JPH0734919B2 - Drying equipment for water-containing waste - Google Patents
Drying equipment for water-containing wasteInfo
- Publication number
- JPH0734919B2 JPH0734919B2 JP1296157A JP29615789A JPH0734919B2 JP H0734919 B2 JPH0734919 B2 JP H0734919B2 JP 1296157 A JP1296157 A JP 1296157A JP 29615789 A JP29615789 A JP 29615789A JP H0734919 B2 JPH0734919 B2 JP H0734919B2
- Authority
- JP
- Japan
- Prior art keywords
- water
- dryer
- carrier gas
- containing waste
- drying
- 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 - Fee Related
Links
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims description 80
- 238000001035 drying Methods 0.000 title claims description 27
- 239000002699 waste material Substances 0.000 title claims description 23
- 239000012159 carrier gas Substances 0.000 claims description 36
- 238000001816 cooling Methods 0.000 claims description 16
- 239000008236 heating water Substances 0.000 claims description 2
- 238000007791 dehumidification Methods 0.000 description 19
- 239000000498 cooling water Substances 0.000 description 11
- 230000007423 decrease Effects 0.000 description 7
- 229920006395 saturated elastomer Polymers 0.000 description 5
- 238000001704 evaporation Methods 0.000 description 3
- 230000008020 evaporation Effects 0.000 description 3
- 230000004044 response Effects 0.000 description 3
- 239000007787 solid Substances 0.000 description 3
- 230000003247 decreasing effect Effects 0.000 description 2
- 230000018044 dehydration Effects 0.000 description 2
- 238000006297 dehydration reaction Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000000034 method Methods 0.000 description 2
- 239000010802 sludge Substances 0.000 description 2
- 238000003756 stirring Methods 0.000 description 2
- 238000013459 approach Methods 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- -1 for example Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 230000004043 responsiveness Effects 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
- 239000010801 sewage sludge Substances 0.000 description 1
- 239000008399 tap water Substances 0.000 description 1
- 235000020679 tap water Nutrition 0.000 description 1
- 230000000007 visual effect Effects 0.000 description 1
Landscapes
- Drying Of Solid Materials (AREA)
- Treatment Of Sludge (AREA)
Description
【発明の詳細な説明】 （産業上の利用分野） 本発明は下水処理施設等において脱水ケーキ等の含水廃
棄物の乾燥に使用される含水廃棄物の乾燥装置に関する
ものである。TECHNICAL FIELD The present invention relates to a water-containing waste drying apparatus used for drying water-containing waste such as dehydrated cake in a sewage treatment facility or the like.
（従来の技術及び発明が解決しようとする課題） 上水、下水汚泥や海浜、港湾のヘドロ等を処理するに
は、フィルタープレス等の脱水装置によって汚泥を脱水
して所定量の水分を含有する脱水ケーキを製造し、この
脱水ケーキを乾燥して水分量を例えば55重量％以下とし
て焼却炉へと投入し、焼却処理することが行われてい
る。このため従来から例えば特開昭60−178284号公報に
示されるように、水蒸気により加熱された攪拌羽根によ
ってケーキを移送しつつ加熱乾燥を行わせるパドルドラ
イヤ型の乾燥設備が広く用いられている。このような従
来の乾燥設備は上記供給量の増減や送り速度の調整等に
よってある程度は乾燥能力の制御が可能であるが、供給
される脱水ケーキの水分変動が大きいと乾燥が進みすぎ
る。そして、乾燥機から排出される脱水ケーキが過乾燥
となると、後処理の焼却炉において、たとえば燃焼が乾
燥段側に移行して炉体が損傷すること等のトラブルを起
し、操業が不安定となった。(Problems to be solved by conventional techniques and inventions) In order to treat tap water, sewage sludge, sludge on beaches, harbors, etc., the sludge is dehydrated by a dehydrating device such as a filter press to contain a predetermined amount of water. BACKGROUND ART A dehydrated cake is manufactured, and the dehydrated cake is dried and put into an incinerator with a water content of 55% by weight or less, for incineration. For this reason, conventionally, for example, as disclosed in JP-A-60-178284, a paddle dryer type drying equipment has been widely used in which heating and drying are performed while transferring a cake by a stirring blade heated by steam. In such a conventional drying equipment, the drying capacity can be controlled to some extent by increasing or decreasing the supply amount or adjusting the feeding speed, but if the water content of the supplied dehydrated cake fluctuates greatly, the drying will proceed too much. Then, if the dehydrated cake discharged from the dryer becomes overdried, in an incinerator for post-treatment, for example, combustion shifts to the drying stage side, causing troubles such as damage to the furnace body, resulting in unstable operation. Became.
このため、供給される脱水ケーキの入口水分（乾燥機の
入口における脱水ケーキ水分）が低い場合には、水蒸気
圧力を低下させたり、乾燥機への脱水ケーキの投入量を
減少させ、乾燥機を通さない脱水ケーキと混合したりし
ていた。Therefore, when the inlet water content of the supplied dehydrated cake (dehydrated cake water content at the inlet of the dryer) is low, the steam pressure is reduced or the amount of the dehydrated cake fed into the dryer is reduced to reduce the dryer. It was mixed with a dehydrated cake that would not pass through.
しかし、乾燥機内における脱水ケーキの滞留時間は機種
により変動するが大体１時間以上あるうえ、水蒸気圧力
や脱水ケーキの投入量を変更しても、操作後、定常状態
となるのに４〜５時間を要するため、即応性がなく、不
安定時間が４〜５時間続き、燥炉がしにくく、また乾燥
能力が低下した。However, the residence time of the dehydrated cake in the dryer varies depending on the model, but it is about 1 hour or more, and even if the steam pressure or the amount of the dehydrated cake is changed, it takes 4 to 5 hours to reach a steady state after the operation. Therefore, there was no responsiveness, the unstable time lasted for 4 to 5 hours, the drying oven was difficult to operate, and the drying capacity was lowered.
本発明の課題は、乾燥機へと収容される含水廃棄物中の
水分量の変化に対応して速やかに乾燥品の水分量を制御
でき、しかも乾燥能力の低下しない含水廃棄物の乾燥装
置を提供することである。An object of the present invention is to provide a drying apparatus for a water-containing waste that can quickly control the water content of a dried product in response to a change in the water content in a water-containing waste stored in a dryer, and that does not lower the drying capacity. Is to provide.
（課題を解決するための手段） 本発明は、含水廃棄物を加熱してこの含水廃棄物から水
分を蒸発させる乾燥機と；この乾燥機から送られかつ前
記水分を含有するキャリアガスを収容し、このキャリア
ガスを冷却除湿する除湿機と；この除湿機から排出され
た前記キャリアガスを前記乾燥機内へと循環するキャリ
アガス循環手段と；乾燥後の前記含水廃棄物中の水分を
計測する水分計測手段と；除湿時の前記キャリアガスの
冷却温度を検出する温度検出手段と；前記含水廃棄物中
の水分の計測値に従って前記冷却温度を制御する制御手
段とを有する含水廃棄物の乾燥装置に係るものである。(Means for Solving the Problems) The present invention relates to a dryer for heating water-containing waste to evaporate water from the water-containing waste; and a carrier gas sent from the dryer and containing the water. A dehumidifier for cooling and dehumidifying the carrier gas; a carrier gas circulating means for circulating the carrier gas discharged from the dehumidifier into the dryer; a moisture for measuring the water content in the water-containing waste after drying An apparatus for drying water-containing waste, comprising: measuring means; temperature detecting means for detecting a cooling temperature of the carrier gas during dehumidification; and control means for controlling the cooling temperature according to a measured value of water in the water-containing waste. It is related.
（実施例） 第１図は本発明に係る乾燥装置の一例を示す制御系統図
である。この図面において、実線は主としてキャリアガ
スの流れを、太線は脱水ケーキの流れを、破線は電気信
号の流れをそれぞれ示す。(Example) FIG. 1 is a control system diagram showing an example of a drying apparatus according to the present invention. In this drawing, the solid line mainly shows the flow of carrier gas, the thick line shows the flow of dehydrated cake, and the broken line shows the flow of electric signal.
フィルタープレス等によって製造された脱水ケーキは、
投入口1aより乾燥機１内へと投入され、図面において左
方から右方へと送られる間に加熱脱水され、排出口1bよ
り所定水分量の乾燥品となって排出され、搬送、焼却等
の次工程へと廻される。加熱機１は好ましくは、内部に
攪拌羽根を備えたパドルドライヤ型のものであるが、こ
れには限定されない。The dehydrated cake produced by a filter press etc.
It is put into the dryer 1 from the input port 1a, heated and dehydrated while being sent from the left to the right in the drawing, and discharged from the output port 1b as a dry product with a predetermined amount of water, transported, incinerated, etc. It is sent to the next process of. The heater 1 is preferably a paddle dryer type with stirring blades inside, but is not limited to this.
乾燥機１内で脱水ケーキから水分が蒸発すると、この水
分を空気等のキャリアガスで運んでキャリアガス排出口
1dより排出し、除湿塔２内へと供給する。除湿塔２の図
面において右側には冷却水供給手段５が配置され、制御
弁４を開いて所定流量の冷却水を除湿塔２内へと散布す
ると除湿塔２内のキャリアガスが冷却される。キャリア
ガス、例えば空気の飽和水分量が後述するように温度が
下がるとそれにつれて低下するため、冷却されたキャリ
アガス中の水蒸気が結露し、冷却水と共に除湿塔の下部
に流れ排水部３へと排出される。When water is evaporated from the dehydrated cake in the dryer 1, this water is carried by a carrier gas such as air and the carrier gas outlet
It is discharged from 1d and supplied into the dehumidification tower 2. Cooling water supply means 5 is arranged on the right side of the dehumidification tower 2 in the drawing, and when the control valve 4 is opened and a predetermined flow rate of cooling water is sprayed into the dehumidification tower 2, the carrier gas in the dehumidification tower 2 is cooled. As the saturated moisture content of the carrier gas, for example, air, decreases as the temperature decreases as described later, the water vapor in the cooled carrier gas condenses and flows with the cooling water to the lower part of the dehumidifying tower to the drainage section 3. Is discharged.
冷却除湿されたキャリアガスは除湿塔２内から排出さ
れ、循環ファン６によって送風口1cより再び乾燥機１内
へと送風され、新たな脱水ケーキより蒸発した水分を再
び脱湿塔２へと運ぶ。キャリアガスを乾燥機１内へと循
環する前にヒーター12で加熱するのが好ましい。The carrier gas that has been cooled and dehumidified is discharged from the dehumidification tower 2, is blown again into the dryer 1 through the blower port 1c by the circulation fan 6, and the moisture evaporated from the new dehydrated cake is conveyed again to the dehumidification tower 2. . It is preferable to heat the carrier gas with the heater 12 before circulating it into the dryer 1.
乾燥品排出口1b付近には水分計７を配し、乾燥品の水分
量を測定する。この測定値は目視インジケーター８を介
して演算器９へと送られ、次いで制御器10へと入力され
る。除湿塔から排出されたキャリアガスの冷却温度を温
度検出器11で検出し、電気信号として制御器10へと入力
する。これら乾燥品の水分量の測定値とキャリアガスの
冷却温度の検出値とに基づいて制御弁４を操作し、除湿
塔２内に散布する冷却水の水量を操作し、除湿塔２内で
のキャリアガスの冷却温度を変える。A moisture meter 7 is arranged near the dry product outlet 1b to measure the moisture content of the dry product. This measured value is sent to the computing unit 9 via the visual indicator 8 and then input to the controller 10. The temperature detector 11 detects the cooling temperature of the carrier gas discharged from the dehumidifying tower, and inputs it to the controller 10 as an electric signal. The control valve 4 is operated based on the measured value of the water content of these dried products and the detected value of the cooling temperature of the carrier gas to operate the water amount of the cooling water sprayed in the dehumidification tower 2 so that Change the cooling temperature of the carrier gas.
例えば、乾燥機１へと投入する脱水ケーキの水分を80重
量％とし、乾燥品の水分を40重量％とするように乾燥機
の能力が設計されている場合、トータルケーキ量を仮に
1000kgとすると、投入時の脱水ケーキ及び乾燥品の固形
分量及び水分量は以下の通りになる。For example, if the capacity of the dryer is designed so that the water content of the dehydrated cake to be fed to the dryer 1 is 80% by weight and the water content of the dried product is 40% by weight, the total cake amount is temporarily set.
Assuming 1000 kg, the solid content and water content of the dehydrated cake and dried product at the time of addition are as follows.
固形分量 水分量 全 量 投入時の脱水ケーキ 200kg 800kg 1000kg 乾燥品 200kg 133kg 333kg 従って、乾燥機の水分蒸発能力は667kgである。 Solid content Water content Total amount of dehydrated cake 200kg 800kg 1000kg Dry product 200kg 133kg 333kg Therefore, the moisture evaporation capacity of the dryer is 667kg.
ここで、仮に投入する脱水ケーキの水分量が変動し、75
重量％となったりすると、蒸発水分能力は一定であるた
め、以下の関係となる。Here, the amount of water in the dehydrated cake to be put in temporarily fluctuates,
When the weight percentage is reached, the evaporation moisture capacity is constant, so the following relationship is established.
固形分量 水分量 全 量 投入時の脱水ケーキ 250kg 750kg 1000kg 乾燥品 250kg 83kg 333kg （750−667） 従って、乾燥品の水分量は25％となり、設計値の40％に
くらべて遥かに小さくなり過乾燥となる。Solid content Moisture content Total amount of dehydrated cake 250kg 750kg 1000kg Dry product 250kg 83kg 333kg (750-667) Therefore, the moisture content of the dry product is 25%, much smaller than the design value of 40% and overdried. Becomes
即ち、 の関係が成り立つため、蒸発能力、即ち蒸発水分重量を
一定とすると、入口水分重量が低下すれば必然的に乾燥
品水分重量も低下し、過乾燥となる。That is, Therefore, if the evaporation capacity, that is, the weight of evaporated water is constant, if the weight of water at the inlet decreases, the weight of water in the dried product also inevitably decreases, resulting in overdrying.
これに対し、本実施例に係る脱水ケーキの乾燥装置によ
れば、乾燥品の水分と除湿塔２の出口でのキャリアガス
温度を測定し、乾燥品水分と設定水分との偏差に応じて
除湿塔２への冷却水量を増減することにより、除湿塔２
内でのキャリアガス冷却温度を変えている。従って、除
湿塔２内でのキャリアガスの飽和水分量が温度によって
変わるため、除湿後のキャリアガスの絶対温度を変え、
乾燥機１へと持ち帰る水分量を変えることができる。On the other hand, according to the dehydration cake drying apparatus according to the present embodiment, the moisture of the dried product and the carrier gas temperature at the outlet of the dehumidifying tower 2 are measured, and the dehumidification is performed according to the deviation between the dried product moisture and the set moisture. By increasing or decreasing the amount of cooling water to the tower 2, the dehumidifying tower 2
The carrier gas cooling temperature inside is changed. Therefore, since the saturated moisture content of the carrier gas in the dehumidification tower 2 changes depending on the temperature, the absolute temperature of the carrier gas after dehumidification is changed,
The amount of water brought back to the dryer 1 can be changed.
例えば、乾燥品の水分量が設定値よりも低下すると、乾
燥機１内のキャリアガスの水分量を増加させる蒸発水分
量を減らす必要がある。そこで、脱湿塔２から排出され
たキャリアガスの温度を測定しながら制御器10で制御弁
４を更に閉じ、冷却水の供給量を減少させ、脱湿塔２内
のキャリアガスの温度を上昇させると、飽和水分量が多
くなることから乾燥機への持ち帰り水分量が増え、結果
として、乾燥機１内での蒸発水分量が減る。従って、乾
燥品の水分量を増やして設定値へと近づけることがで
き、これらが設定値へと達したらその状態を保持すれば
よい。For example, when the water content of the dried product falls below the set value, it is necessary to reduce the evaporated water content that increases the water content of the carrier gas in the dryer 1. Therefore, while controlling the temperature of the carrier gas discharged from the dehumidification tower 2, the controller 10 further closes the control valve 4 to reduce the supply amount of cooling water and raise the temperature of the carrier gas in the dehumidification tower 2. Then, the saturated water content increases, and the water content taken back to the dryer increases, and as a result, the evaporated water content in the dryer 1 decreases. Therefore, the water content of the dried product can be increased to approach the set value, and when these reach the set value, the state may be maintained.
このように、本実施例の乾燥装置によれば、乾燥品の水
分量変動に即応して、冷却水の除湿塔への供給量を変化
させるだけで乾燥品の水分量を設定値へと戻すことがで
きる。従って、乾燥品の水分量変動に対して容易かつ迅
速に対応できるので、安定した操業ができる。しかも、
冷却水の除湿塔への供給量のいかんに係らず、乾燥機で
脱水ケーキを乾燥処理でき、処理個数や処理速度は変化
しないので、能率が低下することはない。As described above, according to the drying apparatus of the present embodiment, the moisture content of the dried product is returned to the set value simply by changing the supply amount of the cooling water to the dehumidifying tower in response to the variation of the moisture content of the dried product. be able to. Therefore, it is possible to easily and swiftly respond to fluctuations in the water content of the dried product, so that stable operation can be performed. Moreover,
Regardless of the amount of cooling water supplied to the dehumidifying tower, the dehydrated cake can be dried by a dryer, and the number of processed products and the processing speed do not change, so efficiency does not decrease.
具体的に、キャリアガスとして空気を用いた例を挙げる
と、冷却温度と除湿後の絶対湿度との関係は、以下のよ
うになる。Specifically, taking the example of using air as the carrier gas, the relationship between the cooling temperature and the absolute humidity after dehumidification is as follows.
飽和水分表 空気冷却温度 絶対湿度 40℃ 0.049 kg H2O/kg DG 50℃ 0.086 kg H2O/kg DG 60℃ 0.152 kg H2O/kg DG 70℃ 0.276 kg H2O/kg DG 80℃ 0.546 kg H2O/kg DG 87℃ 1.00 kg H2O/kg DG ここで、除湿塔２の出口における空気の重量を1350k/H
とした場合、乾燥機１への持ち帰り水分量は、 除湿塔出口温度40℃（絶対湿度;0.049kg−H2O/kg−DG）
時の除湿空気中の水分量 1350kg/H×0.049kg−H2O/kg−DG≒66kg/H 除湿塔出口温度70℃（絶対温度;0.279kg−H2O/kg−DG）
時の除湿空気中の水分量 1350kg/H×0.279kg−H2O/kg−DG≒373kg/H となる。乾燥機１の空気排出口1dにおける除湿空気中の
絶対温度を0.5kg−H2O/kg−DGで一定とすると、除湿塔
出口温度が約80℃のときに空気は飽和状態となり、乾燥
機への持ち帰り水分量≒蒸発水分量となるため、乾燥機
１内に投入される脱水ケーキの水分量と、乾燥機１より
排出される乾燥品の水分量とは同じになる。Saturated moisture table Air cooling temperature Absolute humidity 40 ° C 0.049 kg H 2 O / kg DG 50 ° C 0.086 kg H 2 O / kg DG 60 ° C 0.152 kg H 2 O / kg DG 70 ° C 0.276 kg H 2 O / kg DG 80 ° C 0.546 kg H 2 O / kg DG 87 ℃ 1.00 kg H 2 O / kg DG Here, the weight of the air at the outlet of the dehumidifying tower 2 is 1350 k / H.
In this case, the amount of water to be brought back to the dryer 1 is 40 ° C at the dehumidifying tower outlet temperature (absolute humidity; 0.049kg-H 2 O / kg-DG).
Moisture content in dehumidified air at 1350kg / H × 0.049kg−H 2 O / kg−DG ≈ 66kg / H Dehumidifier tower outlet temperature 70 ° C (absolute temperature; 0.279kg−H 2 O / kg−DG)
The amount of water in the dehumidified air at that time is 1350 kg / H × 0.279 kg-H 2 O / kg-DG ≈ 373 kg / H. If the absolute temperature in the dehumidified air at the air outlet 1d of the dryer 1 is kept constant at 0.5 kg-H 2 O / kg-DG, the air will be saturated when the dehumidifying tower outlet temperature is approximately 80 ° C, and the dryer will Since the amount of water to be brought back to the product is approximately equal to the amount of evaporated water, the amount of water in the dehydrated cake put into the dryer 1 and the amount of water in the dried product discharged from the dryer 1 are the same.
キャリアガスの冷却温度を変えるには、上記のように冷
却水の供給量を変える場合の他、冷却水の温度を変える
方法もある。In order to change the cooling temperature of the carrier gas, there is a method of changing the temperature of the cooling water in addition to changing the supply amount of the cooling water as described above.
次いで、実際に図面に示す装置を作動させて脱水ケーキ
を乾燥した例を示す。Next, an example in which the dehydrated cake is dried by actually operating the device shown in the drawing is shown.
即ち、乾燥機入口での脱水ケーキ水分、乾燥機出口での
脱水ケーキ乾燥品水分、乾燥機出口でのキャリアガス温
度、及び除湿塔出口でのキャリアガス温度を測定した。
冷却は20℃の水で行った。結果を表に示す。That is, the dehydrated cake water content at the dryer inlet, the dehydrated cake dried product water content at the dryer outlet, the carrier gas temperature at the dryer outlet, and the carrier gas temperature at the dehumidifying tower outlet were measured.
Cooling was performed with water at 20 ° C. The results are shown in the table.
この結果から解るように、本発明により、乾燥品水分の
変動を抑えることができる。即ち、従来であれば、脱水
ケーキ水分が75％のときには乾燥品水分が25％付近にな
るのに対し、本実施例では水分変動は僅か４％である。
しかも、除湿塔出口キャリアガス温度を更に少し上げれ
ば、更に細かく微調整を行えることが明らかである。 As can be seen from this result, the present invention can suppress the fluctuation of the water content of the dried product. That is, in the conventional case, when the water content of the dehydrated cake is 75%, the water content of the dried product is around 25%, whereas in the present embodiment, the water content fluctuation is only 4%.
Moreover, it is apparent that finer fine adjustment can be performed by raising the temperature of the carrier gas at the outlet of the dehumidification tower a little more.
（発明の効果） 本発明に係る廃棄物の乾燥装置によれば、乾燥後の含水
廃棄物中の水分を計測し、かつ除湿時のキャリアガスの
冷却温度を検出し、前記の水分の計測値に従って前記冷
却温度を制御しているので、除湿時のキャリアガス中の
水分量を制御でき、従って除湿後のキャリアガスを乾燥
機内へと送風していることから、乾燥機内へと持ち帰ら
れる水分量を制御できる。これにより、乾燥機内の湿度
を制御できることから、この乾燥機内で加熱される含水
廃棄物からの水分蒸発量を制御でき、最終的に乾燥後の
含水廃棄物中の水分量を制御できる。(Effect of the Invention) According to the waste drying apparatus of the present invention, the water content of the water-containing waste after drying is measured, and the cooling temperature of the carrier gas at the time of dehumidification is detected to obtain the measured value of the water content. Since the cooling temperature is controlled in accordance with the above, it is possible to control the amount of water in the carrier gas during dehumidification. Therefore, since the carrier gas after dehumidification is blown into the dryer, the amount of water taken back into the dryer Can be controlled. As a result, since the humidity inside the dryer can be controlled, the amount of water evaporated from the water-containing waste heated in the dryer can be controlled, and finally the amount of water in the water-containing waste after drying can be controlled.
従って、乾燥後の含水廃棄物中の水分量変動に即応し
て、基本的に除湿時のキャリアガスの冷却温度を変化さ
せるだけで乾燥後の含水廃棄物中の水分量をもとに戻す
ことができる。このように、水分量変動に対して容易か
つ迅速に対応できるので、安定した操業が可能であり、
しかも乾燥機内での含水廃棄物の処理量や処理速度等は
変化しないので、能率が低下することはない。Therefore, it is possible to restore the water content in the water-containing waste after drying basically by simply changing the cooling temperature of the carrier gas during dehumidification, in response to the change in the water content in the water-containing waste after drying. You can In this way, it is possible to respond to fluctuations in water content easily and quickly, so stable operation is possible,
Moreover, since the treatment amount and treatment speed of the water-containing waste in the dryer do not change, the efficiency does not decrease.
よって本発明は従来の問題点を一掃した、含水廃棄物の
乾燥装置として、産業に寄与するところは極めて大であ
る。Therefore, the present invention greatly contributes to the industry as an apparatus for drying water-containing waste, which eliminates the conventional problems.
第１図は脱水ケーキの乾燥装置の制御系統図である。 １……乾燥機、２……脱湿塔 ４……制御弁、５……冷却水供給装置 ６……循環ファン、７……水分計 ９……演算器、10……制御器 11……温度検出器、12……ヒーター FIG. 1 is a control system diagram of a dehydration cake drying device. 1 ... Dryer, 2 ... Dehumidifying tower, 4 ... Control valve, 5 ... Cooling water supply device, 6 ... Circulation fan, 7 ... Moisture meter, 9 ... Computing unit, 10 ... Controller, 11 ... Temperature detector, 12 ... heater
Claims (1)
水分を蒸発させる乾燥機と；この乾燥機から送られかつ
前記水分を含有するキャリアガスを収容し、このキャリ
アガスを冷却除湿する除湿機と；この除湿機から排出さ
れた前記キャリアガスを前記乾燥機内へと循環するキャ
リアガス循環手段と；乾燥後の前記含水廃棄物中の水分
を計測する水分計測手段と；除湿時の前記キャリアガス
の冷却温度を検出する温度検出手段と；前記含水廃棄物
中の水分の計測値に従って前記冷却温度を制御する制御
手段とを有する含水廃棄物の乾燥装置。1. A dryer for heating water-containing waste to evaporate water from the water-containing waste; and a carrier gas sent from the dryer and containing the water, which is cooled and dehumidified. A dehumidifier; a carrier gas circulating means for circulating the carrier gas discharged from the dehumidifier into the dryer; a moisture measuring means for measuring the water content in the water-containing waste after drying; An apparatus for drying water-containing waste, comprising: temperature detecting means for detecting a cooling temperature of a carrier gas; and control means for controlling the cooling temperature according to a measured value of water in the water-containing waste.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP1296157A JPH0734919B2 (en) | 1989-11-16 | 1989-11-16 | Drying equipment for water-containing waste |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP1296157A JPH0734919B2 (en) | 1989-11-16 | 1989-11-16 | Drying equipment for water-containing waste |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH03157200A JPH03157200A (en) | 1991-07-05 |
| JPH0734919B2 true JPH0734919B2 (en) | 1995-04-19 |
Family
ID=17829901
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP1296157A Expired - Fee Related JPH0734919B2 (en) | 1989-11-16 | 1989-11-16 | Drying equipment for water-containing waste |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH0734919B2 (en) |
-
1989
- 1989-11-16 JP JP1296157A patent/JPH0734919B2/en not_active Expired - Fee Related
Also Published As
| Publication number | Publication date |
|---|---|
| JPH03157200A (en) | 1991-07-05 |
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