JPH01121616A - Control method for circulation particles volume and its control device in fluidized bed type-burner - Google Patents
Control method for circulation particles volume and its control device in fluidized bed type-burnerInfo
- Publication number
- JPH01121616A JPH01121616A JP28008587A JP28008587A JPH01121616A JP H01121616 A JPH01121616 A JP H01121616A JP 28008587 A JP28008587 A JP 28008587A JP 28008587 A JP28008587 A JP 28008587A JP H01121616 A JPH01121616 A JP H01121616A
- Authority
- JP
- Japan
- Prior art keywords
- bed
- circulating
- particles
- chamber
- temperature
- 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.)
- Granted
Links
- 239000002245 particle Substances 0.000 title claims abstract description 96
- 238000000034 method Methods 0.000 title claims description 10
- 239000007787 solid Substances 0.000 claims description 12
- 239000002699 waste material Substances 0.000 description 15
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 14
- 239000004576 sand Substances 0.000 description 8
- 238000007599 discharging Methods 0.000 description 6
- 239000000446 fuel Substances 0.000 description 4
- 238000002485 combustion reaction Methods 0.000 description 3
- 230000007423 decrease Effects 0.000 description 3
- 239000000377 silicon dioxide Substances 0.000 description 3
- 239000011343 solid material Substances 0.000 description 3
- 239000000428 dust Substances 0.000 description 2
- 150000003839 salts Chemical class 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 239000010815 organic waste Substances 0.000 description 1
- 238000005192 partition Methods 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 230000009257 reactivity Effects 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000007789 sealing Methods 0.000 description 1
- 238000010977 unit operation Methods 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/1809—Controlling processes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00548—Flow
Abstract
Description
【発明の詳細な説明】
〔産業上の利用分野〕
本発明は、流動床式焼却炉に係わり、特に、フリーボー
ド室内を循環する循環粒の量を最適な値に制御すること
のできる流動床式焼却炉における循環粒量の制御方法お
よびその装置に関する。[Detailed Description of the Invention] [Industrial Application Field] The present invention relates to a fluidized bed incinerator, and in particular, a fluidized bed in which the amount of circulating particles circulating in a freeboard chamber can be controlled to an optimum value. This invention relates to a method for controlling the amount of circulating particles in a type incinerator and an apparatus therefor.
〔従来の技術〕−
近時、都市ごみ等の焼却に流動床式焼却炉が用いられる
ようになってきている。[Prior Art] - In recent years, fluidized bed incinerators have come to be used to incinerate municipal waste.
第２図は、実公昭４６−１６４７４号公報に開示される
流動床式焼却炉を示すもので、図において符号１１は、
炉容器を示している。Figure 2 shows a fluidized bed incinerator disclosed in Japanese Utility Model Publication No. 46-16474, and the reference numeral 11 in the figure is
The furnace vessel is shown.
炉容器１１の下部には、珪砂等からなる不活性粒状固形
物１３によりベッド１５が形成され、このベッド１５が
流動層を形成する流動床となる。A bed 15 is formed in the lower part of the furnace vessel 11 by an inert granular solid material 13 made of silica sand or the like, and this bed 15 serves as a fluidized bed.
このベッド１５の上部の空間は、フリーボード室１７と
され、また、ベッド１５の下部には、ベッド１５に空気
を供給する空気室１９が配置されている。The space above the bed 15 is used as a freeboard chamber 17, and an air chamber 19 for supplying air to the bed 15 is arranged below the bed 15.
炉容器１１の上部には、廃棄物を炉容器１１内に供給す
るための供給管２１が開口しており、この供給管２１に
は、スクリュコンベア２３により廃棄物が供給される。A supply pipe 21 for supplying waste into the furnace vessel 11 is opened in the upper part of the furnace vessel 11, and waste is supplied to this supply pipe 21 by a screw conveyor 23.
炉容器１１の空気室１９には、空気供給管２５が開口し
ており、送風機２７からの空気が供給される。An air supply pipe 25 opens into the air chamber 19 of the furnace vessel 11, and air from a blower 27 is supplied thereto.
また、フリーボード室１７の上部と下部とはサイクロン
２９の配置される配管３１により連通されている。Further, the upper and lower parts of the freeboard chamber 17 are communicated with each other by a pipe 31 in which a cyclone 29 is arranged.
さらに、炉容器１１のベッド１５部には、燃料供給管３
３が開口している。Furthermore, a fuel supply pipe 3 is provided in the bed 15 of the furnace vessel 11.
3 is open.
以上のように構成された流動床式焼却炉では、炉容器１
１の上部の供給管２１から供給された廃棄物は、ベッド
１５上に落下し、空気室１りからの空気および燃料供給
管３３からの燃料により効率的に焼却される。In the fluidized bed incinerator configured as above, the furnace vessel 1
1 falls onto the bed 15 and is efficiently incinerated by air from the air chamber 1 and fuel from the fuel supply pipe 33.
そして、この流動床式焼却炉では、廃棄物の燃焼により
生じた灰分、塵埃等は、フリーボード室１７の上部から
サイクロン２９に導かれ分離され、主に灰分のみがフリ
ーボード室１７の下部に循環される。In this fluidized bed incinerator, ash, dust, etc. generated by combustion of waste are led to the cyclone 29 from the upper part of the freeboard chamber 17 and separated, and mainly only the ash is transferred to the lower part of the freeboard chamber 17. It is circulated.
この灰分の循環により、主に、有機廃棄物を有効に酸化
することが可能となる。This ash circulation primarily makes it possible to effectively oxidize organic waste.
しかしながら、このような従来の流動床式焼却炉では、
ベッド１５部において廃棄物の可燃分を完全燃焼するこ
とが困難であり、一部がフリーボード室１７内で燃焼す
るため、フリーボード室１７の上部の温度が極端に上昇
し、このような場合には、廃棄物の焼却量を減少する必
要があるという問題がある。However, in such conventional fluidized bed incinerators,
It is difficult to completely burn the combustible content of the waste in the bed 15, and some of it is burned in the freeboard chamber 17, so the temperature in the upper part of the freeboard chamber 17 rises extremely. The problem is that the amount of waste incinerated needs to be reduced.
特に、都市ごみの場合には、フリーボード室１７の上部
の温度が９５０℃前後に上昇することがあり、一方、こ
の場合には、ベッド１５部の温度は、５５０℃前後であ
る。In particular, in the case of municipal waste, the temperature of the upper part of the freeboard chamber 17 may rise to around 950°C, while in this case, the temperature of the bed 15 is around 550°C.
本発明者はかかる従来の問題を解決すべ・く鋭意研究し
た結果、フリーボード室１７の熱エネルギをベッド１５
部に供給することができれば、フリーボード室１７の温
度が低下するとともに、炉容器１１内の温度分布が均一
化され、これにより効率的な廃棄物の焼却を行なうこと
ができることを見出した。As a result of intensive research aimed at solving such conventional problems, the present inventor has discovered that the thermal energy of the freeboard room 17 can be transferred to the bed 15.
It has been found that if the waste can be supplied to the waste chamber, the temperature of the freeboard chamber 17 will be lowered and the temperature distribution within the furnace vessel 11 will be made uniform, thereby making it possible to efficiently incinerate waste.
そして、本発明者は、かかる知見に基づいて、炉容器の
下部に不活性粒状固形物によりベッドを形成し、このベ
ッドの上部の空間をフリーボード室とするとともに、前
記炉容器の前記ベッドの下部にベッドに空気を供給する
空気室を設けてなる流動床式焼却炉において、前記不活
性粒状固形物を、比較的粒径の大きい流動粒と、粒径の
小さい循環粒とにより構成するとともに、前記フリーボ
ード室の上部と前記ベッド部とをサイクロンの配置され
る循環粒循環配管により連通し、前記循環粒を前記フリ
ーボード室を介して前記循環粒循環配管内を循環させ、
前記炉容器内の温度分布を均一化することを特徴とする
流動床式焼却炉の温度分布均一化方法を発明した。Based on this knowledge, the present inventors formed a bed of inert granular solids in the lower part of the furnace vessel, made the space above this bed a freeboard chamber, and In a fluidized bed incinerator provided with an air chamber at the bottom for supplying air to the bed, the inert granular solids are composed of fluidized particles having a relatively large particle size and circulating particles having a small particle size, and , communicating the upper part of the freeboard chamber and the bed part through a circulating particle circulation pipe in which a cyclone is disposed, and circulating the circulating particles in the circulating particle circulation pipe via the freeboard chamber,
We have invented a method for uniformizing temperature distribution in a fluidized bed incinerator, which is characterized by uniformizing the temperature distribution within the furnace vessel.
この発明は、本出願人により、昭和６２年９月１４日に
出願されているが、この発明によれば、フリーボード室
内の熱エネルギは循環粒によりベッド部に効率的に運搬
され、ベッド部の流動粒に伝達され、これにより、炉容
器内の温度分布が均一化されることとなり、容易、確実
に炉容器内の温度分布を均一化することができる。This invention was filed by the present applicant on September 14, 1988, and according to this invention, thermal energy in the freeboard chamber is efficiently transported to the bed section by circulating particles, and As a result, the temperature distribution inside the furnace vessel can be made uniform, and the temperature distribution inside the furnace vessel can be easily and reliably made uniform.
しかしながら、上述した発明においては、循環粒の量を
制御するための具体的手段については、触れられていな
い。However, the above invention does not mention any specific means for controlling the amount of circulating particles.
一方、循環粒の量を最適に制御することは、炉容器内の
伝熱９反応等の単位操作上重要である。On the other hand, optimal control of the amount of circulating particles is important for unit operations such as heat transfer in a furnace vessel.
そこで、循環粒の量を直接計量することが考えられるが
、この場合には、炉容器内が非常に高温になるため、種
々の困難が伴うという問題がある。Therefore, it has been considered to directly measure the amount of circulating grains, but in this case, there is a problem that the inside of the furnace container becomes very high temperature, which is accompanied by various difficulties.
本発明者はかかる従来の問題を解決すべく鋭意研究した
結果、循環粒の量が所定量より増加した場合には、フリ
ーボード室の上部と下部との圧力差が増大し、一方、循
環粒の量が所定量より減少した場合には、フリーボード
室の上部と下部との温度差が増大することを見出した。As a result of intensive research to solve such conventional problems, the inventors of the present invention found that when the amount of circulating particles increases beyond a predetermined amount, the pressure difference between the upper and lower parts of the freeboard chamber increases; It has been found that when the amount of .
本発明は、かかる知見に基づいてなされたもので、容易
、確実に循環粒の量を制御することのできる流動床式焼
却炉における循環粒量の制御方法およびその装置を提供
することを目的とする。The present invention was made based on this knowledge, and an object of the present invention is to provide a method and apparatus for controlling the amount of circulating particles in a fluidized bed incinerator that can easily and reliably control the amount of circulating particles. do.
本発明にかかわる流動床式焼却炉における循環粒量の制
御方法は、炉容器の下部に不活性粒状固形物によりベッ
ドを形成し、このベッドの上部の空間をフリーボード室
とするとともに、前記炉容器の前記ベッドの下部にベッ
ドに空気を供給する空気室を設け、さらに、前記不活性
粒状固形物を、比較的粒径の大きい流動粒と、粒径の小
さい循環粒とにより構成するとともに、前記フリーボー
ド室の上部と前記ベッド部とをサイクロンの配置される
循環粒循環配管により連通し、前記循環粒を前記フリー
ボード室を介して前記循環粒循環配管内に循環させる流
動床式焼却炉において、前記フリーボード室の上部と下
部との圧力差が予め定められた一定値を越えた時に、前
記循環粒を前記炉容器外に排出し、一方、前記フリーボ
ード室の上部と前記ベッドとの温度差が予め定められた
一定値を越えた時に、前記循環粒を前記炉容器内に供給
し前記炉容器内の循環粒量を制御するものである。The method for controlling the amount of circulating particles in a fluidized bed incinerator according to the present invention is to form a bed of inert granular solids in the lower part of the furnace container, and use the space above the bed as a freeboard chamber. An air chamber is provided below the bed of the container to supply air to the bed, and the inert granular solids are composed of fluidized particles having a relatively large particle size and circulating particles having a small particle size, A fluidized bed incinerator in which the upper part of the freeboard chamber and the bed section are connected through a circulating particle circulation pipe in which a cyclone is arranged, and the circulating particles are circulated through the freeboard chamber and into the circulating particle circulation pipe. When the pressure difference between the upper and lower parts of the freeboard chamber exceeds a predetermined constant value, the circulating particles are discharged to the outside of the furnace vessel, while the upper part of the freeboard chamber and the bed are When the temperature difference exceeds a predetermined constant value, the circulating grains are supplied into the furnace vessel to control the amount of circulating grains in the furnace vessel.
また、本発明の流動床式焼却炉における循環粒量の制御
装置は、炉容器の下部に不活性粒状固形物によりベッド
を形成し、このベッドの上部の空間をフリーボード室と
するとともに、前記炉容器の前記ベッドの下部にベッド
に空気を供給する空気室を設け、さらに、前記不活性粒
状固形物を、比較的粒径の大きい流動粒と、粒径の小さ
い循環粒とにより構成するとともに、前記フリーボード
室の上部と前記ベッド部とをサイクロンの配置される循
環粒循環配管により連通し、前記循環粒を前記フリーボ
ード室を介して前記循環粒循環配管内に循環させる流動
床式焼却炉において、前記フリーボード室の上部の圧力
を測定する上部圧力計と、前記フリーボード室の下部の
圧力を測定する下部圧力計と、前記フリーボード室の上
部の温度を測定する上部温度計と、前記ベッドの温度を
測定する下部温度針と、前記上部圧力計、下部圧力計、
上部温度計および下部温度計からの圧力信号および温度
信号を入力し、下部圧力計の示す圧力値から上部圧力計
の示す圧力値を減算した値が予め定められた一定値を越
えた時に、前記循環粒を前記炉容器外に排出する排出機
構を作動するとともに、上部温度計の示す温度値から下
部温度計の示す温度値を減算した値が予め定められた一
定値を越えた時に、前記循環粒を前記炉容器内に供給す
る供給機構を作動する制御装置とを備えたものである。Furthermore, the apparatus for controlling the amount of circulating particles in a fluidized bed incinerator of the present invention forms a bed of inert granular solids in the lower part of the furnace container, and uses the space above the bed as a freeboard chamber. An air chamber for supplying air to the bed is provided in the lower part of the bed of the furnace vessel, and the inert granular solids are composed of fluidized particles having a relatively large particle size and circulating particles having a small particle size. , fluidized bed incineration in which the upper part of the freeboard chamber and the bed part are connected through a circulating particle circulation pipe in which a cyclone is arranged, and the circulating particles are circulated through the freeboard chamber into the circulating particle circulation pipe. In the furnace, an upper pressure gauge that measures the pressure in the upper part of the freeboard chamber, a lower pressure gauge that measures the pressure in the lower part of the freeboard chamber, and an upper thermometer that measures the temperature in the upper part of the freeboard chamber. , a lower temperature needle for measuring the temperature of the bed, the upper pressure gauge, the lower pressure gauge,
The pressure signal and temperature signal from the upper and lower thermometers are input, and when the value obtained by subtracting the pressure value indicated by the upper pressure gauge from the pressure value indicated by the lower pressure gauge exceeds a predetermined constant value, the The discharge mechanism for discharging circulating grains out of the furnace vessel is operated, and when the value obtained by subtracting the temperature value indicated by the lower thermometer from the temperature value indicated by the upper thermometer exceeds a predetermined constant value, the circulating grains are and a control device for operating a supply mechanism for supplying grains into the furnace vessel.
本発明の流動床式焼却炉における循環粒量の制御方法に
おいては、フリーボード室の上部と下部との圧力差が予
め定められた一定値を越えた時に循環粒が炉容器外に排
出され、一方、フリーボード室の上部とベッドとの温度
差が予め定められた一定値を越えた時に、循環粒が炉容
器内に供給される。In the method for controlling the amount of circulating particles in a fluidized bed incinerator of the present invention, when the pressure difference between the upper and lower parts of the freeboard chamber exceeds a predetermined constant value, the circulating particles are discharged outside the furnace vessel, On the other hand, when the temperature difference between the upper part of the freeboard chamber and the bed exceeds a predetermined constant value, circulating grains are fed into the furnace vessel.
また、本発明の流動床式焼却炉における循環粒量の制御
装置においては、下部圧力計の示す圧力値から上部圧力
計の示す圧力値を減算した値が予め定められた一定値を
越えた時に、循環粒を炉容器外に排出する排出機構が制
御装置により作動され、一方、上部温度計の示す温度値
から下部温度計の示す温度値を減算した値が予め定めら
れた一定値を越えた時に、循環粒を炉容器内に供給する
供給機構が制御装置により作動される。In addition, in the circulating particle amount control device in a fluidized bed incinerator of the present invention, when the value obtained by subtracting the pressure value indicated by the upper pressure gauge from the pressure value indicated by the lower pressure gauge exceeds a predetermined constant value, , the discharge mechanism for discharging the circulating grains out of the furnace vessel is activated by the control device, while the value obtained by subtracting the temperature value indicated by the lower thermometer from the temperature value indicated by the upper thermometer exceeds a predetermined constant value. At times, a feed mechanism is actuated by the control device to feed circulating grains into the furnace vessel.
以下、本発明方法およびその装置の詳細を図面を用いて
説明する。Hereinafter, details of the method and apparatus of the present invention will be explained using the drawings.
第１図は、本発明の流動床式焼却炉における循環粒量の
制御装置が配置される流動床式焼却炉の一例を示すもの
で、図において符号３５は、炉容器を示している。FIG. 1 shows an example of a fluidized bed incinerator in which a control device for controlling the amount of circulating particles in a fluidized bed incinerator according to the present invention is arranged, and in the figure, reference numeral 35 indicates a furnace vessel.
炉容器３５の下部には、珪砂等からなる不活性粒状固形
物３７によりベッド３９が形成され、このベッド３９が
流動床となる。このベッド３９の上部の空間は、フリー
ボード室４１とされ、また、ベッド３９の下部には、ベ
ッド３９に空気を供給する空気室４３が配置されている
。A bed 39 is formed in the lower part of the furnace vessel 35 by an inert granular solid material 37 made of silica sand or the like, and this bed 39 becomes a fluidized bed. The space above the bed 39 is used as a freeboard chamber 41, and an air chamber 43 for supplying air to the bed 39 is arranged below the bed 39.
炉容器３５の側部には、都市ごみ等の廃棄物を炉容器３
５内に供給するための供給管４５が開口しており、この
供給管４５には、シールバルブ４７が配置されている。On the side of the furnace container 35, waste such as municipal garbage is stored in the furnace container 3.
A supply pipe 45 for supplying the inside of the fuel cell 5 is open, and a seal valve 47 is disposed in the supply pipe 45.
炉容器３５の空気室４３には、空気供給管４９が開口し
ており、図示しない空気予熱器からの１次空気が供給さ
れる。An air supply pipe 49 opens into the air chamber 43 of the furnace vessel 35, and primary air is supplied from an air preheater (not shown).
また、炉容器３５のベッド３９部上方には、オイルガン
５０および起動バーナ５１が配置されている。Further, an oil gun 50 and a starting burner 51 are arranged above the bed 39 portion of the furnace vessel 35.
そして、フリーボード室４１の上部とベッド３９部とを
連通して、サイクロン５３の配置される循環粒循環配管
５５が配置されている。A circulating particle circulation pipe 55 in which a cyclone 53 is arranged is arranged to communicate the upper part of the freeboard chamber 41 and the bed 39 section.
また、ベッド３９部の下方には、隔壁板５７゜空気室４
３および炉容器３５を貫通して、後述する流動粒を残渣
とともに排出する排出管５９が開口している。Further, below the bed 39 section, there is a partition plate 57° air chamber 4.
3 and the furnace vessel 35 to open a discharge pipe 59 for discharging fluidized grains together with residue, which will be described later.
一方、炉容器３５の側方には、循環粒を供給する供給管
６１が開口している。On the other hand, a supply pipe 61 for supplying circulating grains is opened on the side of the furnace vessel 35.
排出管５９と供給管６１との間には、スクリュコンベア
からなる残渣排出機６３．振動ふるい６５、回収砂コン
ベア６７が配置され、回収砂コンベア６７の近傍には、
流動粉受は入れホッパ６９が配置され、また、供給管６
１の端部には、分岐ダンパ７０および貯蔵ホッパフェが
配置されている。Between the discharge pipe 59 and the supply pipe 61 is a residue discharger 63 consisting of a screw conveyor. A vibrating sieve 65 and a recovered sand conveyor 67 are arranged, and near the recovered sand conveyor 67,
A hopper 69 is arranged to receive the fluidized powder, and a supply pipe 6
At the end of 1, a branch damper 70 and a storage hopper are arranged.
そして、この流動床式焼却炉では、ベッド３９を形成す
る不活性粒状固形物３７は、比較的粒径の大きい流動粒
と、粒径の小さい循環粒とにより構成されており、循環
粒の粒径は、はぼ１００ミクロンメートルとされている
。In this fluidized bed incinerator, the inert granular solids 37 forming the bed 39 are composed of relatively large fluidized particles and small circulating particles. The diameter is approximately 100 micrometers.
また、運転時における循環粒の総重量は、流動粒の総重
量の１０〜２０％とされている。Further, the total weight of circulating grains during operation is 10 to 20% of the total weight of fluidized grains.
しかして、この実施例では、循環粒の量を最適状態に調
整するための流動床式焼却炉における循環粒量の制御装
置が配置されている。Therefore, in this embodiment, a control device for the amount of circulating particles in the fluidized bed incinerator is provided to adjust the amount of circulating particles to an optimum state.
この流動床式焼却炉における循環粒量の制御装置は、上
下圧力計、上下温度計および制御装置とから主体部分が
構成されている。A control device for the amount of circulating particles in this fluidized bed incinerator is mainly composed of an upper and lower pressure gauge, an upper and lower temperature gauge, and a control device.
すなおち、フリーボード室４１の上部には、フリーボー
ド室４１の上部の圧力を測定する上部圧力計７３が配置
されており、また、フリーボード室４１の下部には、フ
リーボード室４１の下部の圧力を測定する下部圧力計７
５が配置されている。In other words, an upper pressure gauge 73 for measuring the pressure at the upper part of the freeboard chamber 41 is arranged at the upper part of the freeboard chamber 41, and an upper pressure gauge 73 for measuring the pressure at the upper part of the freeboard chamber 41 is arranged at the lower part of the freeboard chamber 41. Lower pressure gauge 7 to measure the pressure of
5 is placed.
さらに、フリーボード室４１の上部には、フリーボード
室４１の上部の温度を測定する上部温度計７７が配置さ
れており、また、ベッド３９には、ベッド３９の温度を
測定する下部温度計７９が配置されている。Further, an upper thermometer 77 for measuring the temperature of the upper part of the freeboard chamber 41 is arranged at the upper part of the freeboard chamber 41, and a lower thermometer 79 for measuring the temperature of the bed 39 is disposed on the bed 39. is located.
また、この実施例では、上部圧力計７３．下部圧力計７
５．上部温度計７７および下部温度計７９からの圧力信
号および温度信号を入力する制御装置８１が配置されて
いる。Further, in this embodiment, the upper pressure gauge 73. Lower pressure gauge 7
5. A control device 81 is arranged to input pressure signals and temperature signals from the upper thermometer 77 and the lower thermometer 79.
この制御装置８１は、下部圧力計７５の示す圧力値から
上部圧力計７３の示す圧力値を減算した値が予め定めら
れた一定値、例えば、数＋ａａＡｑを越えた時に、循環
粒を炉容器３５外に排出する排出機構８３を作動する。This control device 81 controls the circulating grains to be transferred to the furnace vessel 35 when the value obtained by subtracting the pressure value indicated by the upper pressure gauge 73 from the pressure value indicated by the lower pressure gauge 75 exceeds a predetermined constant value, for example, a number + aaAq. The discharge mechanism 83 for discharging to the outside is activated.
この実施例では、排出機構８３は、循環粒循環配管５５
から分岐する分岐管８５とホッパー８７との間に制御弁
８９を配置して構成され、この制御弁８９を開とするこ
とにより、循環粒が炉容器３５外に排出される。In this embodiment, the discharge mechanism 83 includes the circulating particle circulation pipe 55
A control valve 89 is disposed between a branch pipe 85 branching from the hopper 87 and a hopper 87, and by opening the control valve 89, circulating grains are discharged to the outside of the furnace vessel 35.
また、制御装置８１は、上部温度計７９の示す温度値か
ら下部温度計７７の示す温度値を減算した値が予め定め
られた一定値、例えば１００°Ｃを越えた時に、循環粒
を炉容器３５内に供給する供給機構９１を作動する。Further, the control device 81 controls the circulating grains to be transferred to the furnace vessel when the value obtained by subtracting the temperature value indicated by the lower thermometer 77 from the temperature value indicated by the upper thermometer 79 exceeds a predetermined constant value, for example, 100°C. 35 is activated.
この実施例では、供給機構９１は、炉容器３５に開口す
る供給管６１と貯蔵ホッパー７１との間に制御弁９３を
配置して構成され、この制御弁９３を開とすることによ
り、循環粒が貯蔵ホッパー７１から炉容器３５内に供給
される。In this embodiment, the supply mechanism 91 is configured by disposing a control valve 93 between the supply pipe 61 that opens into the furnace vessel 35 and the storage hopper 71, and by opening the control valve 93, the circulating particles are is fed into the furnace vessel 35 from the storage hopper 71.
以上のように構成された流動床式焼却炉は、以下述べる
ようにして運転される。The fluidized bed incinerator configured as described above is operated as described below.
すなわち、運転開始に際して流動粒として、約７５０ｋ
ｇ／ｒＷの３号あるいは４号の珪砂が供給管６１からベ
ッド３９部に投入され、空気供給管４９から１次空気が
空気室４３内に供給され、この後、起動バーナ５１が点
火され、ヒートアップが開始される。In other words, at the start of operation, approximately 750k is produced as fluidized particles.
g/rW No. 3 or No. 4 silica sand is introduced into the bed 39 from the supply pipe 61, primary air is supplied into the air chamber 43 from the air supply pipe 49, and after this, the starting burner 51 is ignited. Heat-up begins.
流動粒が６００℃の温度に達した時に、オイルガン５０
によりベッド３９部にオイルが直接噴霧され、昇温され
る。なお、この時には、起動バーナ５１は消されている
。When the fluidized grain reaches a temperature of 600℃, the oil gun 50
Oil is directly sprayed onto the bed 39 and the temperature is raised. Note that, at this time, the starting burner 51 is turned off.
オイルガン５０により８００°Ｃまで昇温した時点で、
供給配管６１から循環粒が、流動粒の１０〜２０重量％
供給される。When the temperature is raised to 800°C with oil gun 50,
The circulating grains from the supply pipe 61 are 10 to 20% by weight of the fluidized grains.
Supplied.
循環粒が８００ ’Ｃになった時点で廃棄物が供給管４
５から炉容器３５内に供給される。この廃棄物の投入後
、廃棄物の燃焼熱により、オイルガン５０からのオイル
の消費量が徐々に減少し、通常は零となる。When the circulating grain reaches 800'C, the waste is transferred to the supply pipe 4.
5 into the furnace vessel 35. After the waste is introduced, the amount of oil consumed from the oil gun 50 gradually decreases to zero due to the heat of combustion of the waste.
そして、この状態で廃棄物の燃焼が行なわれるが、ベッ
ド３９を形成する不活性粒状固形物３７のうち循環粒は
、フリーボード室４１を上昇し、サイクロン５３により
分離され、循環粒循環配管５５を通り、ベッド３９部に
循環される。なお、この流動床式焼却炉では、サイクロ
ン５３により主に循環粒のみが捕獲され、灰分、塵埃等
は、外部に排出される。Then, waste is burned in this state, and the circulating particles among the inert granular solids 37 forming the bed 39 rise in the freeboard chamber 41, are separated by the cyclone 53, and are removed from the circulating particle circulation pipe 55. The water is circulated through the bed 39. In this fluidized bed incinerator, only circulating particles are mainly captured by the cyclone 53, and ash, dust, etc. are discharged to the outside.
一方、運転時あるいは運転終了後に、流動粒は、排出管
５９から排出され、残液排出機６５を通り、振動ふるい
６５で残渣を分離された後、回収砂コンベア６７を通り
、ベッド３９部に分岐ダンパ７０により再循環され、あ
るいは流動砂貯蔵ホッパ７１または流動砂受入ホッパ６
９に貯蔵される。On the other hand, during the operation or after the operation, the fluidized particles are discharged from the discharge pipe 59, pass through the residual liquid discharger 65, and after the residue is separated by the vibrating sieve 65, they pass through the recovery sand conveyor 67 and are sent to the bed 39 section. It is recirculated by the branch damper 70, or the fluidized sand storage hopper 71 or the fluidized sand receiving hopper 6.
Stored at 9.
そして、以上のように構成された流動床式焼却炉におけ
る循環粒量の制御装置では、循環粒の量が増大し、下部
圧力計７５の示す圧力値から上部圧力計７３の示す圧力
値を減算した値が予め定められた一定値を越えた時に、
制御装置８１により循環粒を炉容器３５外に排出するた
めの制御弁８９が開とされ、循環粒循環配管５５内の循
環粒が分岐管８５を通り、ホッパー８７から排出される
。In the apparatus for controlling the amount of circulating particles in a fluidized bed incinerator configured as described above, the amount of circulating particles increases, and the pressure value indicated by the upper pressure gauge 73 is subtracted from the pressure value indicated by the lower pressure gauge 75. When the value exceeds a predetermined value,
The control valve 89 for discharging the circulating grains to the outside of the furnace vessel 35 is opened by the control device 81, and the circulating grains in the circulating grain circulation pipe 55 pass through the branch pipe 85 and are discharged from the hopper 87.
一方、循環粒の量が減少し、上部温度計７９の示す温度
値から下部温度計７７の示す温度値を減算した値が予め
定められた一定値を越えた時に、循環粒を炉容器３５内
に供給する供給配管６１の制御弁６１が制御装置により
開とされ、貯蔵ホッパー７１内の循環粒が供給管６１か
ら炉容器３５内に供給される。On the other hand, when the amount of circulating particles decreases and the value obtained by subtracting the temperature value indicated by the lower thermometer 77 from the temperature value indicated by the upper thermometer 79 exceeds a predetermined constant value, the circulating particles are removed from the furnace vessel 35. The control valve 61 of the supply pipe 61 for supplying to the storage hopper 71 is opened by the control device, and the circulating grains in the storage hopper 71 are supplied from the supply pipe 61 into the furnace vessel 35 .
しかして、本発明の流動床式焼却炉における循環粒量の
制御装置では、循環粒の量が最適な所定量より増加した
場合には、フリーボード室３５の上部と下部との圧力差
が増大するため、下部圧力計７５の示す圧力値から上部
圧力計７３の示す圧力値を減算した値が予め定められた
一定値を越え、制御装置８１により循環粒が炉容器３５
外に排出されることとなる。Therefore, in the apparatus for controlling the amount of circulating particles in a fluidized bed incinerator of the present invention, when the amount of circulating particles increases beyond the optimal predetermined amount, the pressure difference between the upper and lower parts of the freeboard chamber 35 increases. Therefore, the value obtained by subtracting the pressure value indicated by the upper pressure gauge 73 from the pressure value indicated by the lower pressure gauge 75 exceeds a predetermined constant value, and the control device 81 causes the circulating grains to be transferred to the furnace vessel 35.
It will be discharged outside.
一方、循環粒の量が最適な所定量より減少した場合には
、フリーボード室４１の上部とベッド３９との温度差が
増大するため、上部温度計７９の示す温度値から下部温
度計７７の示す温度値を減算した値が予め定められた一
定値を越え、制御装置８１により、循環粒が炉容器３５
内に供給されることとなる。On the other hand, when the amount of circulating grains decreases below the optimal predetermined amount, the temperature difference between the upper part of the freeboard chamber 41 and the bed 39 increases, so that the temperature value indicated by the upper thermometer 79 changes from the temperature value indicated by the lower thermometer 77. When the value obtained by subtracting the temperature value shown in FIG.
It will be supplied within
従って、本発明の流動床式焼却炉における循環粒量の制
御装置によれば容易、 ｉ’ｉ実に循環粒の量を制御す
ることが可能となる。Therefore, according to the apparatus for controlling the amount of circulating particles in a fluidized bed incinerator of the present invention, it is possible to easily control the amount of circulating particles.
また、本発明の流動床式焼却炉における循環粒量の制御
方法によれば、フリーボード室４１の上部と下部との圧
力差が予め定められた一定値を越えた時に循環粒が炉容
器３５外に排出され、一方、フリーボード室４１の上部
と下部との温度差が予め定められた一定値を越えた時に
、循環粒が炉容器３５内に供給されることとなるため、
容易、 ＩＩｉ！実に循環粒の量を制御することが可能
となる。Further, according to the method for controlling the amount of circulating particles in a fluidized bed incinerator of the present invention, when the pressure difference between the upper and lower parts of the freeboard chamber 41 exceeds a predetermined constant value, the circulating particles are transferred to the furnace vessel 35. On the other hand, when the temperature difference between the upper and lower parts of the freeboard chamber 41 exceeds a predetermined constant value, the circulating grains are supplied into the furnace vessel 35.
Easy, IIi! Indeed, it becomes possible to control the amount of circulating particles.
また、以上のように構成された流動床式焼却炉では、フ
リーボード室４１内の熱エネルギは循環粒によりベッド
３９部に効率的に運搬され、ベッド３９部の流動粒に伝
達されるため、炉容器３５内の温度分布が確実に均一化
される。In addition, in the fluidized bed incinerator configured as above, the thermal energy in the freeboard chamber 41 is efficiently transported to the bed 39 section by the circulating grains and transmitted to the fluidized grains in the bed 39 section. The temperature distribution within the furnace vessel 35 is reliably made uniform.
また、この実施例では、循環粒循環配管５５の下端をベ
ッド３９部の流動層下部に開口したので、従来のように
流動層のガスがサイクロン５３の下部に吹き出すことが
なく、複雑なシール機構を省略することが可能となる。In addition, in this embodiment, the lower end of the circulating particle circulation pipe 55 is opened at the lower part of the fluidized bed in the bed 39 section, so that the gas in the fluidized bed does not blow out to the lower part of the cyclone 53 as in the conventional case, and a complicated sealing mechanism is required. can be omitted.
また、循環粒の循環量の制御は、流動層の空筒速度を変
化すること、および循環粒の系内ホールド量を変化する
ことにより容易に可能となる。Further, the amount of circulating particles can be easily controlled by changing the cylinder velocity of the fluidized bed and by changing the amount of circulating particles held in the system.
さらに、この実施例では、フリーボード室４１が、循環
粒の作用により希薄流動層となるため、フリーボード室
４１における反応性および伝熱性を向上でき、従来より
断面積、負荷および容積負荷を大きく取れるので、炉容
器３５をコンパクトなものにすることが可能となる。Furthermore, in this embodiment, the freeboard chamber 41 becomes a dilute fluidized bed due to the action of the circulating particles, so the reactivity and heat conductivity in the freeboard chamber 41 can be improved, and the cross-sectional area, load, and volume load can be increased compared to the conventional one. Since it can be removed, the furnace vessel 35 can be made compact.
また、この実施例では、サイクロン５３は、循環粒のみ
を捕集し、焼却灰は、捕集しないため、スケールおよび
タリンカーの発生に繋がる焼却灰中に含有されるＮａ、
に等の塩を速やかに炉容器３５外に排出することが可能
となる。In addition, in this embodiment, the cyclone 53 collects only the circulating particles and does not collect the incinerated ash.
It becomes possible to quickly discharge salts such as salts to the outside of the furnace vessel 35.
また、この実施例では、不活性粒状固形物３７として、
予め粒径の定められた流動粒と循環粒とを使用するよう
にしたので、設計上の燃焼および反応を正確に達成する
ことが可能となる。Moreover, in this example, as the inert particulate solid material 37,
Since fluidized particles and circulating particles with predetermined particle sizes are used, it is possible to accurately achieve the designed combustion and reaction.
さらに、この実施例では、ベッド３９部の下部に流動粒
を残渣とともに排出する排出管５９を設けたので、振動
ふるい６５を通して流動粒のみをベッド３９に循環する
ことが可能となる。Furthermore, in this embodiment, since the discharge pipe 59 for discharging the fluidized particles together with the residue is provided at the lower part of the bed 39, it is possible to circulate only the fluidized particles to the bed 39 through the vibrating sieve 65.
以上述べたように、本発明の構動床式焼却炉における循
環粒量−の制御方法によれば、フリーボード室の上部と
下部との圧力差が予め定められた一定値を越えた時に、
循環粒を炉容器外に排出し、一方、フリーボード室の上
部と下部との温度差が予め定められた一定値を越えた時
に、循環粒を炉容器内に供給し炉容器内の循環粒量を制
御するようにしたので、容易、１１実に循環粒の量を制
御することができるという利点がある。As described above, according to the method for controlling the amount of circulating particles in a structured bed incinerator of the present invention, when the pressure difference between the upper and lower parts of the freeboard chamber exceeds a predetermined constant value,
The circulating grains are discharged outside the furnace vessel, and when the temperature difference between the upper and lower parts of the freeboard chamber exceeds a predetermined value, the circulating grains are supplied into the furnace vessel and the circulating grains inside the furnace vessel are discharged. Since the amount is controlled, there is an advantage that the amount of circulating grains can be easily controlled.
また、本発明の流動床式焼却炉における循環粒量の制御
装置では、装置を、フリーボード室の上部の圧力を測定
する上部圧力計と、フリーボード室の下部の圧力を測定
する下部圧力計と、フリーボード室の上部の温度を測定
する上部温度計と、フリーボード室の下部の温度を測定
する下部温度計と、上部圧力計、下部圧力計、上部温度
計および下部温度計からの圧力信号および温度信号を入
力し、下部圧力計の示す圧力値から上部圧力計の示す圧
力値を減算した値が予め定められた一定値を越えた時に
、循環粒を炉容器外に排出する排出機構を作動するとと
もに、上部温度計の示す温度値から下部温度計の示す温
度値を減算した値が予め定められた一定値を越えた時に
、循環粒を炉容器内に供給する供給機構を作動する制御
装置から構成したので、簡易な構成により容易、確実に
循環粒の量を制御することができるという利点がある。Furthermore, in the apparatus for controlling the amount of circulating particles in a fluidized bed incinerator of the present invention, the apparatus includes an upper pressure gauge that measures the pressure in the upper part of the freeboard chamber, and a lower pressure gauge that measures the pressure in the lower part of the freeboard chamber. , an upper thermometer that measures the temperature at the top of the freeboard chamber, a lower thermometer that measures the temperature at the bottom of the freeboard chamber, and the pressures from the upper pressure gauge, the lower pressure gauge, the upper thermometer, and the lower thermometer. A discharge mechanism that inputs signals and temperature signals and discharges circulating grains from the furnace vessel when the value obtained by subtracting the pressure value indicated by the upper pressure gauge from the pressure value indicated by the lower pressure gauge exceeds a predetermined constant value. At the same time, when the value obtained by subtracting the temperature value indicated by the lower thermometer from the temperature value indicated by the upper thermometer exceeds a predetermined constant value, the supply mechanism for supplying circulating grains into the furnace vessel is operated. Since it is composed of a control device, there is an advantage that the amount of circulating particles can be easily and reliably controlled with a simple structure.
第１図は本発明の流動床式焼却炉における循環粒量の制
御装置の一実施例が配置される流動床式焼却炉の一例を
示す縦断面図である。
第２図は従来の流動床式焼却炉を示す縦断面図である。
〔主要な部分の符号の説明〕
３５・・・炉容器
３９・・・ベッド
４１・・・フリーボード室
５３・・・サイクロン
５５・・・循環籾循環配管
５９・・・排出管
６１・・・供給管
７３・・・上部圧力計
７５・・・下部圧力計
７７・・・上部温度計
７９・・・下部温度計
８１・・・制御装置
８３・・・排出機構
９１・・・供給機構。
第２図FIG. 1 is a longitudinal sectional view showing an example of a fluidized bed incinerator in which an embodiment of the circulating particle amount control device in a fluidized bed incinerator according to the present invention is arranged. FIG. 2 is a longitudinal sectional view showing a conventional fluidized bed incinerator. [Explanation of symbols of main parts] 35...furnace vessel 39...bed 41...freeboard chamber 53...cyclone 55...circulation paddy circulation pipe 59...discharge pipe 61... Supply pipe 73... Upper pressure gauge 75... Lower pressure gauge 77... Upper thermometer 79... Lower thermometer 81... Control device 83... Discharge mechanism 91... Supply mechanism. Figure 2
Claims (2)
形成し、このベッドの上部の空間をフリーボード室とす
るとともに、前記炉容器の前記ベッドの下部にベッドに
空気を供給する空気室を設け、さらに、前記不活性粒状
固形物を、比較的粒径の大きい流動粒と、粒径の小さい
循環粒とにより構成するとともに、前記フリーボード室
の上部と前記ベッド部とをサイクロンの配置される循環
粒循環配管により連通し、前記循環粒を前記フリーボー
ド室を介して前記循環粒循環配管内に循環させる流動床
式焼却炉において、前記フリーボード室の上部と下部と
の圧力差が予め定められた一定値を越えた時に、前記循
環粒を前記炉容器外に排出し、一方、前記フリーボード
室の上部と前記ベッドとの温度差が予め定められた一定
値を越えた時に、前記循環粒を前記炉容器内に供給し前
記炉容器内の循環粒量を制御することを特徴とする流動
床式焼却炉における循環粒量の制御方法。(1) A bed is formed at the bottom of the furnace vessel by inert granular solids, the space above the bed is used as a freeboard chamber, and an air chamber is provided at the bottom of the bed of the furnace vessel for supplying air to the bed. Further, the inert granular solids are composed of relatively large fluidized particles and small circulating particles, and the upper part of the freeboard chamber and the bed section are arranged in a cyclone. In a fluidized bed incinerator in which the circulating particles are communicated by a circulating particle circulation pipe in which the circulating particles are circulated through the freeboard chamber and into the circulating particle circulation pipe, the pressure difference between the upper and lower parts of the freeboard chamber is When the temperature difference between the upper part of the freeboard chamber and the bed exceeds a predetermined value, the circulating grains are discharged out of the furnace vessel when the temperature exceeds a predetermined value. A method for controlling the amount of circulating particles in a fluidized bed incinerator, characterized in that the amount of circulating particles in the furnace container is controlled by supplying the circulating particles into the furnace container.
形成し、このベッドの上部の空間をフリーボード室とす
るとともに、前記炉容器の前記ベッドの下部にベッドに
空気を供給する空気室を設け、さらに、前記不活性粒状
固形物を、比較的粒径の大きい流動粒と、粒径の小さい
循環粒とにより構成するとともに、前記フリーボード室
の上部と前記ベッド部とをサイクロンの配置される循環
粒循環配管により連通し、前記循環粒を前記フリーボー
ド室を介して前記循環粒循環配管内に循環させる流動床
式焼却炉において、前記フリーボード室の上部の圧力を
測定する上部圧力計と、前記フリーボード室の下部の圧
力を測定する下部圧力計と、前記フリーボード室の上部
の温度を測定する上部温度計と、前記ベッドの温度を測
定する下部温度計と、前記上部圧力計、下部圧力計、上
部温度計および下部温度計からの圧力信号および温度信
号を入力し、下部圧力計の示す圧力値から上部圧力計の
示す圧力値を減算した値が予め定められた一定値を越え
た時に、前記循環粒を前記炉容器外に排出する排出機構
を作動するとともに、上部温度計の示す温度値から下部
温度計の示す温度値を減算した値が予め定められた一定
値を越えた時に、前記循環粒を前記炉容器内に供給する
供給機構を作動する制御装置とを備えたことを特徴とす
る流動床式焼却炉における循環位置の制御装置。(2) A bed is formed at the bottom of the furnace vessel by inert granular solids, the space above the bed is used as a freeboard chamber, and an air chamber is provided at the bottom of the bed of the furnace vessel for supplying air to the bed. Further, the inert granular solids are composed of relatively large fluidized particles and small circulating particles, and the upper part of the freeboard chamber and the bed section are arranged in a cyclone. In a fluidized bed incinerator, the pressure at the upper part of the freeboard chamber is measured. a lower pressure gauge for measuring the pressure in the lower part of the freeboard chamber, an upper thermometer for measuring the temperature in the upper part of the freeboard chamber, a lower thermometer for measuring the temperature in the bed, and the upper pressure gauge. A predetermined constant value is obtained by subtracting the pressure value indicated by the upper pressure gauge from the pressure value indicated by the lower pressure gauge. When the temperature exceeds the temperature, a discharge mechanism is operated to discharge the circulating grains out of the furnace vessel, and the value obtained by subtracting the temperature value indicated by the lower thermometer from the temperature value indicated by the upper thermometer reaches a predetermined constant value. A control device for controlling a circulation position in a fluidized bed incinerator, comprising: a control device for operating a supply mechanism for supplying the circulating particles into the furnace vessel when the circulating particles are exceeded.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP28008587A JPH0816526B2 (en) | 1987-11-05 | 1987-11-05 | Method and apparatus for controlling circulating particle amount in fluidized bed incinerator |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP28008587A JPH0816526B2 (en) | 1987-11-05 | 1987-11-05 | Method and apparatus for controlling circulating particle amount in fluidized bed incinerator |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH01121616A true JPH01121616A (en) | 1989-05-15 |
| JPH0816526B2 JPH0816526B2 (en) | 1996-02-21 |
Family
ID=17620102
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP28008587A Expired - Fee Related JPH0816526B2 (en) | 1987-11-05 | 1987-11-05 | Method and apparatus for controlling circulating particle amount in fluidized bed incinerator |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH0816526B2 (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH037807A (en) * | 1989-06-02 | 1991-01-16 | Ngk Insulators Ltd | Controller and control of furnace temperature in fluidized bed incinerator |
| EP0694331A1 (en) * | 1994-07-28 | 1996-01-31 | GEC ALSTHOM Stein Industrie | Process and device for controlling the internal circulation of a fluidised bed reactor and reactor provided with such a device |
| JP2009204282A (en) * | 2008-02-29 | 2009-09-10 | Mhi Environment Engineering Co Ltd | Sludge treatment method and sludge treatment system with circulating fluidized bed furnace |
| JP2020159584A (en) * | 2019-03-25 | 2020-10-01 | 住友金属鉱山株式会社 | Method for starting circulation fluidized bed boiler |
-
1987
- 1987-11-05 JP JP28008587A patent/JPH0816526B2/en not_active Expired - Fee Related
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH037807A (en) * | 1989-06-02 | 1991-01-16 | Ngk Insulators Ltd | Controller and control of furnace temperature in fluidized bed incinerator |
| EP0694331A1 (en) * | 1994-07-28 | 1996-01-31 | GEC ALSTHOM Stein Industrie | Process and device for controlling the internal circulation of a fluidised bed reactor and reactor provided with such a device |
| FR2723003A1 (en) * | 1994-07-28 | 1996-02-02 | Gec Alsthom Stein Ind | METHOD AND DEVICE FOR CONTROLLING INTERNAL CIRCULATION IN A FLUIDIZED BED REACTOR AND REACTOR PROVIDED WITH SUCH A DEVICE |
| US5628967A (en) * | 1994-07-28 | 1997-05-13 | Gec Alsthom Stein Industrie | Method and a device for monitoring the internal circulation in a fluidized bed reactor, and a reactor provided with such a device |
| US5700431A (en) * | 1994-07-28 | 1997-12-23 | Gec Alsthom Stein Industrie | Method and a device for monitoring the internal circulation in a fluidized bed reactor, and a reactor provided with such a device |
| JP2009204282A (en) * | 2008-02-29 | 2009-09-10 | Mhi Environment Engineering Co Ltd | Sludge treatment method and sludge treatment system with circulating fluidized bed furnace |
| JP2020159584A (en) * | 2019-03-25 | 2020-10-01 | 住友金属鉱山株式会社 | Method for starting circulation fluidized bed boiler |
Also Published As
| Publication number | Publication date |
|---|---|
| JPH0816526B2 (en) | 1996-02-21 |
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