JPS63235395A - Method of conducting optimum treatment of sewage sludge to convert it into oleaginous matter - Google Patents
Method of conducting optimum treatment of sewage sludge to convert it into oleaginous matterInfo
- Publication number
- JPS63235395A JPS63235395A JP6963587A JP6963587A JPS63235395A JP S63235395 A JPS63235395 A JP S63235395A JP 6963587 A JP6963587 A JP 6963587A JP 6963587 A JP6963587 A JP 6963587A JP S63235395 A JPS63235395 A JP S63235395A
- Authority
- JP
- Japan
- Prior art keywords
- reaction
- sewage sludge
- pressure
- sludge
- temp
- 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
- 239000010801 sewage sludge Substances 0.000 title claims abstract description 32
- 238000000034 method Methods 0.000 title claims description 24
- 238000006243 chemical reaction Methods 0.000 claims abstract description 44
- 239000000126 substance Substances 0.000 claims description 13
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical class O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 11
- 239000010802 sludge Substances 0.000 abstract description 19
- 239000002002 slurry Substances 0.000 abstract description 5
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 abstract description 4
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 abstract description 3
- 229910001873 dinitrogen Inorganic materials 0.000 abstract description 3
- 239000007789 gas Substances 0.000 abstract description 3
- 239000001569 carbon dioxide Substances 0.000 abstract description 2
- 229910002092 carbon dioxide Inorganic materials 0.000 abstract description 2
- 239000000446 fuel Substances 0.000 abstract description 2
- 230000035484 reaction time Effects 0.000 abstract description 2
- 239000000463 material Substances 0.000 abstract 5
- 229920006395 saturated elastomer Polymers 0.000 abstract 1
- 239000003054 catalyst Substances 0.000 description 13
- 239000008346 aqueous phase Substances 0.000 description 8
- 238000000926 separation method Methods 0.000 description 8
- 239000005416 organic matter Substances 0.000 description 7
- 239000000047 product Substances 0.000 description 6
- 239000007788 liquid Substances 0.000 description 5
- 239000012071 phase Substances 0.000 description 5
- 238000001816 cooling Methods 0.000 description 4
- 239000010865 sewage Substances 0.000 description 4
- YMWUJEATGCHHMB-UHFFFAOYSA-N Dichloromethane Chemical compound ClCCl YMWUJEATGCHHMB-UHFFFAOYSA-N 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 238000012545 processing Methods 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 description 2
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 2
- 230000029087 digestion Effects 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 238000005191 phase separation Methods 0.000 description 2
- 229920000642 polymer Polymers 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 238000012360 testing method Methods 0.000 description 2
- 239000000654 additive Substances 0.000 description 1
- 230000000996 additive effect Effects 0.000 description 1
- 238000005273 aeration Methods 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 229910052783 alkali metal Inorganic materials 0.000 description 1
- 150000001339 alkali metal compounds Chemical class 0.000 description 1
- 150000001340 alkali metals Chemical class 0.000 description 1
- 229910052786 argon Inorganic materials 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 238000005119 centrifugation Methods 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 239000002440 industrial waste Substances 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 238000011085 pressure filtration Methods 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 238000004062 sedimentation Methods 0.000 description 1
- 229910000029 sodium carbonate Inorganic materials 0.000 description 1
- 238000000638 solvent extraction Methods 0.000 description 1
Landscapes
- Treatment Of Sludge (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
Description
【発明の詳細な説明】
〔技術分野〕
本発明は、下水汚泥の油化処理方法に関するものである
。DETAILED DESCRIPTION OF THE INVENTION [Technical Field] The present invention relates to a method for treating sewage sludge into oil.
下水処理場から排出される汚泥（下水汚泥）は、全国で
年間約５０００万イ（含水率９８％）という莫大な量で
あり、年々増加の傾向にある。従来、このような下水汚
泥の処理に関しては、その８０％前後が脱水後、埋立処
分されているが、しかし、この場合には埋立地確保の問
題があり、都市化の発展により、その埋立地確保は年々
困難になってきている。また、下水汚泥は焼却処理する
ことも可能であり、この方法は、その処廟生成物が被処
理原料である下水汚泥の量に比して著しく減容化された
焼却灰であり、被処理原料の減容化という点からは非常
に有効な方法である。しかしながら、この方法の場合、
下水汚泥中の水分の蒸発に多大の熱エネルギーを要する
ために、ランニングコストが高く、経済的でないという
問題を有している。このような現状に対し、本発明者ら
は、特願昭６０−２７９６７９号において、下水汚泥の
液化処理方法を提案している。この方法は、下水汚泥中
の有機物をアルカリ性条件下、高められた温度において
、該温度の飽和水蒸気圧以上の加圧下で加熱反応処理し
た後、得られた反応処理生成物を冷却処理するというも
のである、しかしながら、この方法は、汚泥に対して、
アルカリ性条件の形成のため、あらかじめ、外部から炭
酸ナトリウム等のアルカリ金属化合物を添加する方法の
ものであるため、ランニングコストの増大、更には、設
備投資の増大を導き、実用上、大きな問題である。The amount of sludge (sewage sludge) discharged from sewage treatment plants is a huge amount, approximately 50 million units (water content: 98%), annually nationwide, and is increasing year by year. Conventionally, around 80% of such sewage sludge is dehydrated and then disposed of in a landfill.However, in this case, there is a problem in securing a landfill, and with the development of urbanization, the landfill is becoming more and more Securing it is becoming more difficult every year. In addition, sewage sludge can also be incinerated, and in this method, the product is incinerated ash whose volume is significantly reduced compared to the amount of sewage sludge that is the raw material to be treated. This is a very effective method from the point of view of reducing the volume of raw materials. However, with this method,
Since a large amount of thermal energy is required to evaporate water in the sewage sludge, the running cost is high and it is not economical. In response to this current situation, the present inventors have proposed a method for liquefying sewage sludge in Japanese Patent Application No. 60-279679. In this method, organic matter in sewage sludge is subjected to a heat reaction treatment under alkaline conditions at an elevated temperature under pressure higher than the saturated water vapor pressure at that temperature, and then the resulting reaction treatment product is subjected to a cooling treatment. However, for sludge, this method
In order to create alkaline conditions, an alkali metal compound such as sodium carbonate is added externally in advance, which leads to increased running costs and further increases in equipment investment, which is a major problem in practice. .
本発明は、前記下水汚泥処理に兄られる問題を解決する
ことを目的とする。The purpose of the present invention is to solve the problems encountered in sewage sludge treatment.
本発明によれば、下水汚泥を油化処理する方法において
、あらかじめ反応を促進させるアルカリ物質を添加する
ことなく、反応温度を１５０〜３５０℃とし、該反応温
度の飽和水蒸気圧以上の加圧下で処理することを特徴と
する下水汚泥の最適油化処理方法が提供される。According to the present invention, in a method for treating sewage sludge into oil, the reaction temperature is set at 150 to 350°C without adding an alkaline substance to promote the reaction in advance, and the reaction temperature is set at a pressure higher than the saturated water vapor pressure at the reaction temperature. An optimal method for treating sewage sludge into oil is provided.
本発明において被処理原料として用いる下水汚泥として
は、通常の下水処理場から排出される各種の汚泥があり
、このようなものには、例えば、最初沈殿池汚泥や、余
剰汚泥及びそれらの混合汚泥等が包含される。下水の処
理方式には、特別な限定はないが、滞留時間（酸化時間
）の長い長時間エアレーション法等より、通常採用され
ている標準活性汚泥法等の方が望ましい。また、下水汚
泥は、消化処理後のものでもよいが、好ましくは消化処
理を受けていない生汚泥の使用が有利である。The sewage sludge used as the raw material to be treated in the present invention includes various types of sludge discharged from ordinary sewage treatment plants, such as primary sedimentation tank sludge, surplus sludge, and mixed sludge thereof. etc. are included. There are no particular limitations on the sewage treatment method, but the commonly used standard activated sludge method is preferable to the long-term aeration method, which requires a long residence time (oxidation time). The sewage sludge may be one that has been subjected to digestion treatment, but it is advantageous to use raw sludge that has not undergone digestion treatment.
本発明で用いる下水汚泥の有機物比は、通常４０〜９０
％、好ましくは６０％以上である。The organic matter ratio of the sewage sludge used in the present invention is usually 40 to 90.
%, preferably 60% or more.
本発明の方法を実施するには、単に、高温高圧に保持す
ればよい、下水汚泥の場合、汚泥中にもともと含まれて
いるアルカリ金属等の無機物が、油化反応を促進する触
媒として働くためである。In order to carry out the method of the present invention, it is sufficient to simply maintain the sewage sludge at high temperature and pressure. In the case of sewage sludge, inorganic substances such as alkali metals originally contained in the sludge act as catalysts to promote the oil conversion reaction. It is.
反応温度は１５０−３５０℃で十分であり、反応圧力は
、その反応温度における飽和水蒸気圧以上１例えば、２
５０℃の場合、５０）ｃｇ／ａＪ、３００℃の場合、９
０ｋｇ／ａｔ以上であればよい。この時１反応温度での
保持時間（反応時間）は、ｉｓｏ〜２５０℃の場合、６
０分以上、２５０℃以上の場合、６０分以内で良いが、
水相に移行する有機物量を減らすためには、なるべく高
い温度で長時間反応させることが望ましい。但し、反応
温度を高くすることや、長い時間反応を行わせるという
ことは、イニシャルコストの増大をまねくので、反応温
度は３００℃以下、保持時間は６０分以下が望ましい。A reaction temperature of 150-350°C is sufficient, and a reaction pressure of 1, for example, 2 or more than the saturated water vapor pressure at that reaction temperature.
At 50℃, 50) cg/aJ, at 300℃, 9
It is sufficient if it is 0 kg/at or more. At this time, the holding time (reaction time) at one reaction temperature is 6
0 minutes or more, and if the temperature is 250℃ or more, it may be within 60 minutes, but
In order to reduce the amount of organic matter transferred to the aqueous phase, it is desirable to carry out the reaction at as high a temperature as possible for a long time. However, since raising the reaction temperature or carrying out the reaction for a long time leads to an increase in initial cost, it is desirable that the reaction temperature is 300° C. or less and the holding time is 60 minutes or less.
本発明において、圧力は、下水汚泥からの水蒸気により
自己発生圧を利用することができるが。In the present invention, the pressure can be self-generated by water vapor from sewage sludge.
必要に応じ、例えば、窒素ガス、炭酸ガス、アルゴンガ
ス等を用いて加圧することもできる。If necessary, pressurization can be performed using, for example, nitrogen gas, carbon dioxide gas, argon gas, or the like.
本発明においては、前記のようにして得られた反応処理
生成物を冷却処理するが、そこで得られた冷却処理生成
物は、相分離性の良好なもので、上部の水性相と下部の
スラリー相とに容易に分離される。この生成物の相分離
性の良いこと及び水性相の透明度の高いことは、本発明
の大きな特徴の１つである。この冷却処理生成物の分離
処理には、通常の固液分離手段が適用されるが、一般に
は、スラリー相と一水性相との間の密度差を利用した分
離手段、例えば、前記静置による重力分離の他、遠心分
離等を採用することができる。In the present invention, the reaction product obtained as described above is subjected to a cooling treatment, and the resulting cooling treatment product has good phase separation, with an upper aqueous phase and a lower slurry. It is easily separated into phases. The good phase separation property of this product and the high transparency of the aqueous phase are one of the major features of the present invention. Normal solid-liquid separation means are applied to the separation treatment of this cooling treatment product, but in general, separation means that utilize the density difference between the slurry phase and the monoaqueous phase, such as the above-mentioned standing method, are used. In addition to gravity separation, centrifugal separation or the like can be employed.
本発明において、生成された油状物質は、下水汚泥中に
初めから含まれていた無機物等と共にスラリー相を形成
、する、このスラリー相から液状の油状物質を分離面取
するには、通常の固液分離手段が用いられるが、油状物
質の回収率を高めるためには、スクリュウプレスや加圧
濾過等の加圧を伴った固液分離処理や、遠心分離等の加
重を伴った固液分離処理に付すのがよい、この場合、必
要に応じ、温度３０−１００℃程度の加熱を併用するこ
とができる。In the present invention, the produced oily substance forms a slurry phase together with the inorganic substances originally contained in the sewage sludge. Liquid separation means are used, but in order to increase the recovery rate of oily substances, solid-liquid separation processing that involves pressurization such as screw press or pressure filtration, or solid-liquid separation processing that involves weight such as centrifugation is recommended. In this case, heating at a temperature of about 30 to 100° C. can be used in combination, if necessary.
本発明によれば、従来産業廃棄物として取り扱われてい
た下水汚泥を、液体燃料（発熱量的８０００ｋｃａｌ／
＃）として有用な油状物質に変換させることができる。According to the present invention, sewage sludge, which was conventionally treated as industrial waste, can be converted into liquid fuel (calorific value of 8000 kcal/
It can be converted into an oily substance useful as #).
しかも、この場合、油状物質の収率は、乾燥有機物基準
でほぼ４０〜５０％もの高い値に達する。Moreover, in this case, the yield of oily substances reaches a high value of approximately 40-50% based on dry organic matter.
その上、本発明では、水相に移行する有機物の割合が少
なく、かつ透明性が高いので、下水処理場の水処理工程
に与える影響が少ないと言える。さらに、本発明におい
ては、汚泥中にもともと含まれていた無機物自身が触媒
作用を示すので、特別に触媒を必要とせず、経済的にも
非常に有利である。それ故１本発明の下水汚泥処理方法
は、技術的、経済的に非常に有利な方法であるというこ
とができる。Furthermore, in the present invention, the proportion of organic matter transferred to the aqueous phase is small and the transparency is high, so it can be said that there is little influence on the water treatment process of a sewage treatment plant. Furthermore, in the present invention, since the inorganic substances originally contained in the sludge themselves exhibit a catalytic action, no special catalyst is required, which is very economically advantageous. Therefore, it can be said that the sewage sludge treatment method of the present invention is a technically and economically advantageous method.
次に、本発明を実施例によりさらに詳細に説明する。 Next, the present invention will be explained in more detail with reference to Examples.
実施例１
下水汚泥として、標準活性汚泥法の処理場から排出され
た混合生汚泥の脱水ケーキを選び、試験に用いた。この
汚泥は高分子凝集剤を添加された後、ベルトプレスにて
脱水されたものである。その代表的な性状は表−１の通
りである。Example 1 As sewage sludge, a dehydrated cake of mixed raw sludge discharged from a treatment plant using the standard activated sludge method was selected and used in the test. This sludge was dehydrated using a belt press after adding a polymer flocculant. Its typical properties are shown in Table-1.
表−１
上記脱水汚泥１００ｇにアルカリ触媒として所定量のＮ
ａ２Ｇｏ３を添加した後、内容量３００ｍ１のオートク
レーブに充填し、３００℃まで加熱した。この際。Table-1 A predetermined amount of N as an alkaline catalyst is added to 100 g of the above dehydrated sludge.
After adding a2Go3, it was filled into an autoclave with an internal capacity of 300 ml and heated to 300°C. On this occasion.
圧力はあらかじめ窒素ガスで１２０ｋｇ／（ｉまで加圧
しておき、温度上昇に伴う圧力増加を圧力５整弁を用い
て、１２０ｋｇ／ｄに制御した。反応は温度が３００℃
に到達後ただちに１００℃以下まで冷却し、終了させた
。加熱前に添加したアルカリ触媒の量はＯｇ（無添加、
０重量部）、 ０．２７ ｇ （０，０１重量部）、０
．５４ ｇ （０，０２重量部）、０．８１ ｇ （０
，０３重量部）、１．０８ ｇ （０，０４重量部）、
１．３５ ｇ （０，０５重量部）、２．７ｇ（０，１
重ｊ＋ｆ、部）、４．０５ ｇ （０，１５重量部）及
び５．４ｇ（０，２重量部）と変えて、計９通りの実験
を行った。The pressure was previously increased to 120 kg/d with nitrogen gas, and the pressure increase due to temperature rise was controlled to 120 kg/d using a pressure 5 regulating valve.The reaction was carried out at a temperature of 300°C.
Immediately after reaching 100°C, the temperature was cooled to 100°C or lower to complete the process. The amount of alkaline catalyst added before heating was Og (no additive,
0 parts by weight), 0.27 g (0.01 parts by weight), 0
．． 54 g (0.02 parts by weight), 0.81 g (0
,03 parts by weight), 1.08 g (0.04 parts by weight),
1.35 g (0.05 parts by weight), 2.7 g (0.1
A total of 9 experiments were conducted by changing the weight (weight j+f, parts), 4.05 g (0.15 parts by weight), and 5.4 g (0.2 parts by weight).
反応終了後、各々の生成物を塩化メチレンを用いた溶媒
抽出法で分離し、油状物質、残渣固形物及び水性相の三
相とした。実験結果を第１図に示す。After the reaction was completed, each product was separated by solvent extraction using methylene chloride to form three phases: an oily substance, a residual solid, and an aqueous phase. The experimental results are shown in Figure 1.
油状物質の生成は触媒を加えなくとも円滑に進行したが
、添加率が０．０５重量部を越えると、油化反応は反対
に阻害された。更に、水性相に移行した有機物の量は触
媒の添加率が増えるにつれて。The production of oil proceeded smoothly even without the addition of a catalyst, but when the addition rate exceeded 0.05 parts by weight, the oil-forming reaction was inhibited. Furthermore, the amount of organic matter transferred to the aqueous phase increased as the catalyst addition rate increased.
増大しており、前述の油状物質の収率からみても。Even in terms of the yield of the oily substance mentioned above.
水性相の性状から言っても触媒を使用しない時が最適で
ある。Considering the properties of the aqueous phase, it is best when no catalyst is used.
実施例２
下水汚泥として、実施例１とは異なる複数の処理場から
混合生汚泥の脱水ケーキを採取し、試験に用いた。これ
らの汚泥はすべて高分子凝集剤を添加された後、ベルト
プレスにて脱水されたものである。これらの汚泥に対し
、実施例１と同様の油化処理を行ない表−２に示す結果
を得た。但し。Example 2 As sewage sludge, dehydrated cakes of mixed raw sludge were collected from a plurality of treatment plants different from those in Example 1 and used in the test. All of these sludges were dehydrated using a belt press after adding a polymer flocculant. These sludges were subjected to the same oil conversion treatment as in Example 1, and the results shown in Table 2 were obtained. however.
触媒の添加率は乾燥固形物に対し、０および０．０５重
量部とした。The addition rate of the catalyst was 0 and 0.05 parts by weight based on the dry solid matter.
表−２油化結果（オイル収率）
上表に示したごとく、すべての汚泥において、アルカリ
触媒陶加えなくとも、油化反応は円滑に進行した。Table 2 Results of oil conversion (oil yield) As shown in the table above, the oil conversion reaction proceeded smoothly in all sludges even without the addition of an alkali catalyst.
実施例３
実施例２の汚泥口を触媒を使用しないで、オートクレー
ブに充填し、所定の温度まで加熱した。この時、圧力は
、反応温度における飽和水蒸気圧＋３０ｋｇ／ｃｄに制
御した０反応温度は２００，２２５，２５０゜２７５、
３００及び３２５℃の６通りとして、その他は実施例１
と同様とした。実験結果を第２図に示す。Example 3 The sludge port of Example 2 was filled into an autoclave without using a catalyst and heated to a predetermined temperature. At this time, the pressure was controlled to the saturated water vapor pressure at the reaction temperature + 30 kg/cd, and the reaction temperature was 200, 225, 250° 275,
Six different temperatures at 300 and 325°C, and the others were as in Example 1.
The same is true. The experimental results are shown in Figure 2.
その結果、油状物質の生成は反応温度を高く操作すると
共に上昇したが、３００℃以上で飽和傾向を示した。こ
の時、水性相に移行した有機物量は３００℃以上におい
ても徐々に減少したが、顕著な差は見られなかった。従
って、反応温度での保持時間をもたない油化処理では、
３００℃が反応温度として最適である。As a result, the production of oily substances increased as the reaction temperature was raised, but showed a tendency to saturation at temperatures above 300°C. At this time, the amount of organic matter transferred to the aqueous phase gradually decreased even at temperatures above 300°C, but no significant difference was observed. Therefore, in oil processing that does not have a holding time at the reaction temperature,
300°C is the optimum reaction temperature.
実施例４
実施例３と同じ脱水汚泥を触媒を使用しないでオートク
レーブに充填し、２００．２２５．２５０，２７５及び
３００℃まで加熱、その温度で６０分間保持した。Example 4 The same dehydrated sludge as in Example 3 was charged into an autoclave without using a catalyst, heated to 200, 225, 250, 275 and 300°C, and held at that temperature for 60 minutes.
この時、圧力は反応温度における飽和水蒸気圧＋３０ｋ
ｇ／ｄに制御した。その後の操作は実施例１と同様とし
た。実験結果を第３図に示す。At this time, the pressure is the saturated water vapor pressure at the reaction temperature + 30k
g/d. The subsequent operations were the same as in Example 1. The experimental results are shown in Figure 3.
その結果、油状物質の生成は保持時間を持たない時と比
べ著しく改善され、２５０℃以上において、オイル収率
は４０％にも達し、飽和傾向を示した。As a result, the production of oily substances was significantly improved compared to the case without holding time, and at temperatures above 250°C, the oil yield reached as much as 40%, showing a tendency to saturation.
実施例５
実施例３と同じ脱水汚泥を触媒を使用しないでオートク
レーブに充填し、 １５０．１７５．２００．２２５℃
まで加熱し、その温度で１２０分間保持した。この時、
圧力は反応温度における飽和水蒸気圧＋３０ｋｇ１ｄに
制御した。その後の操作は実施例１と同様とした。実験
結果を第４図に示す。Example 5 The same dehydrated sludge as in Example 3 was charged into an autoclave without using a catalyst, and the temperature was 150.175.200.225°C.
and held at that temperature for 120 minutes. At this time,
The pressure was controlled to saturated water vapor pressure at the reaction temperature +30 kg1d. The subsequent operations were the same as in Example 1. The experimental results are shown in Figure 4.
その結果、１５０℃の場合、はとんど油化反応は進行し
なかったが、１７５℃以上では、オイル収率は３０％以
上を示した。この事より、低い反応温度においてもある
程度の保持時間をもつことにより、油化反応が円滑に進
行することが明らかとなった。As a result, at 150°C, the oil-forming reaction hardly proceeded, but at 175°C or higher, the oil yield was 30% or more. From this, it has become clear that the oil-forming reaction proceeds smoothly even at low reaction temperatures by allowing a certain amount of holding time.
第１図〜第４図は、それぞれ、実施例１、実施例３、実
施例４及び実施例５の実験結果を示すグラフである。
第１図
触媒添加率
反応温度（℃）
反応温度（℃）1 to 4 are graphs showing the experimental results of Example 1, Example 3, Example 4, and Example 5, respectively. Figure 1 Catalyst addition rate Reaction temperature (℃) Reaction temperature (℃)
Claims (2)
め反応を促進させるアルカリ物質を添加することなく、
反応温度を１５０〜３５０℃とし、該反応温度の飽和水
蒸気圧以上の加圧下で処理することを特徴とする下水汚
泥の最適油化処理方法。(1) In the method of treating sewage sludge to oil, without adding an alkaline substance to accelerate the reaction in advance,
An optimal method for treating sewage sludge into oil, characterized in that the reaction temperature is 150 to 350°C, and the treatment is carried out under pressure higher than the saturated water vapor pressure at the reaction temperature.
度を１５０〜２５０℃とした時、該反応温度における保
持時間を６０分以上とする特許請求の範囲第１項記載の
下水汚泥の最適油化処理方法。(2) In the method of treating sewage sludge to oil, when the reaction temperature is 150 to 250°C, the optimum sewage sludge according to claim 1, wherein the holding time at the reaction temperature is 60 minutes or more. Oil treatment method.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP6963587A JPS63235395A (en) | 1987-03-24 | 1987-03-24 | Method of conducting optimum treatment of sewage sludge to convert it into oleaginous matter |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP6963587A JPS63235395A (en) | 1987-03-24 | 1987-03-24 | Method of conducting optimum treatment of sewage sludge to convert it into oleaginous matter |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPS63235395A true JPS63235395A (en) | 1988-09-30 |
Family
ID=13408517
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP6963587A Pending JPS63235395A (en) | 1987-03-24 | 1987-03-24 | Method of conducting optimum treatment of sewage sludge to convert it into oleaginous matter |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS63235395A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH08168800A (en) * | 1994-08-29 | 1996-07-02 | Agency Of Ind Science & Technol | Method of efficiently incinerating organic sludge |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS61238399A (en) * | 1985-04-15 | 1986-10-23 | Japan Organo Co Ltd | Apparatus for converting sludge to oil |
| JPS61255991A (en) * | 1985-05-08 | 1986-11-13 | シエル・インタ−ナシヨネイル・リサ−チ・マ−チヤツピイ・ベ−・ウイ | Roduction of hydrocarbon-containing liquid from biomass |
-
1987
- 1987-03-24 JP JP6963587A patent/JPS63235395A/en active Pending
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS61238399A (en) * | 1985-04-15 | 1986-10-23 | Japan Organo Co Ltd | Apparatus for converting sludge to oil |
| JPS61255991A (en) * | 1985-05-08 | 1986-11-13 | シエル・インタ−ナシヨネイル・リサ−チ・マ−チヤツピイ・ベ−・ウイ | Roduction of hydrocarbon-containing liquid from biomass |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH08168800A (en) * | 1994-08-29 | 1996-07-02 | Agency Of Ind Science & Technol | Method of efficiently incinerating organic sludge |
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