JPS62102899A - Drying method for organic sludge - Google Patents
Drying method for organic sludgeInfo
- Publication number
- JPS62102899A JPS62102899A JP60241283A JP24128385A JPS62102899A JP S62102899 A JPS62102899 A JP S62102899A JP 60241283 A JP60241283 A JP 60241283A JP 24128385 A JP24128385 A JP 24128385A JP S62102899 A JPS62102899 A JP S62102899A
- Authority
- JP
- Japan
- Prior art keywords
- drying
- air
- sludge
- hot air
- sewage
- 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
- 239000010802 sludge Substances 0.000 title claims abstract description 36
- 238000001035 drying Methods 0.000 title claims abstract description 35
- 238000005273 aeration Methods 0.000 claims abstract description 21
- 239000010865 sewage Substances 0.000 claims abstract description 11
- 238000007602 hot air drying Methods 0.000 claims abstract description 7
- 239000000463 material Substances 0.000 claims abstract description 4
- 238000000034 method Methods 0.000 claims description 14
- 238000005469 granulation Methods 0.000 claims description 6
- 230000003179 granulation Effects 0.000 claims description 6
- 239000002351 wastewater Substances 0.000 abstract description 7
- 238000004332 deodorization Methods 0.000 abstract description 5
- 239000002912 waste gas Substances 0.000 abstract 3
- 235000019645 odor Nutrition 0.000 abstract 1
- 238000005453 pelletization Methods 0.000 abstract 1
- 239000007789 gas Substances 0.000 description 15
- 230000001877 deodorizing effect Effects 0.000 description 8
- 238000009423 ventilation Methods 0.000 description 6
- 239000000428 dust Substances 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 239000000446 fuel Substances 0.000 description 3
- 239000008188 pellet Substances 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- 238000007906 compression Methods 0.000 description 2
- 230000006835 compression Effects 0.000 description 2
- 230000018044 dehydration Effects 0.000 description 2
- 238000006297 dehydration reaction Methods 0.000 description 2
- 238000010790 dilution Methods 0.000 description 2
- 239000012895 dilution Substances 0.000 description 2
- 239000010800 human waste Substances 0.000 description 2
- 238000004062 sedimentation Methods 0.000 description 2
- 206010011224 Cough Diseases 0.000 description 1
- 238000005276 aerator Methods 0.000 description 1
- 238000007605 air drying Methods 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000003337 fertilizer Substances 0.000 description 1
- 239000010842 industrial wastewater Substances 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 244000005700 microbiome Species 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 230000035699 permeability Effects 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000004449 solid propellant Substances 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/10—Biological treatment of water, waste water, or sewage
Landscapes
- Drying Of Solid Materials (AREA)
- Activated Sludge Processes (AREA)
- Treatment Of Sludge (AREA)
Abstract
Description
【発明の詳細な説明】
〔産業上の利用分野〕
本発明は、下水、し尿、各種産業廃水などの有機性lり
水処理において発生する有機性汚泥(殿集沈殴汚泥を含
む)の脱水ケーキを、極めて合理的かつ省エネルギー的
に乾燥する方法に関するものである。[Detailed Description of the Invention] [Field of Industrial Application] The present invention is directed to the dewatering of organic sludge (including sludge and sedimentation) generated in the treatment of organic sewage such as sewage, human waste, and various industrial wastewater. The present invention relates to a method of drying a cake in an extremely rational and energy-saving manner.
(従来の技術〕
有機性汚泥は、脱水−乾燥−焼却という直列プロセスで
処分されるのが代表的かつ一般的な方法である。(Prior Art) A typical and common method is to dispose of organic sludge through a serial process of dehydration, drying, and incineration.
しかし、を機性汚泥は脱水性が悪く、脱水ケーキの水分
が75〜85熟程度と高いため、乾燥、焼却する際に多
量の燃料を必要とするほかに、排出される乾燥排ガスの
脱臭処理のために脱臭設備と高額の脱臭コストを必要と
するという欠点があり、特に後続する焼却工程は乾燥の
良否に左右されるところから、乾燥をいかに効果的、合
理的に行うかがキーポイントになっている。However, organic sludge has poor dehydration properties, and the moisture content of the dehydrated cake is as high as 75-85%, so in addition to requiring a large amount of fuel when drying and incinerating it, it also requires deodorizing treatment of the dried exhaust gas. The drawback is that it requires deodorizing equipment and high deodorizing costs, and the key point is how effectively and rationally drying can be carried out, especially since the subsequent incineration process depends on the quality of drying. It has become.
このように、従来技術においては、低水分の乾燥物を得
るためには多量の燃料を必要とし、またその乾燥排ガス
の悪臭に対する脱臭設備を必要とするという、重大な問
題点をかかえている。As described above, the prior art has serious problems in that it requires a large amount of fuel to obtain a dry product with low moisture content, and also requires deodorizing equipment to deal with the foul odor of the dried exhaust gas.
本発明は、有機性汚泥の脱水ケーキの乾燥を、予備乾燥
と仕上げ乾燥の2段に分割して、効果的、かつ合理的な
乾燥を行い、さらに乾燥排ガスの脱千のため、の経費を
完全に不要にしようとするものである。The present invention divides the drying of a dehydrated cake of organic sludge into two stages, pre-drying and final drying, to perform effective and rational drying, and further reduce the cost of removing drying exhaust gas. The idea is to make it completely unnecessary.
本発明は、有機性汚泥の脱水ケーキを熱風乾燥し、咳熱
風乾壜工程からの乾燥排ガスを汚水の生物処理用の曝気
ブロワ−の吸引空気に混合し、該ブロワ−の吐出空気を
前記熱風乾燥工程から排出された乾燥物に直接接触せし
めてさらに乾燥したのち汚水の生物処理に使用すること
を特徴とする有機性汚泥の乾燥方法十ある。The present invention involves drying a dehydrated cake of organic sludge with hot air, mixing the dry exhaust gas from the cough hot air bottle drying process with the suction air of an aeration blower for biological treatment of sewage, and using the discharge air of the blower with the hot air. There are ten methods for drying organic sludge, which are characterized in that they are brought into direct contact with the dried material discharged from the drying process, further dried, and then used for biological treatment of sewage.
本発明の作用を、その一実施態様を示す図面を参照しな
がら説明すれば、水分75〜85%程度に脱水された有
機性汚泥の脱水ケーキ1は、密閉型の第1熱風乾燥機2
に供給され、温度200〜800℃の熱風3によって乾
燥され、水分40〜50%程度の乾燥汚泥4となって排
出される。また、第1熱風乾燥機2から排出される乾燥
排ガス5 (悪臭がある)は、サイクロンなどの除しん
器6を経由して、汚水の生物処理のためにエアレーショ
ン用空気を供給する曝気ブロワ−7が設置された設置室
8内に導入され、曝気ブロワ−7は吸引空気9中に乾燥
排ガス5を混合して共に吸引して圧縮し、断熱圧縮によ
って吸引する気体の温度よりも50℃程度昇温した吐出
空気10となる。To explain the operation of the present invention with reference to a drawing showing one embodiment thereof, a dehydrated cake 1 of organic sludge dehydrated to about 75 to 85% moisture is dried in a closed first hot air dryer 2.
The sludge is dried by hot air 3 at a temperature of 200 to 800°C, and is discharged as dried sludge 4 with a water content of about 40 to 50%. In addition, the dry exhaust gas 5 (which has a bad odor) discharged from the first hot air dryer 2 is passed through a dust remover 6 such as a cyclone to an aeration blower that supplies aeration air for biological treatment of wastewater. The aeration blower 7 mixes the dry exhaust gas 5 into the suction air 9, sucks it together and compresses it, and uses adiabatic compression to lower the temperature by about 50 degrees Celsius than the temperature of the gas to be sucked. The discharged air 10 becomes heated.
一方、第1熱風乾燥機2から排出された乾燥汚泥4は、
第2段目の密閉型の通気乾燥器11の上部から供給され
て通気乾燥器11内に充填層12を形成し、この充填1
1112の下部から前述の曝気ブロワ−7の吐出空気1
0を上向流にて通気し、充填層12を形成している汚泥
中の水分を吐出空気10の保有する熱によって蒸発、除
去し、仕上げ乾燥が行われる。この仕上げ乾燥された最
終乾燥lη泥13は、曝気ブロワ−7の吐出空気10に
よって高度に乾燥されており、回分的又は連続的に通気
乾燥器11から取り出され、固形燃料もしくは肥料とし
て有効利用される。On the other hand, the dried sludge 4 discharged from the first hot air dryer 2 is
It is supplied from the upper part of the second stage closed type aerated dryer 11 to form a packed layer 12 in the aerated dryer 11.
The discharge air 1 of the aeration blower 7 mentioned above from the lower part of 1112
0 is aerated in an upward flow, water in the sludge forming the packed bed 12 is evaporated and removed by the heat possessed by the discharged air 10, and final drying is performed. This final dried lη mud 13 is highly dried by the discharge air 10 of the aeration blower 7, is taken out from the aeration dryer 11 in batches or continuously, and is effectively used as solid fuel or fertilizer. Ru.
このようにして、乾燥汚泥4の充填層12中の水分を蒸
発させ、熱が消費されて冷却し通気乾燥器11から排出
される排出空気14は、圧力をほとんど失っておらず、
汚水15を受入れる生物処理槽16内の散気器17に供
給され、エアレーンヨン空気として槽16内で噴出され
る。In this way, the moisture in the packed bed 12 of the dried sludge 4 is evaporated, the heat is consumed, the discharged air 14 is cooled and discharged from the ventilation dryer 11, and has almost no pressure loss.
The wastewater 15 is supplied to an aerator 17 in a biological treatment tank 16 that receives the wastewater 15, and is blown out within the tank 16 as air lane air.
なお、曝気ブロワ−7の吐出空気10の配管が通気乾燥
器11に連絡する部分は、保温施工をすることが好まし
く、特に配管が屋外に露出している場合には、雨雪等に
よって著しく冷却されてしまうために一1雨雪等が直接
配管に接触しないようにカバーを設けるとよい。また生
物処理槽16内の散気器17は、ダストによる目詰まり
を防くために、ディフェーザーなどのノンクロッグタイ
プのものを用いるのが好ましい。In addition, it is preferable to insulate the part where the piping for the discharged air 10 of the aeration blower 7 connects to the ventilation dryer 11, and especially if the piping is exposed outdoors, it will not cool down significantly due to rain, snow, etc. It is a good idea to install a cover to prevent rain and snow from coming into direct contact with the pipes. Further, it is preferable to use a non-clog type diffuser such as a diffuser for the diffuser 17 in the biological treatment tank 16 in order to prevent clogging due to dust.
なお、前段の乾燥を行うための第1熱風乾燥機2として
は、各種タイプのものを使用することができるが、攪拌
流動層による連続造粒乾燥機を使用することが°好まし
く、その場合には球形ペレ。Although various types of first hot air dryer 2 can be used for drying the first stage, it is preferable to use a continuous granulation dryer using an agitated fluidized bed. is a spherical Pele.
ト状の水分40〜50%の乾燥汚泥4を得ることができ
るから、第2段目の曝気ブロワ−7による通気゛乾燥器
11において極めて通気性の良い充填層12を形成でき
るばかりでなく、球形ペレット状のために流動性が良好
で、通気乾燥器ll内でのブリッジングに起因する乾燥
物の排出不能トラブルが発生しない。Since dry sludge 4 having a moisture content of 40 to 50% can be obtained in the form of a sheet, not only can a packed bed 12 with extremely good air permeability be formed in the aerated dryer 11 by the second stage aeration blower 7, but also Since it is in the form of spherical pellets, it has good fluidity, and there is no problem of not being able to discharge the dried material due to bridging in the ventilation dryer.
以上述べた本発明の技術的思想の骨子は次の通りである
。The gist of the technical idea of the present invention described above is as follows.
即ち、第1熱風乾燥機2に攪拌流動層による造粒乾燥機
を使用した場合の乾燥排ガス5の温度は、供給する熱風
3の温度(200〜800℃)に対応する湿球温度(5
0〜75°C)を示すので、曝気ブロワ−7の吸引空気
9に混合することによって、吸引空気9の温度を高める
ことが可能となる。That is, when a granulation dryer using an agitated fluidized bed is used as the first hot air dryer 2, the temperature of the dry exhaust gas 5 is the wet bulb temperature (5
0 to 75°C), therefore, by mixing it with the suction air 9 of the aeration blower 7, it becomes possible to increase the temperature of the suction air 9.
したがって、単に吸引空気9 (外気)のみを吸引して
曝気ブロワ−で断熱圧縮する場合よりも高温度の吐出空
気10を得ることができ、この結果、通気乾燥器11に
おいて乾燥に利用される熱量が増加し、より低水分の最
終乾燥汚泥13を得ることができる。Therefore, it is possible to obtain discharge air 10 with a higher temperature than when only suction air 9 (outside air) is sucked in and adiabatically compressed using an aeration blower, and as a result, the amount of heat used for drying in the ventilation dryer 11 is increases, and a final dried sludge 13 with lower moisture content can be obtained.
さらにまた、有機性汚泥の脱水ケーキを熱風乾燥する場
合の大きな問題点は、乾燥排ガス5が強い悪臭を帯びる
ことであり、このために従来は、薬液脱臭、吸着脱臭、
燃焼脱臭などの脱臭装置を必ず設けなければならず、そ
の設備費、運転費が高額となっていた。しかるに、本発
明では熱風乾燥時の乾燥排ガス5を曝気ブロワ−7の吸
引空気9に混合させて汚水の生物処理槽16に供給し、
曝気と共に微生物(活性汚泥)によって生物学的に脱臭
されるので、脱臭設備と脱臭運転費(ランニングコスト
)は完全に不要になる。Furthermore, a major problem when drying a dehydrated cake of organic sludge with hot air is that the dried exhaust gas 5 has a strong odor.
Deodorizing equipment such as combustion deodorizing equipment must be installed, and the equipment and operating costs are high. However, in the present invention, the dry exhaust gas 5 during hot air drying is mixed with the suction air 9 of the aeration blower 7 and supplied to the biological treatment tank 16 for wastewater.
Since deodorization is carried out biologically by microorganisms (activated sludge) along with aeration, deodorization equipment and deodorization operating costs (running costs) are completely unnecessary.
〔実施例]
処理量10okg/日のし尿の低希釈二段活性汚泥プロ
セスから発生する余剰活性汚泥と三次処理工程から排出
された凝集沈殿汚泥との混合汚泥1200 kg・乾燥
固形物7日を、ベルトプレス型脱水機で脱水したケーキ
(水分82.0%)を、まず直径50ONφの攪拌流動
層型の連続造粒乾燥機に供給し、温度800℃の熱風を
供給したところ、水分45%、粒径3〜5鶴の球形ペレ
ット状の乾燥汚泥を得た。このときの連続造粒乾燥機か
ら排出された乾燥排ガスの温度は75°C(湿球温度)
、流量は7.1Nm/minで、悪臭をもつものであっ
た。[Example] A mixed sludge of 1200 kg/7 days of dry solids, which is a mixture of excess activated sludge generated from a low dilution two-stage activated sludge process and coagulated sedimentation sludge discharged from the tertiary treatment process, with a processing amount of 10 kg/day of human waste, The cake (82.0% moisture) dehydrated with a belt press type dehydrator was first fed to a stirred fluidized bed continuous granulation dryer with a diameter of 50ONφ, and hot air at a temperature of 800°C was supplied, resulting in a moisture content of 45%. Dried sludge in the form of spherical pellets with a particle size of 3 to 5 grains was obtained. The temperature of the dry exhaust gas discharged from the continuous granulation dryer at this time was 75°C (wet bulb temperature)
The flow rate was 7.1 Nm/min, and it had a bad odor.
この乾燥排ガスを曝気ブロワ−吸引空気(温度25°C
)に混合したものを曝気ブロワ−で圧縮(圧縮所要動力
90kW)した結果、温度110℃、流ft 80 r
d /min 、ゲージ圧力0.53kgf/c+dの
ブロワ−吐出空気を得た。次に、このプロワ−吐出空気
を、前記の連続造粒乾燥機で得られた球形ペレット状の
乾燥汚泥を通気乾燥器中に直径1mφ、層厚1mに充填
した充填層に通気した結果、水分5〜7%の高度に乾燥
された最終乾燥汚泥を得た。This dry exhaust gas is transferred to an aeration blower with suction air (temperature 25°C).
) was compressed using an aeration blower (required compression power: 90 kW), resulting in a temperature of 110°C and a flow rate of ft 80 r.
Blower discharge air was obtained at a pressure of 0.53 kgf/c+d and a gauge pressure of 0.53 kgf/c+d. Next, the air discharged from the blower was passed through a packed bed in which dried sludge in the form of spherical pellets obtained in the continuous granulation dryer was filled in an aeration dryer to a diameter of 1 mφ and a layer thickness of 1 m. A highly dried final dried sludge of 5-7% was obtained.
一方、通気乾燥器から排出された空気(臭気濃度150
0〜20QO)を、低希釈二段活性汚泥プロセスの硝化
槽にエアレーンヨン用空気として供給した。そして、硝
化槽の水面から排出してくるエアレーション空気をサン
プリングして臭気濃度を測定したところ、400〜50
0であり、悪臭はなく、土のような臭であった。On the other hand, the air discharged from the ventilation dryer (odor concentration 150
0 to 20 QO) was supplied as air for air lane to the nitrification tank of the low dilution two-stage activated sludge process. When we sampled the aeration air discharged from the water surface of the nitrification tank and measured the odor concentration, it was found to be 400 to 50.
0, there was no bad odor, and the odor was like earth.
以上述べたように本発明によれば、次のような顕著な効
果を得ることができる。As described above, according to the present invention, the following remarkable effects can be obtained.
■ 存機性汚泥の脱水ケーキを2段階で乾燥し、後段の
乾燥工程を燃費ゼロという省エネルギー的乾燥を行うと
いう新規な構成をとった結果、全体として乾燥コストが
大幅に節減される。■ As a result of adopting a new configuration in which the dehydrated cake of organic sludge is dried in two stages, and the latter drying process is performed in an energy-saving manner with zero fuel consumption, the overall drying cost is significantly reduced.
■ 前段の熱風乾燥工程からの乾燥排ガス(外気よりも
高温を示す)を、後段の通気乾燥工程と汚水のエアレー
ンヨンのためのエネルギーを供給する曝気ブロワ−の吸
引外気に混合せしめる構成としたので、後段の乾燥工程
の乾燥用熱エネルギーの増加のために前段の乾燥工程の
排熱を行動利用でき、その結果、前記■の効果と相俟っ
て、極めて省エネルギー型の汚泥乾燥プロセスを確立で
きる。■ The structure is such that the dry exhaust gas from the hot air drying process (which has a higher temperature than the outside air) is mixed with the outside air sucked into the aeration blower, which supplies energy for the air drying process and the wastewater air lane. The waste heat from the previous drying process can be utilized to increase the drying thermal energy for the latter drying process, and as a result, in combination with the effect (2) above, an extremely energy-saving sludge drying process can be established.
■ 悪臭を有する乾燥排ガスは、汚水の生物処理に導か
れて利用され、同時に生物学的に脱臭されるから、脱臭
設備、脱臭経費が不要になる。■ Dry exhaust gas with a bad odor is guided to the biological treatment of wastewater and used, and at the same time it is biologically deodorized, eliminating the need for deodorizing equipment and deodorizing costs.
図面は本発明の一実施態様を示す系統説明図である。
1・・・脱水ケーキ、2・・・第1熱風乾燥機、3・・
・熱風、4・・・乾燥汚泥、5・・・乾燥排ガス、6・
・・除しん器、7・・・曝気ブロワ−18・・・設置室
、9・・・吸引空気、10・・・吐出空気、11・・・
通気乾燥器、12・・・充填層、13・・・最終乾燥汚
泥、14・・・排出空気、15・・・汚水、16・・・
生物処理槽、17・・・散気器。The drawing is a system explanatory diagram showing one embodiment of the present invention. 1... Dehydrated cake, 2... First hot air dryer, 3...
・Hot air, 4... Dried sludge, 5... Dry exhaust gas, 6.
... Dust remover, 7... Aeration blower 18... Installation room, 9... Suction air, 10... Discharge air, 11...
Ventilation dryer, 12... Filled bed, 13... Final dried sludge, 14... Discharged air, 15... Sewage, 16...
Biological treatment tank, 17... air diffuser.
Claims (1)
工程からの乾燥排ガスを汚水の生物処理用の曝気ブロワ
ーの吸引空気に混合し、該ブロワーの吐出空気を前記熱
風乾燥工程から排出された乾燥物に直接接触せしめてさ
らに乾燥したのち汚水の生物処理に使用することを特徴
とする有機性汚泥の乾燥方法。 2、前記熱風乾燥に、攪拌流動層による造粒乾燥を採用
したものである特許請求の範囲第1項記載の有機性汚泥
の乾燥方法。[Claims] 1. A dehydrated cake of organic sludge is dried with hot air, and the dried exhaust gas from the hot air drying process is mixed with suction air of an aeration blower for biological treatment of sewage, and the discharge air of the blower is mixed with the air discharged from the blower. A method for drying organic sludge, which is characterized in that it is brought into direct contact with dried material discharged from a hot air drying process, further dried, and then used for biological treatment of sewage. 2. The method for drying organic sludge according to claim 1, wherein the hot air drying employs granulation drying using an agitated fluidized bed.
Priority Applications (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP60241283A JPS62102899A (en) | 1985-10-30 | 1985-10-30 | Drying method for organic sludge |
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP60241283A JPS62102899A (en) | 1985-10-30 | 1985-10-30 | Drying method for organic sludge |
Publications (2)
Publication Number | Publication Date |
---|---|
JPS62102899A true JPS62102899A (en) | 1987-05-13 |
JPH0374159B2 JPH0374159B2 (en) | 1991-11-26 |
Family
ID=17071956
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
JP60241283A Granted JPS62102899A (en) | 1985-10-30 | 1985-10-30 | Drying method for organic sludge |
Country Status (1)
Country | Link |
---|---|
JP (1) | JPS62102899A (en) |
Cited By (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN101825390A (en) * | 2010-04-27 | 2010-09-08 | 莱芜钢铁集团有限公司 | Double-layered vibrating fluidized-bed drying-classification apparatus |
JP2014169858A (en) * | 2009-06-05 | 2014-09-18 | Megtec Systems Inc | Method of regulating drying of web in dryer by convective and radiative heat transfer |
-
1985
- 1985-10-30 JP JP60241283A patent/JPS62102899A/en active Granted
Cited By (7)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JP2014169858A (en) * | 2009-06-05 | 2014-09-18 | Megtec Systems Inc | Method of regulating drying of web in dryer by convective and radiative heat transfer |
US9228779B2 (en) | 2009-06-05 | 2016-01-05 | Megtec Systems, Inc. | Infrared float bar |
JP2016191550A (en) * | 2009-06-05 | 2016-11-10 | メグテック システムズ インコーポレイテッド | Method of adjusting drying of web in dryer by convection heat transfer and radiation heat transfer |
US9746235B2 (en) | 2009-06-05 | 2017-08-29 | Megtec Systems, Inc. | Infrared float bar |
US10139159B2 (en) | 2009-06-05 | 2018-11-27 | Babcock & Wilcox Megtec, Llc | Infrared float bar |
US10371443B2 (en) | 2009-06-05 | 2019-08-06 | Durr Megtec, Llc | Infrared float bar |
CN101825390A (en) * | 2010-04-27 | 2010-09-08 | 莱芜钢铁集团有限公司 | Double-layered vibrating fluidized-bed drying-classification apparatus |
Also Published As
Publication number | Publication date |
---|---|
JPH0374159B2 (en) | 1991-11-26 |
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