JPH02212591A - Method for thermal decomposition of waste material - Google Patents
Method for thermal decomposition of waste materialInfo
- Publication number
- JPH02212591A JPH02212591A JP3168289A JP3168289A JPH02212591A JP H02212591 A JPH02212591 A JP H02212591A JP 3168289 A JP3168289 A JP 3168289A JP 3168289 A JP3168289 A JP 3168289A JP H02212591 A JPH02212591 A JP H02212591A
- Authority
- JP
- Japan
- Prior art keywords
- reaction tank
- treatment
- decomposition
- tank
- distribution pipe
- 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.)
- Pending
Links
- 238000000034 method Methods 0.000 title claims abstract description 35
- 239000002699 waste material Substances 0.000 title claims abstract description 20
- 238000005979 thermal decomposition reaction Methods 0.000 title claims abstract description 13
- 238000000354 decomposition reaction Methods 0.000 claims abstract description 48
- 238000010438 heat treatment Methods 0.000 claims abstract description 34
- 238000003860 storage Methods 0.000 claims abstract description 7
- 239000007788 liquid Substances 0.000 claims abstract description 6
- 238000002844 melting Methods 0.000 claims abstract description 5
- 230000008018 melting Effects 0.000 claims abstract description 5
- 239000000463 material Substances 0.000 claims description 27
- 238000009826 distribution Methods 0.000 claims description 23
- 238000000197 pyrolysis Methods 0.000 claims description 10
- 238000006243 chemical reaction Methods 0.000 claims description 4
- 238000010309 melting process Methods 0.000 claims description 3
- 238000000746 purification Methods 0.000 claims description 2
- 238000007599 discharging Methods 0.000 claims 2
- 239000012943 hotmelt Substances 0.000 claims 1
- 239000002994 raw material Substances 0.000 abstract description 12
- 238000011084 recovery Methods 0.000 abstract description 8
- 238000004939 coking Methods 0.000 abstract description 2
- 229920000642 polymer Polymers 0.000 abstract description 2
- 239000007789 gas Substances 0.000 description 11
- 229910052799 carbon Inorganic materials 0.000 description 10
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 9
- 239000000047 product Substances 0.000 description 9
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 9
- 239000004215 Carbon black (E152) Substances 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- 229930195733 hydrocarbon Natural products 0.000 description 4
- 150000002430 hydrocarbons Chemical class 0.000 description 4
- 238000012545 processing Methods 0.000 description 4
- 238000002485 combustion reaction Methods 0.000 description 3
- 238000007796 conventional method Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000012546 transfer Methods 0.000 description 2
- 230000002159 abnormal effect Effects 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 239000004480 active ingredient Substances 0.000 description 1
- 238000013019 agitation Methods 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 239000000567 combustion gas Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 238000005520 cutting process Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 239000012528 membrane Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 239000002244 precipitate Substances 0.000 description 1
- 238000007789 sealing Methods 0.000 description 1
- 239000010802 sludge Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
Description
【発明の詳細な説明】
〔産業上の利用分野〕
本発明は、廃棄物、特に廃油、高粘度廃油、ローポリマ
ー等を熱分解し炭化水素油を回収する処理方法に関する
ものである。DETAILED DESCRIPTION OF THE INVENTION [Industrial Application Field] The present invention relates to a treatment method for thermally decomposing waste, particularly waste oil, high viscosity waste oil, low polymer, etc., to recover hydrocarbon oil.
この種廃棄物の処理として直接焼却処理や埋め立て処理
をすることは二次公害が発生することから望ましくない
、そこで熱分解処理し炭化水素油等の有効成分を回収す
る溶融浴槽すなわちポリノ（入力式（特公昭６０−１４
０４３７号）や！（イブスチーム方式（特公昭５８−２
９８３３号）等が開発されている。It is undesirable to directly incinerate or landfill this kind of waste because it causes secondary pollution.Therefore, thermal decomposition treatment is carried out to recover active ingredients such as hydrocarbon oil, which is called a molten bath or porino (input type). (Tokuko Showa 60-14
No. 0437) Ya! (Evesteam method (Special public service 58-2
No. 9833) etc. have been developed.
ところで、熱分解で最も重要な要素は、加熱技術であっ
て外温と内温の温度差（八Ｔ）が大きい円熟交換効率は
高いが１反対にカーボンの発生は多くなり分解が均一に
行われないためローカルヒーティングの原因となってい
た。またガス発生量（非凝縮ガス）が多く生成油の回収
率の低下をｔｒＩ来する１種々の欠点を解消する必要が
ある。By the way, the most important element in pyrolysis is the heating technology.The temperature difference between the outside temperature and the inside temperature (8T) is large, which increases the efficiency of mature exchange, but on the other hand, the generation of carbon increases and decomposition is not carried out uniformly. This caused local heating. In addition, it is necessary to eliminate various drawbacks such as a large amount of gas generation (non-condensable gas) and a decrease in the recovery rate of produced oil.
しかしながら、従来の方法では原料の連続供給方法、５
！！生するカーボンの処理がネト分なため分解油の回収
効率が低く、また分解反応槽内に発生するカーボンや残
漬物が堆積し連続的に運転することが困短なため運転費
等が高くなり不経済なため実用化され雉いものであった
。However, in the conventional method, continuous supply of raw materials,
! ! The recovery efficiency of cracked oil is low because the carbon produced is treated in a net manner, and the carbon and residue generated in the cracking reaction tank accumulates, making continuous operation difficult and short, resulting in high operating costs. It was not put into practical use because it was uneconomical.
すなわち、ポリバス方式のような外部加熱方式では、処
理は一定量毎にしか行うことができないので１に！！運
転はできず不経済であり、また八゛ｒを大きくして攪半
を強化してもカーボンの発生を防止することはできない
ため伝熱効率を低下してしまい不経済なものであった。In other words, with an external heating method such as the polybath method, processing can only be performed for each fixed amount, so 1! ! It was uneconomical to operate, and even if the agitation was strengthened by increasing 8r, the generation of carbon could not be prevented, resulting in a decrease in heat transfer efficiency, making it uneconomical.
また、パイプスチーム方式であっても外部加熱によるパ
イプ内へのカーボンの堆積は避けることは出来ないもの
であった。Further, even with the pipe steam method, the accumulation of carbon inside the pipe due to external heating cannot be avoided.
また、流動層方式の場合には、生成物への燃焼排ガスの
混入があり生成物の品質が低ドすることとなり分解反応
槽を精留塔に直結できないという構造上の欠点があると
ともに、燃焼１トガスが混入するため非凝縮ガスの有効
利用に限界があった。In addition, in the case of the fluidized bed method, there is a structural disadvantage in that the decomposition reaction tank cannot be directly connected to the rectification column, as the quality of the product deteriorates due to the mixing of combustion exhaust gas into the product. There was a limit to the effective use of non-condensable gas because 1 gas was mixed in.
本発明は、このような欠点を解消すべくしたものであっ
て、熱溶融処理後、連続的に分解反応槽１に供給した処
理物を、加熱炉３内に内装した流通パイプ５に送入して
加熱すると共に、一部をガス化しつつパイプ５内を３
ｍ／ｓｅｃ以上の流速で流通させ分解反応槽１に排出し
てなる方法である。The present invention is intended to eliminate such drawbacks, and after the heat melting process, the treated material that has been continuously supplied to the decomposition reaction tank 1 is fed into the distribution pipe 5 installed in the heating furnace 3. At the same time, the inside of the pipe 5 is heated by gasifying a part of it.
This is a method in which the water is passed through the water at a flow rate of m/sec or higher and discharged into the decomposition reaction tank 1.
また第２の発明方法として、廃棄物を溶融槽１２内に投
入し熱溶融する工程と１Ｍ熱溶融処理工程で溶融された
ｌｆ！融処理物を貯蔵する貯蔵工程でｌｒ？蔵された溶
融処理物を分解反応槽１内に連続的に供給した処理物を
、放出口５ｂ、送入口５ａとなる端部を分解反応槽１の
側壁の］二下面に連接すると共に加熱炉３内に内装した
流通パイプ５内を３ｍ１ｓｅｃ以上の流速で流通する熱
分解工程と、該熱分解工程で加熱された生成物を前記分
解反応槽ｌ内に放出して精製処理する工程とからなる方
法である。Further, as a second method of the invention, the lf! lr in the storage process of storing the melted product? The stored molten processed material is continuously fed into the decomposition reaction tank 1, and the end portions which will become the discharge port 5b and the inlet port 5a are connected to the bottom surface of the side wall of the decomposition reaction tank 1, and the heated product is placed in a heating furnace. The process consists of a thermal decomposition process in which the flow rate is at least 3 ml/sec through a distribution pipe 5 installed in the thermal decomposition process, and a process in which the heated product in the thermal decomposition process is discharged into the decomposition reaction tank l for purification treatment. It's a method.
本発明は、上記のような方法によりなるものであるので
以ドのような作用がある。Since the present invention is based on the method described above, it has the following effects.
この場合、流通パイプ５内での処理物の加熱温度を４１
０〜４６０℃とすることが回収油の回収効率が高くなり
望ましい。In this case, the heating temperature of the processed material in the distribution pipe 5 is set to 41
It is desirable that the temperature be 0 to 460°C, as this will increase the recovery efficiency of the recovered oil.
本発明の方法では１分解反応槽ｌと処理物を加熱する加
熱炉３とに分割しているので後処理が容易であるだけで
なく、熱溶融した処理物は、−旦分解反応槽１に供給し
た後、加熱炉３内に内装した流通パイプ５に送−り込ま
れ一部をガス化しつつ通過し分解反応槽ｌに送り込まれ
、この分解反応槽ｌ内で加熱処理物は完全にガス化する
こととなるので内部等の危険がなく安心して連続運転が
出来る。Since the method of the present invention is divided into one decomposition reaction tank 1 and a heating furnace 3 for heating the processed material, not only is the post-treatment easy, but the heat-molten processed material is first transferred to the decomposition reaction tank 1. After being supplied, the material is fed into the distribution pipe 5 installed in the heating furnace 3, passes through it while being partially gasified, and is fed into the decomposition reaction tank 1, where the heated material is completely converted to gas. , so continuous operation can be carried out with peace of mind without any internal danger.
また、処理物は、流通パイプ５内を３１／ｓａｃ以上の
流速で通過するためパイプの内壁面へのコーキングをほ
ぼ完全に防止することが出来るので安定した処理能力の
低丁もなく連続的な運転が可能となる。In addition, since the processed material passes through the distribution pipe 5 at a flow rate of 31/sac or more, caulking on the inner wall surface of the pipe can be almost completely prevented, so there is no drop in stable processing capacity and continuous processing is possible. Driving becomes possible.
更にまた、加熱炉３内には、端部が前記分解反応＃ＦＩ
と連通している耐熱性のある流通パイプ５を内装してお
り、処理物は流通パイプ５内を高速で流通するようにし
ているので、ΔＴが大きい状態でかつ堺膜係数の効率を
高め、総括伝熱係数を驚異的に向りさせると共に最大の
問題点であったカーボンの発生を防止しかつ分解を均一
化できるためローカルヒーティングの発生を防ぐ結果生
成油の回収率を８０ｗｔ％以上にすることが出来ること
となった。Furthermore, in the heating furnace 3, the end portion is connected to the decomposition reaction #FI.
A heat-resistant distribution pipe 5 is installed inside which communicates with the flow pipe 5, and the processed material is allowed to flow through the distribution pipe 5 at high speed, so that the ΔT is large and the efficiency of the Sakai membrane coefficient is increased. In addition to dramatically improving the overall heat transfer coefficient, it also prevents the generation of carbon, which was the biggest problem, and homogenizes decomposition, thereby preventing the occurrence of local heating and increasing the recovery rate of produced oil to over 80wt%. It became possible to do so.
廃棄物は、原料貯蔵槽１４内で加熱処理していると水分
や軽質油等の不純物が蒸発処理された処理物を分解反応
槽１に供給されることとなり、より良質の炭化水素油の
回収が可能となる。When the waste is heat-treated in the raw material storage tank 14, the treated product from which impurities such as water and light oil have been evaporated is supplied to the decomposition reaction tank 1, and higher quality hydrocarbon oil is recovered. becomes possible.
また１分解反応槽１内では分解残漬は比重値により底部
に沈澱することとなるが、その沈澱物を液状混合状態で
連続的に槽外に抜き取ることにより分解反応槽１内は常
に正常な状態を保つことが出来る。In addition, in the decomposition reaction tank 1, the decomposition residue will settle to the bottom depending on the specific gravity, but by continuously extracting the precipitate out of the tank in a liquid mixed state, the inside of the decomposition reaction tank 1 will always be normal. It is possible to maintain the condition.
熱分解湿度は、加熱炉３の出口湿度で制御して操作を行
うことにより連Ｍ運転を行っても流通パイプ５にカーボ
ンの堆１１１がないので長持１ｆｔｌ一定した条件で加
熱でき、安定した回収率を保つことが出来る。The pyrolysis humidity is controlled by the outlet humidity of the heating furnace 3, and even if continuous M operation is performed, there is no carbon deposit 111 in the distribution pipe 5, so 1 ftl can be heated under constant conditions for a long time, resulting in stable recovery. It is possible to maintain the rate.
（実施例）
次に本発明の実施例について図面を参照しながら説明す
る。(Example) Next, an example of the present invention will be described with reference to the drawings.
１１は、溶融槽１２を持った〃χ料命命断装置あって原
料貯蔵槽１４と供給ポンプ１３を介して連設している。Reference numeral 11 denotes a material life cutting device having a melting tank 12, which is connected to a raw material storage tank 14 via a supply pump 13.
１は１分解反応槽であって、前記原料貯蔵Ｍ１４と原料
供給ポンプ１５を介して連接されている、分解反応槽ｌ
の底部には分解槽＠環ポンプ８を連接し濾過器９を介し
て分解反応槽１に循環させて分解反応槽１の内部温度を
均一化するようにしている。そして、スラッジの一部は
′Ｊ！！続的に槽外へ排出しつるように分解槽循環ポン
プ８と濾過器９間にはバルブ１．６．１７を連接してい
る。1 is a decomposition reaction tank 1, which is connected to the raw material storage M14 via a raw material supply pump 15.
A decomposition tank@ring pump 8 is connected to the bottom of the decomposition tank and circulates it to the decomposition reaction tank 1 through a filter 9 to equalize the internal temperature of the decomposition reaction tank 1. And some of the sludge is 'J! ! A valve 1.6.17 is connected between the decomposition tank circulation pump 8 and the filter 9 so as to continuously discharge the water out of the tank.
３は、加熱炉でド部に燃焼室３ａを有す外筒４ａの略中
央部分に底部を開口した内筒４を立設している。外筒４
ａ内には９両端部が分解反応槽１に連設されト方より」
二部に向けて螺旋状に羅闘している流通パイプ５を内装
している。Reference numeral 3 is a heating furnace, and an inner cylinder 4 having an open bottom is provided upright at approximately the center of an outer cylinder 4a having a combustion chamber 3a at the corner thereof. Outer cylinder 4
Inside a, both ends of 9 are connected to the decomposition reaction tank 1, and from the side of 9.
A distribution pipe 5 spirally spiraling toward the second part is installed inside.
そして、該流通パイプ５には、高速循環ポンプ６によっ
て分解反応槽Ｉの下方より処理物が送り込まれ、該処理
物は４１０〜４６０℃に加熱され、流通パイプ５内を３
ｍ／ｓｅｃ以上の流速で流通するようにしている。そ
して、パイプ５内でガス化雰囲気となった処理物は、パ
イプ５の放出口５ｂより分解反応Ｍ１の上部に放出され
＝−気にガス化し熱分解する。そして生成物は上部出口
より前記分解反応Ｍ１のに部に放出される。Then, the processed material is fed into the distribution pipe 5 from below the decomposition reaction tank I by a high-speed circulation pump 6, and the processed material is heated to 410 to 460°C.
It is made to flow at a flow rate of m/sec or more. The treated material, which has become a gasified atmosphere within the pipe 5, is discharged from the discharge port 5b of the pipe 5 to the upper part of the decomposition reaction M1, and is gasified and thermally decomposed. The product is then discharged from the upper outlet into the decomposition reaction M1.
また１分解反応槽１と加熱が３との間の循環ライン中に
は、濾過装置７を設は流通パイプ５内にコーキングの付
着を防止しつるようにしている。A filtration device 7 is installed in the circulation line between the decomposition reaction tank 1 and the heating device 3 to prevent coking from adhering to the distribution pipe 5.
更にまた。内筒４の頂部に空気抜き孔４ｂを設けること
により加熱炉３内の不足の酸素を供給できるので加熱効
率を高めるこ・とができ、また内筒４のト部より冷却ｍ
の空気が流入し易くなり内筒４の内壁面を冷却され内壁
面の歪み防止を回ることができる。Yet again. By providing an air vent hole 4b at the top of the inner cylinder 4, insufficient oxygen in the heating furnace 3 can be supplied, thereby increasing heating efficiency.
This makes it easier for air to flow in, thereby cooling the inner wall surface of the inner cylinder 4 and preventing distortion of the inner wall surface.
このようにして分解反応槽ｌに放出された精製ガスは精
留塔２に送り込まれて精製されるが、このとき精留塔２
の塔偵温度を２７０〜３５０℃の範囲に制御することに
よりＡｆｆｌ油相当の高品質の炭化水素油を得ることが
出来る７このガス状生成物は、コンデンサー２２で冷却
し、液化した生成油は受液槽２３に回収°される。The purified gas released into the decomposition reaction tank 1 in this way is sent to the rectification column 2 and purified;
By controlling the tower temperature in the range of 270 to 350°C, high quality hydrocarbon oil equivalent to Affl oil can be obtained.7 This gaseous product is cooled in a condenser 22, and the liquefied product oil is The liquid is collected in the liquid receiving tank 23.
そして、精留塔２の塔底より排出された高μ留分は０分
解反応槽１ヘリターンされ再分解することに−より低分
子量適として回収できる。The high μ fraction discharged from the bottom of the rectification column 2 is returned to the zero decomposition reactor 1 and decomposed again, whereby it can be recovered as a low molecular weight fraction.
また、熱分解により発生したＣ４以ドの非凝縮ガスは、
水封槽２４内に導入して槽内の水と接触させることによ
り冷却、洗浄した後、バーナー１０に供給し熱分解用熱
源として利用することができる。In addition, non-condensable gases of C4 and above generated by thermal decomposition are
After being introduced into the water seal tank 24 and brought into contact with the water in the tank to be cooled and washed, it can be supplied to the burner 10 and used as a heat source for pyrolysis.
なお、分解温度の制御は、温度計２０を観察することに
より行い、また分解反応槽１内の液相のレベルは、原料
供給ポンプ１５を連動させたレベル計２１により制御す
ればよい。The decomposition temperature may be controlled by observing the thermometer 20, and the level of the liquid phase in the decomposition reaction tank 1 may be controlled by the level meter 21 linked to the raw material supply pump 15.
本発明は、上述のような方法によりなるものであるので
以下のような効果を有すこととなる。Since the present invention is implemented by the method described above, it has the following effects.
分解反応槽１と加熱炉３とに二分割するとともに処理物
が＠環するように加熱炉３内に内装した流通パイプ５を
分解反応槽ｌに連接しているので′４＆２運転による安
全操業が可能となった。処理物が分解反応槽１と加熱炉
３内を循環することにより加熱炉３の温度が急激にドが
ることがなく常に一定に保たれるからである。It is divided into two parts, the decomposition reaction tank 1 and the heating furnace 3, and the distribution pipe 5 installed inside the heating furnace 3 is connected to the decomposition reaction tank 1 so that the processed material is circulated, so safe operation is possible by '4 & 2 operation. It has become possible. This is because the treated material circulates within the decomposition reaction tank 1 and the heating furnace 3, so that the temperature of the heating furnace 3 does not drop suddenly and is always kept constant.
また処理物は、流通パイプ５内を３ ｍ／ｓａｃ以上の
流速で流通するようにしているのでカーボン等の付着物
質は吹き飛ばされ分解反応槽１内に送り込まれ流通パイ
プ５への付着をなくすことが出来る。Furthermore, since the processed material is made to flow through the distribution pipe 5 at a flow rate of 3 m/sac or more, adhering substances such as carbon are blown away and sent into the decomposition reaction tank 1, thereby eliminating adhesion to the distribution pipe 5. I can do it.
処理物を分解温度とする場合、従来のように加熱炉内に
処理物を投入する方法では長時間要したが１本発明では
流通パイプ５内を通過させるので少量の処理物を順次加
熱することとなり短時間で目的温度とでき、ポリバス方
式に比較して約１７５Ｐ４度に処理時世を短縮できるこ
ととなった。In order to bring the treated material to the decomposition temperature, the conventional method of putting the treated material into a heating furnace takes a long time, but in the present invention, it passes through the distribution pipe 5, so a small amount of the treated material can be heated one after another. Therefore, the target temperature can be reached in a short time, and the processing time can be shortened to about 175P4 degrees compared to the Polybath method.
また、分解温度の制御を１３℃の範囲で行うと安定した
運転が可能となり生成油の回収率が８０ｗｔ％以上を安
定的に確保することができ、非凝縮ガスの発生率も１０
％以下に降下させることが期待できることとなった。In addition, if the decomposition temperature is controlled within the range of 13℃, stable operation is possible, and the recovery rate of produced oil can be stably maintained at 80wt% or more, and the generation rate of non-condensable gas is also 10%.
% or less.
加熱炉３は、ΔＴを大きくシ、また内筒４を設けるとと
もに内筒４と外ｍ４ａ問に螺旋状の流通パイプ５を捲回
しているので燃焼ガスは外筒４ａ内の空間をスピードを
にげて旋回加熱するため熱効率を高められ、また流通パ
イプ５の内部を溶融原料が高速で流通することとなりカ
ーボンの付着をより防止することが出来る。The heating furnace 3 has a large ΔT, is provided with an inner cylinder 4, and has a spiral distribution pipe 5 wound between the inner cylinder 4 and the outer cylinder 4a, so that the combustion gas flows through the space inside the outer cylinder 4a at high speed. Since the molten raw material is rotated and heated, thermal efficiency can be increased, and since the molten raw material flows inside the distribution pipe 5 at high speed, it is possible to further prevent carbon adhesion.
なお、力ｕｄが３の上部には、１ｓ旋状に捲回し水を流
通させる温水パイプ２５ａを内装している余剰ガス燃焼
室２５を突設しておくと、余剰表スを幇
余剰ガス燃焼賞頃２５に導入することにより水封槽２４
が異常圧となる危険を防止することが出来る。In addition, if a surplus gas combustion chamber 25 is provided protruding from the upper part of the force ud of 3, which is equipped with a hot water pipe 25a that is wound in a 1s spiral shape and circulates water, the surplus surface area can be covered and the surplus gas can be burned. Water sealing tank 24 by introducing it to Shokoro 25
The danger of abnormal pressure can be prevented.
図面は１本発明方法を実施する装置の概略図である。
】・・・分解反応槽、２・・・精留塔、３・・・加熱炉
、５・・・流通パイプ、１１・・・原料溶断装置、１４
・・原料貯蔵槽
出願人 株式会社二十−世紀開発The drawing is a schematic diagram of an apparatus for carrying out the method of the invention. ]... Decomposition reaction tank, 2... Rectification column, 3... Heating furnace, 5... Distribution pipe, 11... Raw material fusing device, 14
...Raw material storage tank applicant 20th Century Development Co., Ltd.
Claims (11)
処理物を、加熱炉内に内装した流通パイプに送入して加
熱すると共に、一部をガス化しつつパイプ内を３ｍ／ｓ
ｅｃ以上の流速で流通させ熱分解反応槽に放出してなる
ことを特徴とする廃棄物の熱分解処理方法(1) After the heat melting process, the treated material is continuously supplied to the decomposition reaction tank and is heated by feeding it into the distribution pipe installed in the heating furnace, and at the same time, the inside of the pipe is heated by 3m/3m while gasifying a part of it. s
A method for pyrolysis treatment of waste, characterized by discharging it into a pyrolysis reaction tank by distributing it at a flow rate of ec or higher.
反応槽に供給している請求項１記載の廃棄物の熱分解処
理方法(2) The method for thermal decomposition treatment of waste according to claim 1, wherein the treated material is supplied to the decomposition reaction tank after being subjected to heat treatment after the hot melt treatment.
４６０℃である請求項１又は２記載の廃棄物の熱分解処
理方法(3) The heating temperature of the processed material in the distribution pipe is 410~
The method for thermally decomposing waste according to claim 1 or 2, wherein the temperature is 460°C.
している請求項１、２又は３記載の廃棄物の熱分解処理
方法(4) The method for thermal decomposition treatment of waste according to claim 1, 2 or 3, wherein the heating temperature of the thermally melted material is controlled within a range of ±3°C.
分解残渣を槽外に排出するようにしている請求項１、２
、３又は４記載の廃棄物の熱分解処理方法(5) Claims 1 and 2, wherein the decomposition residue is continuously discharged from the bottom of the decomposition reaction tank in a liquid mixed state to the outside of the tank.
, 3 or 4, the method for thermal decomposition of waste
熱溶融処理工程で溶融された溶融処理物を貯蔵する貯蔵
工程で貯蔵された溶融処理物を熱分解反応槽内に連続的
に供給した処理物を、放出口、送入口となる端部を分解
反応槽の側面上下に連接すると共に加熱炉内に内装した
流通パイプ内を３ｍ／ｓｅｃ以上の流速で流通する熱分
解工程と、該熱分解工程で加熱された生成物を前記熱分
解反応槽内に放出して精製処理する工程とからなる廃棄
物の熱分解処理方法(6) The process of putting the waste into a melting tank and thermally melting it, and the storage process of storing the molten product melted in the heat melting process, the stored molten product is continuously placed in the pyrolysis reaction tank. A pyrolysis process in which the treated material is passed through a flow rate of 3 m/sec or more through a distribution pipe that connects the ends that serve as the discharge port and inlet to the upper and lower sides of the decomposition reaction tank and is installed inside the heating furnace. and a step of discharging the heated product in the pyrolysis step into the pyrolysis reaction tank for purification treatment.
パイプに送入している請求項６記載の廃棄物の熱分解処
理方法(7) The method for pyrolysis treatment of waste according to claim 6, wherein the treated material is fed into a distribution pipe after being subjected to heat treatment after the heat melting treatment.
４６０℃である請求項６又は７記載の廃棄物の熱分解処
理方法(8) The heating temperature of the processed material in the distribution pipe is 410~
The method for thermally decomposing waste according to claim 6 or 7, wherein the temperature is 460°C.
ている請求項６、７又は８記載の廃棄物の熱分解処理方
法(9) The method for thermal decomposition treatment of waste according to claim 6, 7 or 8, wherein the heating temperature of the thermally melted material is controlled within a range of ±3°C.
に分解残渣を槽外に排出するようにしている請求項６、
７、８又は９記載の廃棄物の熱分解処理方法(10) Claim 6, wherein the decomposition residue is continuously discharged from the bottom of the decomposition reaction tank in a liquid mixed state to the outside of the tank.
The method for thermal decomposition of waste according to 7, 8 or 9
いる請求項６、７、８、９又は１０記載の廃棄物の熱分
解処理方法(11) The method for thermal decomposition treatment of waste according to claim 6, 7, 8, 9 or 10, wherein the temperature at the top of the rectification column is 270 to 350°C.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP3168289A JPH02212591A (en) | 1989-02-10 | 1989-02-10 | Method for thermal decomposition of waste material |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP3168289A JPH02212591A (en) | 1989-02-10 | 1989-02-10 | Method for thermal decomposition of waste material |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPH02212591A true JPH02212591A (en) | 1990-08-23 |
Family
ID=12337867
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP3168289A Pending JPH02212591A (en) | 1989-02-10 | 1989-02-10 | Method for thermal decomposition of waste material |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH02212591A (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH02212592A (en) * | 1989-02-10 | 1990-08-23 | Nijiyuuitsuseiki Kaihatsu:Kk | Device for thermal decomposition of waste material |
| JPH03143991A (en) * | 1989-06-15 | 1991-06-19 | Nijiyuuitsuseiki Kaihatsu:Kk | Thermal decomposition apparatus for fluid waste |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS4962575A (en) * | 1972-10-19 | 1974-06-18 | ||
| JPS4966776A (en) * | 1972-10-30 | 1974-06-28 | ||
| JPS5141001A (en) * | 1974-10-04 | 1976-04-06 | Kyoshige Hayashi | Horiorefuinkeijushikokeibutsukaraekitainenryoseizosuru hoho |
| JPH02212592A (en) * | 1989-02-10 | 1990-08-23 | Nijiyuuitsuseiki Kaihatsu:Kk | Device for thermal decomposition of waste material |
-
1989
- 1989-02-10 JP JP3168289A patent/JPH02212591A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS4962575A (en) * | 1972-10-19 | 1974-06-18 | ||
| JPS4966776A (en) * | 1972-10-30 | 1974-06-28 | ||
| JPS5141001A (en) * | 1974-10-04 | 1976-04-06 | Kyoshige Hayashi | Horiorefuinkeijushikokeibutsukaraekitainenryoseizosuru hoho |
| JPH02212592A (en) * | 1989-02-10 | 1990-08-23 | Nijiyuuitsuseiki Kaihatsu:Kk | Device for thermal decomposition of waste material |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH02212592A (en) * | 1989-02-10 | 1990-08-23 | Nijiyuuitsuseiki Kaihatsu:Kk | Device for thermal decomposition of waste material |
| JPH03143991A (en) * | 1989-06-15 | 1991-06-19 | Nijiyuuitsuseiki Kaihatsu:Kk | Thermal decomposition apparatus for fluid waste |
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