HC1 in various devices after the melting furnace.
  • the invention according to claim 1 comprises forming a fluidized bed in a loop shape, and separating the middle of the looped fluidized bed with a moving bed and having a plurality of independent free boards. It is characterized in that the fluidized medium is circulated using the specific gravity difference between the moving bed and the fluidized bed as the driving force.
  • the fluidized bed in the loop fluidized bed according to the first aspect, is formed in an annular shape, and a cycle opening combustion melting is formed at the center of the annular fluidized bed. It is characterized by building a furnace.
  • the invention according to claim 3 is the annular fluidized bed according to claim 2, wherein the annular fluidized bed is partitioned by two moving beds to form a pyrolysis gasification fluidized bed and a combustion fluidized bed of a class.
  • the generated pyrolysis gas is supplied to the cycle-port combustion melting furnace in the center.
  • the invention according to claim 4 is characterized in that, in the annular fluidized bed according to claim 2, a heat transfer tube is provided in the moving bed.
  • the invention according to claim 5 provides the annular fluidized bed according to claim 4, wherein the annular fluidized bed is partitioned by two moving beds to form a dechlorination fluidized bed and a pyrolysis gasification fluidized bed. It is characterized in that the generated pyrolysis gas is supplied to the central cyclone combustion melting furnace.
  • FIG. 1 is an explanatory view of a system embodiment including a longitudinal sectional view of a circulating fluidized bed according to the present invention.
  • the circulating fluidized bed body is a Y-Y sectional view common to FIGS. 2 and 3.
  • FIG. 2 is a circulating fluidized bed according to the third aspect of the present invention, and is a view as seen from the arrow P in FIG.
  • FIG. 3 is a circulating fluidized bed according to the third aspect of the present invention, and is a sectional view taken along line XX of FIG.
  • FIG. 4 is a development sectional view of R_R of FIG.
  • FIG. 5 is an explanatory view of another system embodiment including a vertical sectional view of the circulating fluidized bed of the present invention.
  • the circulating fluidized bed main body is a Y-Y sectional view common to FIGS. 6 and 7.
  • FIG. 6 is a circulating fluidized bed according to the fourth and fifth aspects of the present invention, and is a view as seen from the arrow P in FIG.
  • FIG. 7 is a circulating fluidized bed according to the fourth and fifth aspects of the present invention, and is a cross-sectional view taken along line XX of FIG.
  • FIG. 8 is an R-R development sectional view of FIG.
  • FIG. 9 shows another embodiment of the gas dispersion plate and the gas chamber.
  • FIG. 10 is a longitudinal sectional view of a conventional two-column circulation type fluidized bed.
  • FIG. 11 is a view on arrow Z in FIG. BEST MODE FOR CARRYING OUT THE INVENTION
  • the pyrolysis gasification fluidized bed 1 and the combustion fluidized bed 2 are formed in an annular shape by an outer cylinder wall 3 and an inner cylinder wall 4.
  • the fluidized bed is partitioned by moving layers 9 and 10 composed of a partition 6 having an opening 5 at the upper end and a partition 8 having an opening 7 at the lower end.
  • non-oxidizing gas 13 such as recirculated pyrolysis gas 13 and combustion air 14 are supplied to 12 respectively
  • fluidized medium sand
  • a pyrolysis gasification fluidized bed 1 and a combustion fluidized bed 2 are formed.
  • the non-oxidizing gas refers to a gas containing no oxygen, such as recycle gas of the pyrolysis gases, refers to the this non-oxidizing gas containing no 0 2 (oxygen) combustion-supporting .
  • the composition of the pyrolysis gas is CO (—carbon oxide), H 2
  • the fluidized medium (sand) is the pyrolysis gasification fluidized bed 1 ⁇ the upper opening 5 ⁇ Moving bed 9—opening at lower end 7 ⁇ combustion fluidized bed 2 ⁇ opening at upper end 5 ⁇ moving bed 10 ⁇ opening at lower end 7 ⁇ pyrolysis gasifier 1 That is, if the upper surface 17 of the fluidized bed is higher than the lower surface 18 of the opening 5 at the upper end, the fluid medium overflows and circulates automatically in the direction of arrow 19, and the circulation speed is the width B of the moving bed.
  • the flow rate is regulated by the overflow height ⁇ .
  • the circulation speed can be controlled by adjusting the height H of the fluidized bed.
  • the flue gas 24 is taken out from the flue gas outlet 26 through the free board 25, but the two free boards 22 and 25 are separated by the partition walls 6 and 8 and the moving bed 9 and 10 and are independent.
  • the force opening Li one this good Una pyrolysis gas is about 5 0 ⁇ 0 k C a 1 Z m 3 This has been experimentally confirmed to be reached.
  • reference numeral 27 denotes a double discharge valve for removing incombustible residue, and the removed incombustible residue is sieved and the fluid medium (sand) under the sieve is returned to the fluidized bed again.
  • the inner cylinder wall 4 of the annular fluidized bed is extended slightly upward, and the combustion gas 21 is formed on the upper part of the cylinder as shown in FIGS.
  • the supply port 29 and the supply port 31 for the pressurized air 30 are provided tangentially, and an exhaust gas outlet 32 is provided at the center of the upper part.
  • the fluidized bed is constructed in an annular shape.
  • the fluidized bed in order to circulate the fluidized medium, is not limited to an annular shape, but is formed into an elliptical annular shape. Any shape is acceptable.
  • the fluidized medium is extruded and moved in a "place-and-place" manner, so there is no risk of short-circuiting as in the conventional two-column circulating type, and the height H of the fluidized bed is reduced. At least, the reaction is sufficiently promoted in the fluidized bed. Therefore, the circulating fluidized bed is not limited to heat treatment of solid waste, but can be applied to cracking of heavy oil, for example.
  • the dispersion plate 15 is formed into a V-shape, and the gas chamber 11 is set to 1 1 — 1 to 1 1 — Divide as shown in 4 and supply to the outer gas chambers 1 1 1 1 and 1 1-4 Supply the gas pressure of the gas pipe 13-1 to the inner gas chambers 1 1-2 and 1 1-13 It is advisable to raise the gas pressure higher than the gas pressure of the gas pipe 13-2 to agitate the fluidized bed as shown by arrow 44.
  • a gas cleaning device 43 for cleaning 4 A to remove H C 1 is provided. Air is supplied from the gas chamber 11 below the pyrolysis gasification fluidized bed 1 as fluidizing gas to perform pyrolysis at about 400 to 600 ° C by partial combustion. However, since the waste plastics as raw materials have a high calorific value, a high-strength port gas which can be sufficiently applied to the cycle-port combustion melting furnace 28 can be obtained. A part of the clean pyrolysis gas from the gas cleaning device 4 3 is recirculated and supplied as a fluidizing gas for the dechlorination fluidized bed 2 A from the gas chamber 12, and partial combustion as necessary At least, adjust to the appropriate temperature of 300 to 350 ° C for dechlorination.
  • waste plastic raw material including vinyl chloride is supplied from the raw material supply device 20 to the dechlorination fluidized bed 2A, The solids from which incombustibles have been removed from the double discharge valve 27 and from which chlorine has been removed are moved to the pyrolysis gasification fluidized bed 1 together with the fluidized medium and gasified.
  • HC 1 rich gas 24 A discharged from the gas outlet 26 A of the dechlorination fluidized bed 2 A is purified by the gas cleaning device 43, then combined with the pyrolysis gas 21, and then supplied from the supply port 29. Supplied to cyclone combustion melting furnace 28.
  • a plurality of fluidized beds having independent free boards are formed in a loop shape, and the fluidized medium is extruded in a "roll-to-roll type" so that each fluidized bed is extruded. Because the bed is circulated, there is no danger of short-circuiting and circulation as in the conventional two-column circulation system.If the height of the fluidized bed is reduced, the reaction is sufficiently promoted and the fluidization power is reduced.
  • the equipment can be made compact.
  • the cyclone combustion melting furnace is provided at the center of the annular fluidized bed and the outside is surrounded by the fluidized bed. Heat radiation from walls ⁇ No need for expensive furnace walls to prevent heat loss.
  • the gas calorie is high even in the low-calorie high-moisture content refuse, and the cycle requiring rapid high-temperature heating is required. It can be used as a fuel for the mouth combustion melting furnace. That is, it is possible to provide a “gasification and melting furnace” that can be used regardless of the calorific value of the raw material waste.
  • the fluidized bed temperature can be adjusted in the intermediate moving bed, a circulating fluidized bed composed of a plurality of fluidized beds having different temperatures can be constructed.
  • a gasification and fusion furnace that combines a pyrolysis gasification fluidized bed furnace and a cyclone combustion and melting furnace, which have many environmental advantages, is used.
  • the furnace can be made compact and its applicability can be greatly expanded.
  • the present invention relates to a fluidized bed used for heat treatment of solid waste such as municipal solid waste and waste plastic, and can be suitably used for waste treatment.

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  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Gasification And Melting Of Waste (AREA)

Abstract

L'invention concerne un lit fluidisé circulant destiné au traitement thermique de déchets solides tels que des déchets urbains et des déchets plastiques. Le lit fluidisé circulant est de type en boucle et se divise en lits fluidisés (1, 2) séparés dans une partie intermédiaire par des lits mobiles (9, 10) et comportant des panneaux libres indépendants (22, 25). Dans le lit fluidisé circulant, un milieu fluide est mis en circulation par une force d'entraînement générée par la différence entre les lits mobiles (9, 10) et les lits fluidisés (1, 2).
PCT/JP1999/001663 1998-03-31 1999-03-31 Lit fluidise circulant WO1999051917A1 (fr)

Priority Applications (2)

Application Number Priority Date Filing Date Title
JP2000542609A JP3497822B2 (ja) 1998-03-31 1999-03-31 循環流動層
AU30538/99A AU3053899A (en) 1998-03-31 1999-03-31 Circulating fluidized bed

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
JP10/125210 1998-03-31
JP12521098 1998-03-31

Publications (1)

Publication Number Publication Date
WO1999051917A1 true WO1999051917A1 (fr) 1999-10-14

Family

ID=14904615

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/JP1999/001663 WO1999051917A1 (fr) 1998-03-31 1999-03-31 Lit fluidise circulant

Country Status (3)

Country Link
JP (1) JP3497822B2 (fr)
AU (1) AU3053899A (fr)
WO (1) WO1999051917A1 (fr)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP2978821B1 (fr) * 2013-03-28 2020-11-11 Carbon Gold Limited Procédé de production de biochar

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
KR102175676B1 (ko) * 2019-02-20 2020-11-06 주식회사 대경에스코 유동상 열분해장치 및 이를 이용한 유기성 물질의 열분해 방법

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS5135467B2 (fr) * 1972-12-14 1976-10-02
JPS51130079A (en) * 1975-05-06 1976-11-12 Agency Of Ind Science & Technol Method and apparatus for fluidized thermal decomposition of organic so lid city wastes
JPS5330480A (en) * 1976-09-01 1978-03-22 Ishigaki Mech Ind Recycling fluid layer thermocracking furnace
JPS5839194B2 (ja) * 1975-04-14 1983-08-27 カブシキガイシヤ エバラセイサクシヨ ユウキブツノネツブンカイホウホウ オヨビ ネツブンカイソウチ
JPS6235004B2 (fr) * 1979-06-20 1987-07-30 Ebara Mfg
JPH102543A (ja) * 1996-06-11 1998-01-06 Ebara Corp 流動層ガス化燃焼炉

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS5135467B2 (fr) * 1972-12-14 1976-10-02
JPS5839194B2 (ja) * 1975-04-14 1983-08-27 カブシキガイシヤ エバラセイサクシヨ ユウキブツノネツブンカイホウホウ オヨビ ネツブンカイソウチ
JPS51130079A (en) * 1975-05-06 1976-11-12 Agency Of Ind Science & Technol Method and apparatus for fluidized thermal decomposition of organic so lid city wastes
JPS5330480A (en) * 1976-09-01 1978-03-22 Ishigaki Mech Ind Recycling fluid layer thermocracking furnace
JPS6235004B2 (fr) * 1979-06-20 1987-07-30 Ebara Mfg
JPH102543A (ja) * 1996-06-11 1998-01-06 Ebara Corp 流動層ガス化燃焼炉

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP2978821B1 (fr) * 2013-03-28 2020-11-11 Carbon Gold Limited Procédé de production de biochar

Also Published As

Publication number Publication date
JP3497822B2 (ja) 2004-02-16
AU3053899A (en) 1999-10-25

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