JPS6261861B2 - - Google Patents
Info
- Publication number
- JPS6261861B2 JPS6261861B2 JP15887380A JP15887380A JPS6261861B2 JP S6261861 B2 JPS6261861 B2 JP S6261861B2 JP 15887380 A JP15887380 A JP 15887380A JP 15887380 A JP15887380 A JP 15887380A JP S6261861 B2 JPS6261861 B2 JP S6261861B2
- Authority
- JP
- Japan
- Prior art keywords
- dryer
- steam
- boiler
- lignite
- heat
- 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.)
- Expired
Links
- 238000010438 heat treatment Methods 0.000 claims description 27
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 17
- 238000001035 drying Methods 0.000 claims description 12
- 238000000034 method Methods 0.000 claims description 10
- 239000005416 organic matter Substances 0.000 claims description 9
- 238000010248 power generation Methods 0.000 claims description 6
- 230000003134 recirculating effect Effects 0.000 claims 1
- 239000003077 lignite Substances 0.000 description 24
- 239000007789 gas Substances 0.000 description 18
- 239000012530 fluid Substances 0.000 description 9
- 239000003245 coal Substances 0.000 description 7
- 238000011084 recovery Methods 0.000 description 7
- 238000002485 combustion reaction Methods 0.000 description 6
- 230000005611 electricity Effects 0.000 description 5
- 239000010802 sludge Substances 0.000 description 5
- 238000009833 condensation Methods 0.000 description 4
- 230000005494 condensation Effects 0.000 description 4
- 238000001704 evaporation Methods 0.000 description 3
- 230000008020 evaporation Effects 0.000 description 3
- 229910052799 carbon Inorganic materials 0.000 description 2
- 239000000428 dust Substances 0.000 description 2
- 239000011368 organic material Substances 0.000 description 2
- 239000002028 Biomass Substances 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 240000007594 Oryza sativa Species 0.000 description 1
- 235000007164 Oryza sativa Nutrition 0.000 description 1
- 239000013064 chemical raw material Substances 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000009841 combustion method Methods 0.000 description 1
- 238000011109 contamination Methods 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000010981 drying operation Methods 0.000 description 1
- 239000004744 fabric Substances 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000010903 husk Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 235000019645 odor Nutrition 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 235000009566 rice Nutrition 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 239000004449 solid propellant Substances 0.000 description 1
- 239000010902 straw Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
- 239000002023 wood Substances 0.000 description 1
Landscapes
- Drying Of Solid Materials (AREA)
- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
Description
【発明の詳細な説明】
本発明は間接加熱乾燥機を有効に利用して発電
を行う含水有機物の乾燥方法に関する。DETAILED DESCRIPTION OF THE INVENTION The present invention relates to a method for drying water-containing organic matter that effectively utilizes an indirect heating dryer to generate electricity.
本発明にいう、含水有機物とは、廃水処理後の
汚泥のみならず、地下資源としての石炭、代表的
例としては褐炭、またバイオマス（生物体）とし
ての有機物、代表例としてバカス、木材、藁、も
みがら、木の皮等の有機物の含水物も含まれる意
である。以下褐炭について説明を進めるが、その
思想を汲みすれば、本発明は、他の有機物にも適
用できることは明白であろう。 In the present invention, water-containing organic matter refers to not only sludge after wastewater treatment, but also coal as an underground resource, typically lignite, and organic matter as biomass (organisms), typical examples being bacas, wood, and straw. It also includes hydrated organic matter such as rice husks, tree bark, etc. The description below will be made regarding lignite, but if the concept is taken into account, it will be obvious that the present invention can be applied to other organic substances.
褐炭の種類はきわめて多く、炭素と水素との比
によつてその性質が変わる。また褐炭のうちには
大量の水分を含む褐炭があるが、これを液化して
化学原料とする場合には、反応にあずからない水
を除去する必要がある。さらに、これを燃料とし
て利用する場合にも、予め水分を除去して燃焼す
れば、熱効率の寄与となる。これらの目的達成の
ため、従来一般に実施されている褐炭の乾燥ある
いは脱水法としては、高圧蒸気を用いてオートク
レーブ中に褐炭を装入し、熱処理を行い、褐炭の
物理的構造を変化させて水分を絞り出す方法があ
る。この方法では、必要熱量が後述する間接加熱
よりも少いことが知られているが、高温高圧の良
質の蒸気を発生させてこれを直接利用することが
できず、また熱処理後の装置より回収できる蒸気
量が少いため、全体的な熱利用効率が低い。 There are many types of brown coal, and its properties change depending on the ratio of carbon to hydrogen. Some lignite coals contain a large amount of water, but when liquefied and used as a chemical raw material, it is necessary to remove the water that does not participate in the reaction. Furthermore, even when using this as a fuel, if moisture is removed before combustion, it will contribute to thermal efficiency. To achieve these objectives, the conventional lignite drying or dehydration method involves charging lignite into an autoclave using high-pressure steam, heat-treating it, and changing the physical structure of the lignite to remove moisture. There is a way to squeeze it out. It is known that this method requires less heat than indirect heating, which will be described later, but it is not possible to generate high-temperature, high-pressure, high-quality steam and use it directly, and it cannot be recovered from equipment after heat treatment. Since the amount of steam produced is small, the overall heat utilization efficiency is low.
他方、回転式乾燥機に多数の加熱管を挿入し、
加熱蒸気を導入し、間接加熱によつて褐炭を加熱
し水分を蒸発させるものがある。この場合、乾燥
炭の一部をボイラーに供給してボイラーの熱効率
を向上させることは可能であるが、乾燥機からの
排気の中には、空気が含まれているところから、
蒸気の凝縮温度は一般に80℃前後で、再利用は困
難である。 On the other hand, by inserting a large number of heating tubes into a rotary dryer,
There is one that introduces heated steam and indirectly heats lignite to evaporate water. In this case, it is possible to improve the thermal efficiency of the boiler by supplying some of the dry coal to the boiler, but since the exhaust air from the dryer contains air,
The condensation temperature of steam is generally around 80°C, making reuse difficult.
本発明はかかる従来法の問題点を踏えつつ開発
されたもので、その目的は褐炭等の含水有機物そ
れ自体の乾燥のみならず、乾燥時に蒸発した水分
を含有する乾燥排気ガスの凝縮温度を不凝縮性ガ
スの混入を避け、かつ乾燥機を間接加熱型としま
た過熱水蒸気を循環することで上昇させ発電用と
して利用し、また乾燥有機物の燃焼による熱を高
圧蒸気として回収して発電用として利用し、ター
ビン排蒸気は前記乾燥へ送り二重効用的な発電を
行うようになし、もつて全体としてきわめて優れ
た熱効率を与える乾燥法を提供することにある。 The present invention was developed taking into consideration the problems of the conventional method, and its purpose is not only to dry the water-containing organic matter itself such as lignite, but also to reduce the condensation temperature of the dry exhaust gas containing the moisture evaporated during drying. In order to avoid contamination with non-condensable gases, the dryer is an indirect heating type, and the superheated steam is circulated to raise the temperature and used for power generation.The heat from the combustion of dry organic matter is recovered as high pressure steam and used for power generation. The object of the present invention is to provide a drying method in which the turbine exhaust steam is sent to the dryer to generate double-effect power, thereby providing extremely excellent thermal efficiency as a whole.
以下本発明を褐炭の乾燥を例にとつた図面に示
す具体例によつて説明すると、１は間接加熱部１
ａを有する間接加熱乾燥機で、これに含水褐炭２
が供給される。間接加熱部１ａには過熱蒸気が通
される。これによつて、含水褐炭２の乾燥が図ら
れるとともに、排気ガスがダクト３を介してサイ
クロン４およびその後バツグフイルター５に通さ
れ、除塵後、蒸発器７に導かれる。蒸発器７には
フロンＲ−114等の作動流体が通る循環路８が構
成されており、排気ガスが蒸発器７を通り排出管
９へ排出される際、蒸発器７へ流入する凝縮状態
の作動流体の蒸発が行なわれる。この蒸発した作
動流体は、タービン１０に至り、膨張時の回転力
により発電機１１を回す。その後、作動流体はコ
ンデンサー１２において凝縮せられ、ポンプ６に
より再び蒸発器７へ循環される。 The present invention will be explained below with reference to a specific example shown in the drawings taking drying of lignite as an example.
In an indirect heating dryer with a
is supplied. Superheated steam is passed through the indirect heating section 1a. As a result, the hydrous lignite 2 is dried, and the exhaust gas is passed through the duct 3 to the cyclone 4 and then to the bag filter 5, and after removing dust, is led to the evaporator 7. The evaporator 7 has a circulation path 8 through which a working fluid such as Freon R-114 passes, and when exhaust gas passes through the evaporator 7 and is discharged to the exhaust pipe 9, the condensed state flowing into the evaporator 7 Evaporation of the working fluid takes place. This evaporated working fluid reaches the turbine 10 and rotates the generator 11 by the rotational force during expansion. The working fluid is then condensed in the condenser 12 and circulated again to the evaporator 7 by the pump 6.
他方、排気ガスはダクト１３を介して循環ブロ
ワ１４によりガス加熱用ボイラー１５に送られ、
後述する過熱蒸気の熱を受けて加熱せられた後、
ダクト１６を通して間接加熱乾燥機１へ循環され
る構成となつている。 On the other hand, the exhaust gas is sent to a gas heating boiler 15 via a duct 13 by a circulation blower 14,
After being heated by the heat of superheated steam described later,
It is configured to be circulated to the indirect heating dryer 1 through a duct 16.
また間接加熱乾燥機１において乾燥された乾燥
褐炭は供給路１７を通して燃焼ボイラー１８へ供
給される。この際、サイクロン４およびバツグフ
イルター５において分離された微粉褐炭もそれぞ
れ供給路１９，２０を介してボイラー１８へ供給
される。ボイラー１８へ供給された乾燥褐炭は燃
焼された後、そのダストは排出路２１を通して排
出される。 Further, the dry lignite dried in the indirect heating dryer 1 is supplied to a combustion boiler 18 through a supply path 17. At this time, the pulverized lignite separated in the cyclone 4 and bag filter 5 is also supplied to the boiler 18 via supply paths 19 and 20, respectively. After the dry lignite supplied to the boiler 18 is burned, its dust is discharged through the discharge passage 21.
このボイラー１８には熱回収部２２が設けられ
ており、ボイラ水供給ポンプ２３によりボイラ水
が供給される。ボイラ水は熱回収部２２におい
て、ボイラー１８における発生熱を吸収しドラム
２４を通して更に熱回収部２２ａを通り過熱され
てタービン２５へ至る。タービン２５では膨張時
の回転力により発電機２６を回した後、過熱蒸気
が循環路２８を通して間接加熱部１ａへと送られ
る。この返送過熱蒸気の一部は、先に述べたよう
に、分岐路２９によりガス加熱用ボイラー１５に
与えられた後、熱回収部２２へと再循環される。
さらに間接加熱部１ａに与えられた過熱蒸気は、
含水褐炭を乾燥させた後、送給路３０を介してボ
イラー１８の熱回収部２２へ送給される。３１は
乾燥褐炭の一部を排出するための排出路である。 This boiler 18 is provided with a heat recovery section 22 and is supplied with boiler water by a boiler water supply pump 23. In the heat recovery section 22, the boiler water absorbs the heat generated in the boiler 18, passes through the drum 24, and further passes through the heat recovery section 22a, where it is superheated and reaches the turbine 25. In the turbine 25, after rotating a generator 26 by the rotational force during expansion, the superheated steam is sent to the indirect heating section 1a through the circulation path 28. A portion of this returned superheated steam is given to the gas heating boiler 15 through the branch path 29, and then is recirculated to the heat recovery section 22, as described above.
Furthermore, the superheated steam given to the indirect heating section 1a is
After drying the hydrous lignite, it is sent to the heat recovery section 22 of the boiler 18 via the feed path 30. 31 is a discharge path for discharging a portion of the dry lignite.
このような方法を採ると、含水褐炭の乾燥に際
し、間接加熱乾燥機１を用いているので、排気ガ
ス中の蒸発水分の凝縮温度を高めることができ
る。そして間接加熱乾燥機１を用いることと相俟
つて、排気ガスは循環再使用しているから、乾燥
機１内を通過する非凝縮性ガスの量は凝縮する含
水褐炭からの蒸発水分に比較して極力少くでき、
ある場合には非凝縮性ガスのない過熱蒸気とでき
る。その結果、高い凝縮温度の排気ガスが得ら
れ、この排気ガスによつて、作動流体と熱交換さ
せることによつて、高い圧力で蒸発する作動流体
が得られ、十分発電用として用いることができ
る。なお、本プロセスで系外に排出されるのは主
として凝縮水であり、非凝縮ガスがあつたとして
も僅かであるから、汚泥の乾燥などを図る場合の
悪臭対策はきわめて容易である。 When such a method is adopted, since the indirect heating dryer 1 is used when drying the hydrous lignite, the condensation temperature of the evaporated water in the exhaust gas can be increased. In addition to using the indirect heating dryer 1, the exhaust gas is recycled and reused, so the amount of non-condensable gas passing through the dryer 1 is compared to the evaporated water from the condensed hydrous lignite. can be done as little as possible,
In some cases, it can be superheated steam without non-condensable gases. As a result, exhaust gas with a high condensation temperature is obtained, and by exchanging heat with the working fluid, a working fluid that evaporates at high pressure is obtained, which can be used for power generation. . Note that in this process, mainly condensed water is discharged outside the system, and only a small amount of non-condensed gas is present, so it is extremely easy to take measures against bad odors when drying sludge.
一方、ボイラー１８には乾燥した水分の少い褐
炭が供給されるので、燃焼効率が高い、そして、
もし汚泥を対象とする場合でも、汚泥の発熱量は
小さいが、乾燥汚泥は石炭のような固形燃料とし
ての取扱を行うことができるため、燃焼手段とし
て、微粉炭燃焼炉、ロストル付の石炭ボイラーあ
るいは流動ボイラーのような、単位体積当りの熱
容量の高いものを用いることができるから、安価
な設備で足り、かつ熱回収を容易に行うことがで
きる。またボイラー１８では水蒸気を過熱蒸気と
することができる程、高温操作ができるから、そ
の過熱蒸気によつてタービン２５による発電を行
うことができる。ここでタービン３２の排気温度
はほぼ120〜150℃程度で低い温度である。もし乾
燥機として直接加熱式のものを採用し、タービン
からの排気を乾燥用空気の加温用として用いたと
しても、高い加熱用空気温度は得られず、水分の
多い含水有機物を乾燥させるには大量の空気が必
要となるばかりでなく、熱効率も悪い。ところ
が、幸いに温度は低いが大きな顕熱を有する水蒸
気であるからして、これを間接加熱式の乾燥機に
導けば、約90％程度の熱効率を得ることができ
る。 On the other hand, since the boiler 18 is supplied with dry brown coal with low moisture content, combustion efficiency is high, and
Even if the target is sludge, the calorific value of sludge is small, but dried sludge can be treated as a solid fuel like coal, so as a combustion method, a pulverized coal combustion furnace or a coal boiler with a rostol is used. Alternatively, a fluid boiler with a high heat capacity per unit volume can be used, so that inexpensive equipment is sufficient and heat can be easily recovered. Further, since the boiler 18 can operate at a high temperature enough to turn water vapor into superheated steam, the turbine 25 can generate electricity using the superheated steam. Here, the exhaust gas temperature of the turbine 32 is low, approximately 120 to 150°C. Even if a direct heating type dryer is adopted and the exhaust air from the turbine is used to heat the drying air, a high heating air temperature cannot be obtained, making it difficult to dry hydrated organic materials with a high moisture content. Not only does it require a large amount of air, but it also has poor thermal efficiency. Fortunately, however, water vapor has a low temperature but a large amount of sensible heat, and if this is led to an indirect heating type dryer, a thermal efficiency of about 90% can be achieved.
なお、本発明において用いることができる間接
加熱乾燥機としては、加熱面内蔵型流動層乾燥
機、加熱管内蔵型回転式乾燥機、または加熱板回
転型乾燥機等がある。 Indirect heating dryers that can be used in the present invention include a fluidized bed dryer with a built-in heating surface, a rotary dryer with a built-in heating tube, a rotary dryer with a hot plate, and the like.
以上の通り、本発明によれば、含水有機物の乾
燥熱および燃焼熱を利用し、高い発電効率をもつ
た発電を行うことができるとともに、プロセス全
体の熱効率がきわめて高くなる。 As described above, according to the present invention, it is possible to generate power with high power generation efficiency by using the drying heat and combustion heat of a hydrous organic material, and the thermal efficiency of the entire process is extremely high.
次に実施例を示す。 Next, examples will be shown.
実施例
本例は、水分含水量62.5％の豪州産褐炭
5.6Ton／hrを水分10％にまで乾燥する設備につ
いての例である。Example This example uses Australian lignite with a moisture content of 62.5%.
This is an example of equipment that dries 5.6Ton/hr to a moisture content of 10%.
用いた乾燥機は、内部に全伝熱面積378m2を内
蔵する断面2.4ｍ×5.0ｍ、高さ６ｍの流動層式乾
燥機で、サイクロンは、直径1.5ｍ×全高３ｍの
大きさのものを２基用い、過面積300m2の耐熱
性過布を用いたバツグフイルターを設け、循環
用ブロワとしては、720Nm3／min、吐出圧力400
mm水柱、40Kw電動機駆動とし、循環蒸気過熱器
としては455m2の伝熱面積を持つた多管式を採用
した。乾燥ベーパよりの動力回収システムには作
動流体としてフロンＲ−114を用い伝熱面積86m2
の水平管式蒸発缶を用いて、膨張タービンには軸
流式を用い、200Kwの発電機を取付けた。 The dryer used was a fluidized bed dryer with a cross section of 2.4 m x 5.0 m and a height of 6 m, with a total heat transfer area of 378 m2 , and the cyclone was 1.5 m in diameter x 3 m in total height. Two blowers are used, equipped with a bag filter using heat-resistant cloth with an over area of 300 m 2 , and a circulation blower of 720 Nm 3 /min and a discharge pressure of 400 m 2 .
mm water column, driven by a 40Kw electric motor, and a multi-tube type circulating steam superheater with a heat transfer area of 455m2 was adopted. The power recovery system from dry vapor uses Freon R-114 as the working fluid and has a heat transfer area of 86 m 2
A horizontal tube type evaporator was used, an axial flow type was used for the expansion turbine, and a 200Kw generator was installed.
一方、乾燥炭を燃焼させるボイラは乾燥褐炭を
最大2.6Ton／hrまで処理できる蒸発量30Ton／
hr、蒸気圧力16Kg／cm2gageの微粉炭燃焼ボイラ
ーであり、本装置では発電の必要がないので乾燥
炭全量を燃焼させた。 On the other hand, a boiler that burns dry coal can process dry lignite up to 2.6Ton/hr with an evaporation rate of 30Ton/hr.
This is a pulverized coal-fired boiler with a steam pressure of 16 kg/cm 2 gage, and since there is no need to generate electricity with this equipment, all dry coal was burned.
前記あらかじめ0.2〜1.5mmの粒子である原料の
褐炭は水分62.5％、25℃で5550Kg／hrの割合で大
気圧下で運転されて流動乾燥機へ送られる。乾燥
機内の加熱器には150℃の蒸気によつて加温され
ており、同時に下部より145℃の過熱水蒸気が送
られて流入する原料を流動層内で分散し、褐炭は
内部の加熱器と接触し、はげしい熱移動が起る。
この際ガスに同伴して乾燥機外へ持出されるもの
は殆んど乾燥しており、サイクロンとバツグフイ
ルタにより捕集され、乾燥機より連続的に取り出
される乾燥褐炭と合流して乾燥品として処理され
る。この水分は８〜10％、排出量は約2300Kg／hr
であつた。 The raw brown coal, which is in the form of particles of 0.2 to 1.5 mm, has a moisture content of 62.5%, is operated at a rate of 5550 kg/hr at 25° C. under atmospheric pressure, and is sent to a fluidized fluidized dryer. The heater inside the dryer is heated by steam at 150℃, and at the same time superheated steam at 145℃ is sent from the bottom to disperse the incoming raw material in the fluidized bed. contact and intense heat transfer occurs.
At this time, most of the material taken out of the dryer along with the gas is dry, and is collected by a cyclone and bag filter, combined with the dry lignite that is continuously taken out from the dryer, and processed as a dry product. be done. This water content is 8-10%, and the discharge amount is approximately 2300Kg/hr.
It was hot.
この乾燥操作の条件は加熱水蒸気の供給量が
3570Kg／hr、層内の温度が115℃、出口ガス温度
が120℃、乾燥品の温度が115℃〜116℃、循環ガ
スの流量が720Nm3／minとした。一方、排気すべ
き過熱蒸気は、乾燥機内の圧力を見ながら約3200
〜3300Kg／hrの割合で抜出して、フロンＲ−114
の蒸発器へ送り、蒸発温度85℃、圧力24Kg／cm2
gageでＲ−114を54400Kg／hrの割合で蒸発させ
て、膨張タービンに送り、発電機を動かして、
140Kwhrの発電量を得た。 The conditions for this drying operation are that the amount of heated steam supplied is
The temperature in the bed was 115°C, the outlet gas temperature was 120°C, the temperature of the dried product was 115°C to 116°C, and the flow rate of circulating gas was 720Nm 3 /min. On the other hand, the superheated steam that should be exhausted is approximately 3,200 yen while checking the pressure inside the dryer.
Freon R-114 is extracted at a rate of ~3300Kg/hr.
evaporator, evaporation temperature 85℃, pressure 24Kg/cm 2
evaporate R-114 at a rate of 54400Kg/hr in a gage, send it to an expansion turbine, run a generator,
A power generation amount of 140Kwhr was obtained.
なお、本システムで乾燥された褐炭は前記ボイ
ラに供給し、16Kg／cm2gageの飽和蒸気を22Ton／
hr得た。本実験装置では発生蒸気による発電を実
施しなかつたがもし過熱蒸気を発生させた場合に
は、約2000Kwhr程度の発電が可能であり、その
排蒸気は乾燥機およびプロセスに利用できる。 The lignite dried in this system is supplied to the boiler, which generates saturated steam of 16Kg/cm 2 gage at 22T/22T/cm2.
Got hr. Although this experimental device did not generate electricity using generated steam, if superheated steam was generated, it would be possible to generate approximately 2000Kwhr of electricity, and the exhaust steam could be used for the dryer and process.
図面は本発明法の一例を示すフローシートであ
る。
１……間接加熱乾燥機、１ａ……間接加熱部、
７……蒸発器、８……作動流体循環路、１０……
タービン、１１……発電機、１２……ガス加熱用
ボイラー、１７……供給路、１８……ボイラー、
２２……熱回収部、２５……タービン、２６……
発電機。
The drawing is a flow sheet showing an example of the method of the present invention. 1... Indirect heating dryer, 1a... Indirect heating section,
7... Evaporator, 8... Working fluid circulation path, 10...
Turbine, 11... Generator, 12... Gas heating boiler, 17... Supply path, 18... Boiler,
22... Heat recovery section, 25... Turbine, 26...
Generator.
Claims (1)
接加熱乾燥機へ含水有機物を供給して乾燥させ、
この乾燥に伴う排気ガスの熱を利用して発電を行
い、前記乾燥機により乾燥された乾燥有機物を燃
焼させ、蒸気を発生させ、この蒸気を利用して発
電を行い、発電後の蒸気を前記間接加熱部へ再循
環させることを特徴とする含水有機物の乾燥方
法。1 Supply and dry the hydrated organic matter to an indirect heating dryer having an indirect heating section in which superheated steam circulates,
The heat of the exhaust gas accompanying this drying is used to generate power, the dry organic matter dried by the dryer is combusted, steam is generated, this steam is used to generate power, and the steam after power generation is A method for drying water-containing organic matter, characterized by recirculating it to an indirect heating section.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP15887380A JPS5782683A (en) | 1980-11-13 | 1980-11-13 | Drying of water containing organic matter |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP15887380A JPS5782683A (en) | 1980-11-13 | 1980-11-13 | Drying of water containing organic matter |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS5782683A JPS5782683A (en) | 1982-05-24 |
| JPS6261861B2 true JPS6261861B2 (en) | 1987-12-23 |
Family
ID=15681261
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP15887380A Granted JPS5782683A (en) | 1980-11-13 | 1980-11-13 | Drying of water containing organic matter |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS5782683A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH0546555U (en) * | 1991-11-29 | 1993-06-22 | スズキ株式会社 | Seat knob structure |
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|---|---|---|---|---|
| US8523963B2 (en) * | 2004-10-12 | 2013-09-03 | Great River Energy | Apparatus for heat treatment of particulate materials |
| JP2010255557A (en) * | 2009-04-27 | 2010-11-11 | Minoru Morita | Power generation method using exhaust gas from conductive heat transfer dryer and drying facility having power generation function |
| JP5325023B2 (en) | 2009-05-28 | 2013-10-23 | 三菱重工業株式会社 | Apparatus and method for drying hydrous solid fuel |
| JP2011163628A (en) * | 2010-02-08 | 2011-08-25 | Mitsubishi Heavy Ind Ltd | Method and device for drying wet material |
| JP5473732B2 (en) * | 2010-04-02 | 2014-04-16 | 三菱重工業株式会社 | Low grade coal drying system |
| JP5473734B2 (en) * | 2010-04-02 | 2014-04-16 | 三菱重工業株式会社 | Low grade coal drying system |
| JP2011214817A (en) * | 2010-04-02 | 2011-10-27 | Mitsubishi Heavy Ind Ltd | Fluidized bed drying device and fluidized bed drying facility |
| JP5634100B2 (en) * | 2010-04-02 | 2014-12-03 | 三菱重工業株式会社 | Fluidized bed drying apparatus and fluidized bed drying equipment |
| JP5682917B2 (en) * | 2011-01-12 | 2015-03-11 | 一般財団法人電力中央研究所 | Brown coal drying method and drying system |
| JP5511702B2 (en) * | 2011-01-28 | 2014-06-04 | 三菱重工業株式会社 | Hydrous solid fuel drying equipment |
| AU2011373344B2 (en) * | 2011-07-15 | 2015-06-11 | Mitsubishi Heavy Industries, Ltd. | Fluidized bed drying facility |
| JP6613746B2 (en) * | 2015-09-14 | 2019-12-04 | 株式会社Ｉｈｉ | Drying system |
| JP6159383B2 (en) * | 2015-12-25 | 2017-07-05 | 公益財団法人日本下水道新技術機構 | Sewage sludge drying system |
-
1980
- 1980-11-13 JP JP15887380A patent/JPS5782683A/en active Granted
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH0546555U (en) * | 1991-11-29 | 1993-06-22 | スズキ株式会社 | Seat knob structure |
Also Published As
| Publication number | Publication date |
|---|---|
| JPS5782683A (en) | 1982-05-24 |
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