JP2000070995A - Method and apparatus for treating waste cleaning water of waste gas generated in waste plastic dechlorinating and fuel-converting process - Google Patents
Method and apparatus for treating waste cleaning water of waste gas generated in waste plastic dechlorinating and fuel-converting processInfo
- Publication number
- JP2000070995A JP2000070995A JP24753398A JP24753398A JP2000070995A JP 2000070995 A JP2000070995 A JP 2000070995A JP 24753398 A JP24753398 A JP 24753398A JP 24753398 A JP24753398 A JP 24753398A JP 2000070995 A JP2000070995 A JP 2000070995A
- Authority
- JP
- Japan
- Prior art keywords
- tank
- component
- hydrophobic
- components
- turbid
- 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
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
- Y02W30/00—Technologies for solid waste management
- Y02W30/50—Reuse, recycling or recovery technologies
- Y02W30/62—Plastics recycling; Rubber recycling
Landscapes
- Removal Of Specific Substances (AREA)
- Processing And Handling Of Plastics And Other Materials For Molding In General (AREA)
- Separation, Recovery Or Treatment Of Waste Materials Containing Plastics (AREA)
- Treating Waste Gases (AREA)
- Separation Of Suspended Particles By Flocculating Agents (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
Description
【０００１】[0001]
【発明の属する技術分野】本発明は、廃プラスチックか
ら塩化水素、塩素ガス等を除去して、例えば、燃料等と
して使用する脱塩素燃料化工程において、生成された排
ガスを洗浄処理する湿式アルカリ処理装置からの洗浄排
水処理方法及び装置に関する。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a wet alkali treatment for removing hydrogen chloride, chlorine gas and the like from waste plastics, and for cleaning the exhaust gas generated in a dechlorination fuel process for use as a fuel or the like. The present invention relates to a method and an apparatus for treating wastewater from washing.
【０００２】[0002]
【従来の技術】前記排ガスの洗浄排水中には、非常に高
い濃度のノルマルへキサン抽出成分、ＣＯＤ成分及びそ
の他の混濁成分が含まれ、従来の薬品添加による前記各
成分の酸化、還元及び／または凝集処理技術では、前記
ノルマルヘキサン抽出成分、ＣＯＤ成分及びその他の混
濁成分の濃度を、排水の放流規制値以下にすることは極
めて困難であった。2. Description of the Related Art A very high concentration of a normal hexane extraction component, a COD component and other turbid components are contained in the washing waste water of the exhaust gas, and the oxidation, reduction and / or reduction of each component by conventional chemical addition. Alternatively, with the coagulation treatment technology, it has been extremely difficult to make the concentrations of the normal hexane extraction component, the COD component, and other turbid components equal to or less than the regulated value for discharging the wastewater.
【０００３】[0003]
【発明が解決しようとする課題】本発明は、前記事情に
鑑み、廃プラスチックの脱塩素燃料化工程で生成された
排ガスの洗浄排水中に含まれる高濃度で、しかも性状変
動の激しいノルマルヘキサン抽出成分、ＣＯＤ成分及び
その他の混濁成分を、有効かつ連続的に除去できる処理
方法及び装置を提供することを目的とする。SUMMARY OF THE INVENTION In view of the above circumstances, it is an object of the present invention to extract high-concentration normal hexane which has a high concentration of fluctuations in the properties contained in the washing wastewater of the exhaust gas generated in the process of converting waste plastic into dechlorinated fuel. It is an object of the present invention to provide a processing method and apparatus capable of effectively and continuously removing components, COD components and other turbid components.
【０００４】[0004]
【課題を解決するための手段】請求項１は、洗浄排水中
の不飽和化合物を酸化及び飽和させてＣＯＤ成分濃度を
低減させると同時に疎水性混濁成分とノルマルヘキサン
抽出成分を微細気泡表面に付着浮上させて回収する曝気
工程、硫酸を加えてｐＨ値を調整した後、硫酸第一鉄を
加えて残存疎水性混濁成分をミクロフロック化する工
程、アルカリ添加によるｐＨ値調整工程、高分子凝集助
剤による前記ミクロフロック化された疎水性混濁成分を
凝縮させる工程、凝集された前記疎水性混濁成分を沈殿
分離する工程及び残存するノルマルヘキサン抽出成分、
ＣＯＤ成分及び親水性ゾルを活性炭により吸着除去する
工程と、からなる廃プラスチック脱塩素燃料化工程で生
成された排ガスの洗浄排水処理方法である。In order to reduce the COD component concentration by oxidizing and saturating unsaturated compounds in the washing wastewater, a hydrophobic turbid component and a normal hexane extract component adhere to the surface of the fine bubbles. An aeration step for floating and recovery, a step of adding sulfuric acid to adjust the pH value, a step of adding ferrous sulfate to microfloc the remaining hydrophobic turbid components, a step of adjusting the pH value by adding an alkali, Condensing the microfloc hydrophobic turbid component by the agent, a step of separating the aggregated hydrophobic turbid component by precipitation and a residual normal hexane extract component,
A process for adsorbing and removing the COD component and the hydrophilic sol with activated carbon, and a method for treating waste water produced by the waste plastic dechlorination fuel conversion process.
【０００５】この請求項１の処理方法によれば、前記ノ
ルマルヘキサン抽出成分、ＣＯＤ成分及び疎水性混濁物
質を有効に除去することができる。According to the processing method of the first aspect, the normal hexane extraction component, the COD component and the hydrophobic turbid substance can be effectively removed.
【０００６】請求項２は、洗浄排水が供給される曝気槽
及びその水面に設けられた浮上物質の回収装置、前記曝
気槽から浮上物質が除去された前記洗浄排水が順次供給
される硫酸及び硫酸第一鉄供給自在の反応槽、アルカリ
供給自在のｐＨ調整槽、高分子凝集助剤供給自在の凝集
槽、沈殿槽、及び活性炭槽と、からなる廃プラスチック
脱塩素燃料化工程で生成された排ガスの洗浄排水処理装
置である。A second aspect of the present invention is an aeration tank to which cleaning wastewater is supplied, a recovery device for a floating substance provided on the water surface thereof, sulfuric acid and sulfuric acid to which the cleaning wastewater from which the floating substance has been removed from the aeration tank is sequentially supplied. Exhaust gas generated in the waste plastic dechlorination fuel process consisting of a reaction tank that can supply ferrous iron, a pH adjustment tank that can supply alkali, a coagulation tank that can supply a polymer coagulation aid, a precipitation tank, and an activated carbon tank Cleaning wastewater treatment equipment.
【０００７】この請求項２の処理装置によれば、ノルマ
ルヘキサン抽出成分、ＣＯＤ成分及びその他の疎水性混
濁成分を連続的に除去することができる。According to the processing apparatus of the second aspect, the normal hexane extraction component, the COD component and other hydrophobic turbid components can be continuously removed.
【０００８】請求項３は、前記浮上物質の回収装置にエ
マルジョンブレ−カ−が接続され、疎水性混濁成分及び
ノルマルヘキサン抽出成分と洗浄排水（水分）を分離す
るとともに、疎水性混濁成分及びノルマルヘキサン抽出
成分を除去し、水分を前記曝気槽に戻す前記請求項２に
記載の廃プラスチック脱塩素燃料化工程で生成された排
ガスの洗浄排水処理装置である。In a third aspect of the present invention, an emulsion breaker is connected to the device for recovering the floating substance, and separates a hydrophobic turbid component and a normal hexane extract component from a washing wastewater (moisture). The cleaning and wastewater treatment apparatus for exhaust gas generated in the waste plastic dechlorination fuel conversion step according to claim 2, wherein the hexane extraction component is removed and water is returned to the aeration tank.
【０００９】この請求項３の処理装置によれば、浮上物
質にとして回収された疎水性混濁成分及びノルマルヘキ
サン抽出成分が、油分として分離されて外部に排出処理
され、前記浮上物質に混じって回収された洗浄排水（水
分）は、曝気槽に戻されるため、未処理の洗浄排水が外
部に排出されることがない。According to the third aspect of the present invention, the hydrophobic turbid component and the normal hexane extract component recovered as the floating substance are separated as oil and discharged to the outside, and are mixed with the floating substance and recovered. The washed washing wastewater (moisture) is returned to the aeration tank, so that untreated washing wastewater is not discharged to the outside.
【００１０】請求項４は、前記曝気槽と前記反応槽間に
計量槽を介在させた前記請求項２又は３に記載の廃プラ
スチック脱塩素燃料化工程で生成された排ガスの洗浄排
水処理装置である。A fourth aspect of the present invention is the apparatus for cleaning and discharging waste gas generated in the process of converting waste plastic into dechlorinated fuel according to the second or third aspect, wherein a measuring tank is interposed between the aeration tank and the reaction tank. is there.
【００１１】この請求項４の処理装置によれば、反応槽
に対する洗浄排水の供給量を一定に保つことができる。
したがって反応槽に対する洗浄排水の一定供給量に対し
て、必要とする正確な量の硫酸及び硫酸第一鉄を供給し
て、前記洗浄排水の酸性度制御及びミクロフロック化
を、有効に行うことができる。According to the processing apparatus of the fourth aspect, the supply amount of the washing wastewater to the reaction tank can be kept constant.
Therefore, for a given supply amount of the washing wastewater to the reaction tank, the required exact amount of sulfuric acid and ferrous sulfate are supplied to effectively perform the acidity control and micro flocking of the washing wastewater. it can.
【００１２】請求項５は、前記沈殿槽と前記活性炭槽間
に砂濾過槽を介在させた前記請求項２、３又は４に記載
の廃プラスチック脱塩素燃料化工程で生成された排ガス
の洗浄排水処理装置である。この請求項５の処理装置に
よれば、後に続く前記活性炭槽内の高価な活性炭の吸着
性能の寿命を延長させることができる。A fifth aspect of the present invention is a method for cleaning and discharging waste gas generated in the waste plastic dechlorination fuel conversion step according to the second, third, or fourth aspect, wherein a sand filtration tank is interposed between the settling tank and the activated carbon tank. Processing device. According to the processing device of the fifth aspect, the life of the adsorbing performance of expensive activated carbon in the activated carbon tank that follows can be extended.
【００１３】[0013]
【発明の実施の形態】以下に、本発明の実施の一形態を
図面に基づいて説明する。図１は、本発明の廃プラスチ
ック脱塩素燃料化工程で生成された排ガスの洗浄排水処
理装置のフローチャート、図２は、廃プラスチックの脱
塩燃料化装置の一部を破断した平面図、図３は、図２の
３−３線矢視断面図、図４は、前記廃プラスチックの脱
塩素燃料化装置を含む廃プラスチックの脱塩素燃料化プ
ラントの一例を示すフローチャートである。DESCRIPTION OF THE PREFERRED EMBODIMENTS An embodiment of the present invention will be described below with reference to the drawings. FIG. 1 is a flowchart of an apparatus for cleaning and draining waste gas generated in the waste plastic dechlorination fuel conversion step of the present invention, FIG. 2 is a plan view of a part of the waste plastic desalination fuel conversion apparatus, and FIG. 2 is a sectional view taken along line 3-3 in FIG. 2, and FIG. 4 is a flowchart showing an example of a waste plastic dechlorination fuel plant including the waste plastic dechlorination fuel conversion apparatus.
【００１４】図４において、３１は、廃プラスチックの
溶融及び減容効率を上げるための破砕機、３２は、前記
破砕された廃プラスチックを定量供給機３３へ搬送する
スクリューコンベア、３４は、前記定量供給機３３で定
量化された前記破砕プラスチックを、廃プラスチックの
脱塩素燃料化装置６１の廃プラスチック投入用のホッパ
ー６６へ搬送及び投入するコンベア、６９は、ギアボッ
クス、Ｍは、駆動装置である。In FIG. 4, 31 is a crusher for improving the efficiency of melting and reducing the volume of waste plastic, 32 is a screw conveyor for transporting the crushed waste plastic to a quantitative feeder 33, 34 is A conveyor for transporting and feeding the crushed plastic quantified by the feeder 33 to a hopper 66 for feeding waste plastic of a waste plastic dechlorination fuel conversion device 61, 69 is a gear box, and M is a driving device. .
【００１５】また、３５は、内部にバーナが設けられ、
前記廃プラスチック脱塩素燃料化装置６１へ無酸素炭酸
ガスリッチの燃焼ガスを供給する熱風発生炉、３６は、
前記熱風発生炉３５に設けられた送風ファン、３７は、
熱風発生炉用燃料タンク、３８は、熱風制御用ダンパー
である。The burner 35 is provided with a burner inside.
A hot air generator 36 for supplying a combustion gas rich in oxygen-free carbon dioxide to the waste plastic dechlorination fuel conversion device 61,
The blower fan 37 provided in the hot-air generator 35 includes:
The hot-air generator fuel tank 38 is a hot-air control damper.
【００１６】さらに、３９、４０、は前記脱塩素燃料化
装置６１で脱塩素炭化された廃プラスチックを搬出する
コンベア、４１は、脱塩素炭化された廃プラスチック、
４２は前記廃プラスチック脱塩素燃料化装置６１の、後
述する熱風加熱室６３に接続されたガス排出管、４３
は、排ガス脱臭装置、４４は、排ガスの湿式アルカリ処
理装置、４５は、排ガス洗浄中和液の苛性ソーダ収容タ
ンク、４６、４６、４６は、それぞれポンプ、４７、４
８は、排気ファン、４９は、デミスター、５０は、バグ
フィルタ、５１は、廃液タンクである。Further, 39 and 40 are conveyors for carrying out the waste plastic dechlorinated and carbonized by the dechlorination fuel conversion device 61, 41 is a dechlorinated carbonized waste plastic,
42 is a gas exhaust pipe of the waste plastic dechlorination fuel conversion device 61 connected to a hot air heating chamber 63 described later;
Is an exhaust gas deodorizing device, 44 is a wet alkali treatment device for exhaust gas, 45 is a caustic soda storage tank for an exhaust gas cleaning neutralizing solution, 46, 46, and 46 are pumps, 47 and 4, respectively.
8 is an exhaust fan, 49 is a demister, 50 is a bag filter, and 51 is a waste liquid tank.
【００１７】前記構成の廃プラスチックの脱塩素燃料化
プラントにおいては、廃プラスチックが、前記破砕機３
１で細かに破砕され、前記スクリューコンベア３２によ
って、前記定量供給機３３へ搬送される。In the waste plastic dechlorination fuel conversion plant having the above structure, the waste plastic is supplied to the crusher 3
The powder is finely crushed at 1 and is conveyed to the quantitative feeder 33 by the screw conveyor 32.
【００１８】そして、定量化された廃プラスチックが、
前記廃プラスチックの脱塩素燃料化装置６１に供給され
て脱塩素炭化処理が施され、該脱塩素炭化処理が施され
た廃プラスチック４１が、前記廃プラスチックの脱塩素
燃料化装置６１から排出及び固形化されて、前記コンベ
ア３９、４０によって搬出される。Then, the quantified waste plastic is
The waste plastic is supplied to the dechlorination fuel conversion device 61 and subjected to dechlorination and carbonization. The waste plastic 41 subjected to the dechlorination and carbonization is discharged and solidified from the waste plastic dechlorination and fuel conversion device 61. And is carried out by the conveyors 39 and 40.
【００１９】なお、後述する前記廃プラスチックの脱塩
素燃料化装置６１の熱風加熱室６３から、加熱された燃
焼ガスとともに排出される熱分解により生成された塩化
水素や塩素ガス等は、前記ガス排出管４２から前記排ガ
ス脱臭装置４３及び前記湿式アルカリ処理装置４４等に
導かれ、脱臭及び中和処理等を経て大気に排出される。It should be noted that hydrogen chloride, chlorine gas and the like generated by thermal decomposition discharged together with the heated combustion gas from the hot air heating chamber 63 of the waste plastic dechlorination fuel conversion device 61 described below are discharged from the gas discharge chamber. The waste gas is led from the pipe 42 to the exhaust gas deodorizing device 43 and the wet alkali treatment device 44, etc., and is discharged to the atmosphere after deodorizing and neutralizing.
【００２０】図２及び図３には、廃プラスチックの脱塩
素燃料化装置６１の一例が示されている。同図中、６２
は、圧送部、６３は、該圧送部６２の先端を閉塞する区
画壁６４を介して設けられた熱風加熱室である。FIGS. 2 and 3 show an example of an apparatus 61 for converting waste plastic into dechlorinated fuel. In the figure, 62
Is a hot air supply section, and 63 is a hot air heating chamber provided via a partition wall 64 that closes the tip of the pressure feed section 62.
【００２１】前記圧送部６２は、断面眼鏡形の中空部を
有するケーシング６５、その上部に設けられた前記破砕
された廃プラスチック投入用のホッパー６６、及び投入
された廃プラスチックを、前記区画壁６４に向けて圧縮
しつつ移送する、二本の圧縮スクリュー６７、６８で構
成されている。The pumping section 62 includes a casing 65 having a hollow section having a spectacle-shaped cross section, a hopper 66 for charging the crushed waste plastic provided at an upper portion thereof, and a partition wall 64 for transferring the supplied waste plastic to the partition wall 64. It is composed of two compression screws 67 and 68 which are transported while being compressed toward.
【００２２】さらに、前記二本の圧縮スクリュー６７、
６８の回転軸６７ａ、６８ａが、前記ギアボックス６９
内に延長支持され、該ギアボックス６９内において、前
記回転軸６７ａ、６８ａに歯車７０、７１が設けられ、
それぞれ噛み合わされる。Further, the two compression screws 67,
The rotation shafts 67a, 68a
The gearbox 69 is provided with gears 70, 71 provided on the rotating shafts 67a, 68a.
Each is engaged.
【００２３】そして前記回転軸６７ａ、６８ａの一方、
図示の場合、右側の回転軸６８ａが、前記ギアボックス
６９から突出させられ、減速機等を介して油圧モータや
電動機等の、前記駆動装置Ｍと連結される。And one of the rotating shafts 67a, 68a,
In the case shown in the figure, the right rotating shaft 68a is projected from the gear box 69, and is connected to the driving device M such as a hydraulic motor or an electric motor via a speed reducer or the like.
【００２４】つぎに、前記熱風加熱室６３は、箱形に構
成され、前記熱風発生炉３５からの前記燃焼ガスを内部
に供給する供給口７２、及び前記ガス排出管４２が連結
される排出口７３が、右側面に設けられる。The hot-air heating chamber 63 is formed in a box shape, and has a supply port 72 for supplying the combustion gas from the hot-air generating furnace 35 to the inside, and an exhaust port to which the gas exhaust pipe 42 is connected. 73 is provided on the right side surface.
【００２５】図示の実施の形態では、前記熱風加熱室６
３内に供給された熱風の有する熱量を、無駄にすること
なく有効利用するため、前記熱風加熱炉６３内に後述す
る穴あき管７５に交差して熱風を循環させる、区画ガイ
ド板７４が、設けられている。In the illustrated embodiment, the hot air heating chamber 6
In order to effectively use the amount of heat of the hot air supplied into the hot air 3 without wasting it, a section guide plate 74 that circulates hot air in the hot air heating furnace 63 across a perforated pipe 75 described later, Is provided.
【００２６】すなわち、図２及び図３に示すごとく、前
記熱風加熱室６３内の略中央部に、連通部Ｓをあけて前
記区画ガイド板７４を設け、該区画ガイド板７４で区画
された一方（下流）の隔室６３ａ及び他方（上流）の隔
室６３ｂの前記連通部Ｓと反対側側面に、それぞれ前記
熱風の供給口７２及び排出口７３を設け、前記熱風発生
炉３５から前記供給口７２に供給された熱風が、前記一
方の隔室７３ａから前記他方の隔室７３ｂに循環するよ
うに構成されている。なお、前記区画ガイド板７４は、
一枚に限らず、適数枚、交互に設けて熱風を蛇行させる
ように構成してもよい。That is, as shown in FIGS. 2 and 3, the partition guide plate 74 is provided at a substantially central portion in the hot air heating chamber 63 with a communicating portion S therebetween. A supply port 72 and a discharge port 73 for the hot air are provided on the side of the (downstream) compartment 63a and the other (upstream) compartment 63b on the side opposite to the communication portion S, respectively. The hot air supplied to 72 is configured to circulate from the one compartment 73a to the other compartment 73b. The section guide plate 74 is
Not only one sheet but also an appropriate number of sheets may be alternately provided so as to meander the hot air.
【００２７】つぎに、前記区画壁７４を貫通及び前記熱
風加熱室６３内をほぼ水平に横断して、周囲に適数の穴
７６を有する適数の穴あき管７５が設けられる。なお、
図示の実施の形態のごとく、前記熱風加熱室６３内に前
記区画ガイド板７４を設けた場合には、該区画ガイド板
７４にも、前記穴あき管７５が貫通させられる。Next, an appropriate number of perforated pipes 75 having an appropriate number of holes 76 therearound are provided so as to penetrate the partition wall 74 and substantially horizontally traverse the interior of the hot air heating chamber 63. In addition,
When the partition guide plate 74 is provided in the hot air heating chamber 63 as in the illustrated embodiment, the perforated pipe 75 is also penetrated through the partition guide plate 74.
【００２８】さらに、前記穴あき管７５のそれぞれ内周
面に、凹凸状のスプライン７５ｂを施すと、内部を通過
する廃プラスチックの加熱面積が増大され、加熱効率が
向上させられ、熱分解が迅速且つ効率的に行われる。Further, when the uneven splines 75b are provided on the inner peripheral surfaces of the perforated pipes 75, the heating area of the waste plastic passing therethrough is increased, the heating efficiency is improved, and the thermal decomposition is performed quickly. It is performed efficiently.
【００２９】前記構成の廃プラスチックの脱塩素燃料化
装置６１において、廃プラスチックが、前記圧送部６２
の上部に設けられた前記ホッパー６６から投入される。
投入された前記廃プラスチックは、前記二本の圧縮スク
リュー６７、６８の回転によって、前記区画壁６４に強
く押圧され、同時に擦られ、さらに摩擦熱によって溶融
される。In the waste plastic dechlorination fuel converting apparatus 61 having the above-mentioned structure, the waste plastic is supplied to the pressure feeding section 62.
Is fed from the hopper 66 provided at the upper part of the hopper.
The waste plastic that has been introduced is strongly pressed against the partition wall 64 by the rotation of the two compression screws 67 and 68, is simultaneously rubbed, and is further melted by frictional heat.
【００３０】さらに、前記溶融とともに、前記各穴あき
管７５内に圧入され、前記熱風加熱室６３内において、
１３０〜３６０℃に加熱された前記穴あき管７５内を進
行させられ、それぞれの廃プラスチックの熱分解温度に
おいて熱分解が行われ、分解された塩化水素、塩素ガス
等が、前記穴あき管７５の前記穴７６から排出させられ
る。Further, together with the melting, the molten steel is pressed into each of the perforated pipes 75, and
In the perforated pipe 75 heated to 130 to 360 ° C., pyrolysis is performed at the pyrolysis temperature of each waste plastic, and the decomposed hydrogen chloride, chlorine gas, and the like are transferred to the perforated pipe 75. From the hole 76.
【００３１】そして前記熱分解により生成された前記塩
化水素、塩素ガス等は、熱風加熱室６３内に供給された
燃焼ガスとともに、前記排出口７３から前記脱塩素燃料
化プラントの前記ガス排出管４２を介して、前記排ガス
脱臭装置４３及び前記湿式アルカリ処理装置４４等へ供
給されて、清浄化されて大気に放出される。一方、前記
加熱による熱分解により、塩化水素、塩素ガス等が除去
された前記脱塩素炭化処理が施された廃プラスチック４
１は、前記穴あき管７５の先端部７５ａから排出され
る。The hydrogen chloride, chlorine gas and the like generated by the thermal decomposition together with the combustion gas supplied into the hot air heating chamber 63 are supplied from the outlet 73 to the gas discharge pipe 42 of the dechlorination fuel conversion plant. , Is supplied to the exhaust gas deodorizing device 43 and the wet-type alkaline treatment device 44, etc., and is purified and released to the atmosphere. On the other hand, the waste plastics 4 which have been subjected to the dechlorination and carbonization treatment from which hydrogen chloride, chlorine gas and the like have been removed by the thermal decomposition by heating
1 is discharged from the front end portion 75a of the perforated tube 75.
【００３２】本発明は、前記湿式アルカリ処理装置４４
からの、洗浄排水の処理方法及び装置、具体的には、前
記洗浄排水からノルマルヘキサン抽出成分、ＣＯＤ成分
及びその他の混濁成分を除去する方法及び装置に関す
る。The present invention is directed to the wet-type alkaline processing apparatus 44.
And, more particularly, to a method and an apparatus for removing a normal hexane extraction component, a COD component and other turbid components from the washing wastewater.
【００３３】以下に、図１に基づいて本発明一実施の形
態の装置を説明する。図中、Ａは、前記洗浄排水の供給
管、１は、曝気槽である。該曝気槽１内の底部には、ブ
ロワ２からの空気配管３が配設され、気泡により、前記
洗浄排水の供給管Ａから供給された洗浄排水の曝気が行
われるように構成されている。An apparatus according to an embodiment of the present invention will be described below with reference to FIG. In the figure, A is a supply pipe for the washing drainage, and 1 is an aeration tank. An air pipe 3 from a blower 2 is provided at the bottom in the aeration tank 1 so that the cleaning wastewater supplied from the cleaning wastewater supply pipe A is aerated by air bubbles.
【００３４】つぎに、前記曝気槽１の水面には、ノルマ
ルヘキサン抽出成分及び疎水性混濁成分等の浮上物質の
回収装置４が設けられる。なお、図面実施の形態では、
前記浮上物質の回収装置４を構成するポンプ５に、エマ
ルジョンブレーカー６が連結されている。Next, on the water surface of the aeration tank 1, there is provided an apparatus 4 for collecting floating substances such as a normal hexane extraction component and a hydrophobic turbid component. In the embodiment of the drawings,
An emulsion breaker 6 is connected to a pump 5 constituting the floating substance recovery device 4.
【００３５】該エマルジョンブレーカー６は、前記回収
装置４によって回収されたノルマルヘキサン抽出成分及
び疎水性混濁成分と、水分を、分離し、分離したノルマ
ルヘキサン抽出成分及び疎水性混濁成分を、配管７を介
して回収槽８に導き、さらにポンプ９により外部に排出
して適宜処理するとともに、分離された洗浄排水（水
分）を、配管１０を介して前記曝気槽１に戻す。The emulsion breaker 6 separates the normal hexane extracted component and the hydrophobic turbid component collected by the collecting device 4 from water and the separated normal hexane extracted component and the hydrophobic turbid component, and supplies the separated pipe to the pipe 7. The cleaning water (moisture) is returned to the aeration tank 1 via a pipe 10 while being guided to a collection tank 8 via a pump 9 and discharged to the outside by a pump 9 for appropriate treatment.
【００３６】図中１１は、計量槽であり、前記曝気槽１
から水中ポンプ１２により揚水された、前記洗浄排水の
所定量以上の分を、配管１３を介して前記曝気槽１に循
環させる。そして、前記計量槽１１から一定量の洗浄排
水が、配管１４を通して反応槽１５に供給されるように
構成されている。さらに、該反応槽１５には、硫酸第一
鉄槽１６及び硫酸槽１６ａから、それぞれ硫酸第一鉄及
び硫酸が、供給自在に構成されている。In the figure, reference numeral 11 denotes a measuring tank, and the aeration tank 1
And a predetermined amount or more of the washing wastewater pumped up by the submersible pump 12 is circulated to the aeration tank 1 via a pipe 13. A certain amount of washing wastewater is supplied from the measuring tank 11 to the reaction tank 15 through the pipe 14. Further, the reaction tank 15 is configured so that ferrous sulfate and sulfuric acid can be supplied from a ferrous sulfate tank 16 and a sulfuric acid tank 16a, respectively.
【００３７】さらに前記反応槽１５の下流側に隣接させ
て、該反応槽１５からの処理水が流れ込む、ｐＨ調整槽
１７が、設けられる。図面実施の形態では、底部を開放
した堰１８を介して、前記ｐＨ調整槽１７が、前記反応
槽１５に隣接して設けられている。そして、前記ｐＨ調
整槽１７には、アルカリ槽１９から、アルカリ、具体的
には苛性ソーダが、供給自在に構成される。Further, adjacent to the downstream side of the reaction tank 15, a pH adjusting tank 17 into which the treated water from the reaction tank 15 flows is provided. In the embodiment shown in the drawings, the pH adjustment tank 17 is provided adjacent to the reaction tank 15 via a weir 18 having an open bottom. An alkali, specifically, caustic soda, is supplied to the pH adjusting tank 17 from an alkali tank 19 so as to be freely supplied.
【００３８】さらに、前記ｐＨ調整槽１７の下流側に隣
接させて、該ｐＨ調整槽１７からの処理水が流れ込む、
凝集槽２０が設けられる。図面実施の形態では、上端を
低くした堰２１を介して、前記凝集槽２０が、前記ｐＨ
調整槽１７の下流側に隣接して設けられている。そし
て、前記凝集槽２０には、ポリマー槽２２から、高分子
凝集助剤が供給自在に構成される。Further, adjacent to the downstream side of the pH adjusting tank 17, the treated water from the pH adjusting tank 17 flows.
A coagulation tank 20 is provided. In the embodiment shown in the drawings, the flocculation tank 20 is connected to the pH controller via a weir 21 having a lower end.
It is provided adjacent to the downstream side of the adjustment tank 17. The coagulation tank 20 is configured so that a polymer coagulation aid can be freely supplied from the polymer tank 22.
【００３９】前記のごとく、図面実施の形態では、前記
反応槽１５、前記ｐＨ調整槽１７及び前記凝集槽２０へ
の処理水の流れを、ポンプを使用せずに、前記堰１８及
び２１を設けて、液面差を利用している。したがって、
ポンプが不要であり経済的であるとともに、ポンプの故
障等に伴う、処理工程中断のおそれもない。As described above, in the embodiment shown in the drawings, the flow of the treated water to the reaction tank 15, the pH adjustment tank 17 and the flocculation tank 20 is provided by the weirs 18 and 21 without using a pump. And use the liquid level difference. Therefore,
A pump is unnecessary and economical, and there is no possibility of interruption of a processing step due to a failure of the pump.
【００４０】さらに前記凝集槽２０からの処理水が、配
管２３を介して沈殿槽２４に供給される。該沈殿槽２４
は、漏斗状底部を有し、下端に排水ポンプ２５が連結さ
れ、適時に沈殿物を排出できるように構成されている。Further, the treated water from the coagulation tank 20 is supplied to a settling tank 24 via a pipe 23. The sedimentation tank 24
Has a funnel-shaped bottom, is connected to a drainage pump 25 at the lower end, and is configured to discharge sediment in a timely manner.
【００４１】なお、図面実施の形態では、前記沈殿槽２
４の上澄みを、直接活性炭槽３０に導入することなく、
好ましい実施の形態として、配管２６を介して揚水槽２
７に導入し、さらに、揚水ポンプ２８により砂濾過槽２
９に導入した後に、最終装置である前記活性炭槽３０に
導入し、排出管Ｂから放流される構成になっている。In the embodiment shown in FIG.
4 without introducing the supernatant directly into the activated carbon tank 30.
As a preferred embodiment, the pumping tank 2
7 and the sand filtration tank 2
After being introduced into 9, it is introduced into the activated carbon tank 30 which is the final device, and is discharged from the discharge pipe B.
【００４２】前記の装置においては、前記曝気槽１にお
いて、曝気により、洗浄排水中の不飽和有機化合物が酸
化及び飽和させられて、ＣＯＤ成分濃度が低減させら
れ、水面には、ノルマルヘキサン抽出成分及び疎水性混
濁成分が浮上させられ、該ノルマルヘキサン抽出成分
が、油分として、及び疎水性混濁成分の大部分が、前記
回収装置４によって回収され、前記ポンプ５を介して前
記エマルジョンブレーカー６に導かれる。In the aforesaid apparatus, the aeration tank 1 oxidizes and saturates the unsaturated organic compounds in the washing waste water by aeration, thereby reducing the COD component concentration, and the water surface contains the normal hexane extraction component. And the normal hexane extraction component is recovered as oil and most of the hydrophobic turbid component is recovered by the recovery device 4 and guided to the emulsion breaker 6 via the pump 5. I will
【００４３】そして、ノルマルヘキサン抽出成分及び疎
水性混濁成分と同時に回収された洗浄排水が分離され、
分離されたノルマルヘキサン抽出成分及び疎水性混濁成
分が、前記配管７を介して前記回収槽８に供給され、さ
らに、前記ポンプ９により外部に排出され、分離された
洗浄排水は、前記曝気槽１に戻される。Then, the washing wastewater recovered simultaneously with the normal hexane extraction component and the hydrophobic turbid component is separated,
The separated normal hexane extraction component and the hydrophobic turbid component are supplied to the recovery tank 8 via the pipe 7 and further discharged to the outside by the pump 9. The separated washing wastewater is supplied to the aeration tank 1. Is returned to.
【００４４】つぎに、前記曝気槽１の処理水が、前記水
中ポンプ１２によって前記計量槽１１に供給され、さら
に、前記配管１４を介して前記反応槽１５に供給され
る。そして該反応槽１５内に、前記硫酸槽１６ａから適
量の硫酸が供給され、ｐＨ値が、４．０〜７．０の酸性
度に調整され、さらに、前記硫酸第一鉄槽１６から硫酸
第一鉄が加えられて、処理水中に残存する疎水性混濁成
分が、ミクロフロック化される。Next, the treated water in the aeration tank 1 is supplied to the measuring tank 11 by the submersible pump 12 and further supplied to the reaction tank 15 via the pipe 14. Then, an appropriate amount of sulfuric acid is supplied into the reaction tank 15 from the sulfuric acid tank 16a, the pH value is adjusted to an acidity of 4.0 to 7.0, and further, the sulfuric acid is added from the ferrous sulfate tank 16 to the pH value. With the addition of ferrous iron, the hydrophobic turbid components remaining in the treated water are microflocculated.
【００４５】つぎに、前記反応槽１５の処理水が、前記
堰１８の下方を通って、前記ｐＨ調整槽１７に流れ込
む。そして該ｐＨ調整槽１７内に前記アルカリ槽１９か
ら適量の苛性ソーダが供給されて、ｐＨ値が調整され、
さらに、ｐＨ調整槽１７の処理水が、前記堰２１の上方
から前記凝集槽２０に流れ込む。そして該凝集槽２０内
に、前記ポリマー槽２２から適量の高分子凝集助剤が供
給され、前記ミクロフロックが凝集される。Next, the treated water in the reaction tank 15 flows under the weir 18 into the pH adjustment tank 17. Then, an appropriate amount of caustic soda is supplied from the alkaline tank 19 into the pH adjusting tank 17 to adjust the pH value,
Further, the treated water in the pH adjustment tank 17 flows into the flocculation tank 20 from above the weir 21. Then, an appropriate amount of a polymer coagulant is supplied from the polymer tank 22 into the coagulation tank 20 to coagulate the micro flocs.
【００４６】その後、前記凝集槽２０の処理水が、前記
配管２３を介して前記沈殿槽２４に供給され、凝集され
た疎水性混濁成分が沈殿分離させられる。そして前記沈
殿槽２４の上澄みが、前記配管２６を介して、前記揚水
槽２７に導かれ、さらに、前記ポンプ２８によって、前
記砂濾過槽２９に導入される。Thereafter, the treated water in the flocculation tank 20 is supplied to the sedimentation tank 24 through the pipe 23, and the flocculated hydrophobic turbid components are precipitated and separated. Then, the supernatant of the sedimentation tank 24 is guided to the pumping tank 27 via the pipe 26 and further introduced into the sand filtration tank 29 by the pump 28.
【００４７】そして、該砂濾過槽２９の砂間を通過させ
られた濾過水が、前記活性炭槽３０に導入され、微量に
残存しているノルマルヘキサン抽出成分、ＣＯＤ成分及
び親水性ゾルが吸着除去され、前記排出管Ｂから放流さ
れる。Then, the filtered water passed between the sands of the sand filter tank 29 is introduced into the activated carbon tank 30 to remove and remove trace amounts of the normal hexane extraction component, the COD component and the hydrophilic sol remaining in trace amounts. And discharged from the discharge pipe B.
【００４８】[0048]
【発明の効果】前記本発明の処理方法によれば、脱塩素
燃料化工程で生成されたガスの洗浄排水中のノルマルヘ
キサン抽出成分、ＣＯＤ成分、その他の混濁成分を、有
効に除去することができ、また、本発明の処理装置によ
れば、前記除去工程を、連続的に行うことがが可能であ
る。According to the treatment method of the present invention, it is possible to effectively remove the normal hexane extraction component, the COD component, and other turbid components in the washing wastewater of the gas generated in the dechlorination fuel conversion step. According to the processing apparatus of the present invention, the removing step can be performed continuously.
【図１】本発明の廃プラスチック脱塩素炭工程で生成さ
れた排ガスの洗浄排水処理装置のフローチャートであ
る。FIG. 1 is a flowchart of an apparatus for cleaning and draining waste gas generated in a waste plastic dechlorinated carbon step of the present invention.
【図２】廃プラスチックの脱塩炭化装置の一部を破断し
た平面図である。FIG. 2 is a plan view in which a part of a desalting and carbonizing device for waste plastic is cut away.
【図３】図２の３−３線矢視断面図である。FIG. 3 is a sectional view taken along line 3-3 of FIG. 2;
【図４】図２に示した廃プラスチックの脱塩炭化装置を
含む廃プラスチックの脱塩炭化処理プラントの一例を示
すフローチャートである。FIG. 4 is a flowchart showing an example of a waste plastic desalination and carbonization plant including the waste plastic desalination and carbonization apparatus shown in FIG. 2;
１ 曝気槽 ４ 回収装置 ６ エマルジョンブレーカー １１ 計量槽 １５ 反応槽 １７ ｐＨ調整槽 ２０ 凝集槽 ２４ 沈殿槽 ２９ 砂濾過槽 ３０ 活性炭槽 Reference Signs List 1 aeration tank 4 recovery device 6 emulsion breaker 11 measuring tank 15 reaction tank 17 pH adjustment tank 20 coagulation tank 24 sedimentation tank 29 sand filtration tank 30 activated carbon tank
フロントページの続き (51)Int.Cl.7 識別記号 ＦＩ テーマコート゛(参考） Ｂ０１Ｄ 53/34 Ｃ０２Ｆ 1/56 Ｋ 53/77 1/58 Ａ Ｃ０２Ｆ 1/56 Ｂ２９Ｂ 17/00 ＺＡＢ 1/58 Ｃ１０Ｇ 1/10 ＺＡＢ // Ｂ２９Ｂ 17/00 ＺＡＢ Ｂ０１Ｄ 53/34 Ｅ Ｃ１０Ｇ 1/10 ＺＡＢ Ｂ２９Ｋ 105:26 (72)発明者 中村 雄志 東京都青梅市末広町一丁目７番地２ 株式 会社共立内 (72)発明者 丹所 哲夫 東京都青梅市末広町一丁目７番地２ 株式 会社共立内 (72)発明者 笠井 武 東京都杉並区高円寺北２丁目37番14号スタ ーション・アドＱ102号 株式会社三共プ ロセス・サービス内 (72)発明者 関 勝四郎 埼玉県久喜市中央一丁目10番11号 株式会 社関商店内 (72)発明者 釜瀬 俊英 千葉県八千代市上高野1780番地 川崎重工 業株式会社内 Ｆターム(参考） 4D002 AA18 AA19 AB01 AB02 AC10 BA02 DA02 DA12 FA04 4D038 AA08 AB08 BB04 BB06 BB17 BB18 4D062 BA19 BB12 CA20 DA15 DB01 EA13 EA15 EA16 EA32 FA13 FA16 FA22 4F201 BA05 BC01 BC02 BC10 BC12 BC25 BN44 BP01 BP08 BP23 BP27 BP31 BP40 4H029 CA16 Continued on the front page (51) Int.Cl. 7 Identification symbol FI Theme coat II (reference) B01D 53/34 C02F 1/56 K 53/77 1/58 A C02F 1/56 B29B 17/00 ZAB 1/58 C10G 1 / 10 ZAB // B29B 17/00 ZAB B01D 53/34 E C10G 1/10 ZAB B29K 105: 26 (72) Inventor Yuji Nakamura 1-7-2 Suehirocho, Ome-shi, Tokyo 2 (Kyoritsu, Japan) (72) Invention Tetsuo Tansho 1-7-2 Suehirocho, Ome-shi, Tokyo Inside the Kyoritsu Co., Ltd. (72) Inventor Takeshi Kasai 2-37-14 Koenji Kita Kita, Suginami-ku, Tokyo Station Ad Q102 Sankyo Process Co., Ltd. Within the service (72) Inventor Katsushiro Seki 1-10-11 Chuo, Kuki City, Saitama Prefecture Inside the Seki Store Co., Ltd. (72) Inventor Toshihide Kamase 1780 Kamikono, Yachiyo City, Chiba Prefecture Kawasaki Heavy Industries Ltd.F-term (Reference) 4D002 AA18 AA19 AB01 AB02 AC10 BA02 DA02 DA12 FA04 4D038 AA08 AB08 BB04 BB06 BB17 BB18 4D062 BA19 BB12 CA20 DA15 DB01 EA13 EA15 EA16 EA32 FA13 FA16 FA22 4F201 BA05 BC01 BC02 BC10 BC12 BC25 BN44 BP01 BP08 BP23 BP27 BP31 BP40 4H029 CA16
Claims (5)
和させてＣＯＤ成分濃度を低減させると同時に疎水性混
濁成分とノルマルヘキサン抽出成分を微細気泡表面に付
着浮上させて回収する曝気工程、硫酸を加えてｐＨ値を
調整した後、硫酸第一鉄を加えて残存疎水性混濁成分を
ミクロフロック化する工程、アルカリ添加によるｐＨ値
調整工程、高分子凝集助剤による前記ミクロフロック化
された疎水性混濁成分を凝集させる工程、凝集された前
記疎水性混濁成分を沈殿分離する工程、及び残存するノ
ルマルヘキサン抽出成分、ＣＯＤ成分及び親水性ゾルを
活性炭により吸着除去する工程と、からなることを特徴
とする廃プラスチック脱塩素燃料化工程で生成された排
ガスの洗浄排水処理方法。An aeration step of oxidizing and saturating unsaturated compounds in washing waste water to reduce the concentration of COD components and simultaneously recovering a hydrophobic turbid component and a normal hexane extract component by adhering and floating on the surface of fine bubbles; To adjust the pH value, adding ferrous sulfate to microfloc the remaining hydrophobic turbid component, adjusting the pH value by adding an alkali, and adding the polymer flocculant to the microfloc hydrophobicity. Aggregating the hydrophobic turbid component, sedimenting and separating the agglomerated hydrophobic turbid component, and adsorbing and removing the remaining normal hexane extraction component, COD component and hydrophilic sol with activated carbon. Cleaning wastewater treatment method for waste gas generated in the waste plastic dechlorination fuel conversion process.
その水面に設けられた浮上物質の回収装置（４）、前記
曝気槽（１）から浮上物質が除去された前記洗浄排水が
順次供給される硫酸及び硫酸第一鉄供給自在の反応槽
（１５）、アルカリ供給自在のｐＨ調整槽（１７）、高
分子凝集助剤供給自在の凝集槽（２０）、沈殿槽（２
４）、及び活性炭槽（３０）と、からなることを特徴と
する廃プラスチック脱塩素燃料化工程で生成された排ガ
スの洗浄排水処理装置。2. An aeration tank (1) to which cleaning wastewater is supplied, a floating substance recovery device (4) provided on the surface of the water, and the cleaning wastewater from which the floating substance is removed from the aeration tank (1) is sequentially discharged. Reaction tank (15) capable of supplying supplied sulfuric acid and ferrous sulfate, pH adjusting tank (17) capable of supplying alkali, flocculating tank (20) capable of supplying a polymer flocculant, and sedimentation tank (2)
4) and an activated carbon tank (30).
ジョンブレ−カ−（６）が連結され、疎水性混濁成分及
びノルマルヘキサン抽出成分と水分を分離するととも
に、疎水性混濁成分及びノルマルヘキサン抽出成分を外
部に排出し、水分を前記曝気槽（１）に戻す請求項２に
記載の廃プラスチック脱塩素燃料化工程で生成された排
ガスの洗浄排水処理装置。3. An emulsion breaker (6) is connected to the flotation substance recovery device (4) to separate water from the hydrophobic turbid component and the normal hexane extract component, and to separate the hydrophobic turbid component and the normal hexane component. The apparatus for cleaning and discharging waste gas generated in the process of converting waste plastic into dechlorinated fuel according to claim 2, wherein the extracted component is discharged to the outside and water is returned to the aeration tank (1).
間に計量槽（１１）を介在させた請求項２又は３に記載
の廃プラスチック脱塩素燃料化工程で生成された排ガス
の洗浄排水処理装置。4. The aeration tank (1) and the reaction tank (15)
4. The apparatus for cleaning and discharging waste gas generated in the process of converting waste plastic into dechlorinated fuel according to claim 2, wherein a measuring tank (11) is interposed therebetween.
０）間に砂濾過槽（２９）を介在させた請求項２、３又
は４に記載の廃プラスチック脱塩素燃料化工程で生成さ
れた排ガス洗浄排水処理装置。5. The sedimentation tank (24) and the activated carbon tank (3)
The exhaust gas cleaning wastewater treatment apparatus produced in the waste plastic dechlorination fuel conversion process according to claim 2, wherein a sand filtration tank (29) is interposed between 0 and 0.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP24753398A JP4197063B2 (en) | 1998-09-01 | 1998-09-01 | Waste water treatment method and apparatus for exhaust gas generated in waste plastic dechlorination process |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP24753398A JP4197063B2 (en) | 1998-09-01 | 1998-09-01 | Waste water treatment method and apparatus for exhaust gas generated in waste plastic dechlorination process |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JP2000070995A true JP2000070995A (en) | 2000-03-07 |
| JP4197063B2 JP4197063B2 (en) | 2008-12-17 |
Family
ID=17164921
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP24753398A Expired - Fee Related JP4197063B2 (en) | 1998-09-01 | 1998-09-01 | Waste water treatment method and apparatus for exhaust gas generated in waste plastic dechlorination process |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP4197063B2 (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR101199832B1 (en) | 2012-05-10 | 2012-11-09 | 조동국 | Washing device of crushing waste plastic and recycling method of washing water |
| CN107417025A (en) * | 2017-08-10 | 2017-12-01 | 西安瑞联新材料股份有限公司 | A kind of processing method of folic acid sulfur waste sour water |
| CN111744298A (en) * | 2020-07-09 | 2020-10-09 | 袁思田 | Plastic particle production system equipment for reinforced composite plastic material |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102910765B (en) * | 2012-11-20 | 2013-12-04 | 安徽新天环保科技有限公司 | Demulsifying and flocculating treatment method of machining cutting fluid sewage water |
| CN104843930B (en) * | 2015-04-07 | 2017-05-10 | 安徽建筑大学 | Vacuum pump wastewater treatment system and use method thereof |
| CN105693015A (en) * | 2016-01-27 | 2016-06-22 | 山东省环保产业股份有限公司 | Treatment method of cutting fluid wastewater of automobile engine |
-
1998
- 1998-09-01 JP JP24753398A patent/JP4197063B2/en not_active Expired - Fee Related
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR101199832B1 (en) | 2012-05-10 | 2012-11-09 | 조동국 | Washing device of crushing waste plastic and recycling method of washing water |
| CN107417025A (en) * | 2017-08-10 | 2017-12-01 | 西安瑞联新材料股份有限公司 | A kind of processing method of folic acid sulfur waste sour water |
| CN111744298A (en) * | 2020-07-09 | 2020-10-09 | 袁思田 | Plastic particle production system equipment for reinforced composite plastic material |
Also Published As
| Publication number | Publication date |
|---|---|
| JP4197063B2 (en) | 2008-12-17 |
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