JPS61238399A - Apparatus for converting sludge to oil - Google Patents

Abstract

PURPOSE:To efficiently recover a combustible liquid, by adding an org. solvent to a slurry mixture consisting of the solid substance obtained by thermochemically treating org. sludge under a high temp. and high pressure condition, a combustible liquid and water. CONSTITUTION:Org. sludge 1 is dehydrated by a dehydrator 2 and the dehydrated sludge is supplied to a preheater 5. After the sludge is preheated by the preheater 5, the heated sludge is supplied to a reactor 6 to be thermochemically reacted under a high temp. and high pressure condition. By this method, biomass is thermochemically modified to form various combustible liquids. Subsequently, the solid substance passed through the reactor 6, said combustible liquids and water are mixed to prepare a slurry mixture 9 which is, in turn, supplied to a cooler 7 in a pressurized state to be indirectly cooled by a heating medium 8. Next, the cooled slurry mixture 9 is supplied to an atmosphere state and the oily substance 12 comprising the combustible liquids is selectively recovered.

Description

[Detailed Description of the Invention] <Industrial Application Field> The present invention thermochemically reacts organic sludge such as surplus sludge generated from microbial treatment equipment such as activated sludge equipment under high temperature and high pressure conditions to produce combustible sludge. The present invention relates to a sludge oil converting apparatus that obtains a flammable liquid and uses the flammable liquid as a thermal energy source or electrical energy source for the thermochemical reaction.

<Prior Art> A sludge oil technology has been proposed as one method for treating organic sludge such as surplus sludge generated from various microbial treatment devices.

In other words, it is a technology that thermochemically reacts organic sludge under high temperature and high pressure conditions to obtain fuel oil from biomass.

A device for producing asphalt and fuel oil from sewage sludge has been proposed as this type of technology (EPA Project
Summary EPA-600152-81-24
2Dec, 1981).

This device is based on the flow shown in Figure 5. Organic sludge A is dehydrated to a certain extent in a centrifuge B, the dehydrated sludge C is pressurized by a high-pressure slurry pump D, and first reacted in a reactor F, which will be described later. The high-temperature mixture slurry G immediately after heating is preheated in a preheater E as a heat source, and the preheated dehydrated sludge C is supplied to a reactor F. The reactor F
This method converts biomass into asphalt and fuel oil by reacting it under high temperature and high pressure conditions, and usually converts dehydrated sludge into 250
The reaction is carried out at a temperature of .degree. C. to 350.degree. C. and a pressure higher than the water vapor pressure at the temperature. The slurry G, which is a mixture of solids and fuel oil obtained by such a reaction, is circulated under pressure to the preheater E described above, where heat is exchanged indirectly, and then supplied to the gas-liquid separator H. and release to atmospheric pressure. When the mixture slurry G is released to atmospheric pressure in the gas-liquid separator H, the mixture slurry 〇 boils due to the high temperature, and some water and fuel oil evaporate. Next, the vapor is cooled and liquefied by a cooler I, and the liquid is processed by a centrifuge J, and mechanical gravity separation is performed into waste water and fuel oil. - The mixture slurry G remaining without being evaporated in the dregs separator H is processed by the centrifuge M and separated into waste water N and solid matter 0. Next, the solid matter 0 is supplied to the extractor P, and the distiller S and evaporator V, which will be described later,
Add organic solvent Q to the recovered spiky shells, and now the solids are 0.
Extract the asphalt components in the
is supplied to the distiller S to recover the organic solvent Q and obtain asphalt L-T. On the other hand, the residue U from the extractor P is supplied to the evaporator V to recover the organic solvent adhering to the residue U and obtain a reaction residue W.

The flow of the proposed method for obtaining asphalt and fuel oil is roughly as described above, and the reaction residue W is used as a heat source in the reactor F.

Note that the obtained asphalt is used for its original purpose as asphalt.

<Problems to be solved by the invention> In the conventionally proposed sludge oil converting apparatus shown in FIG. 5, the flammable liquid contained in the reactant slurry G obtained from the reactor F is relatively low. We believe that there are no so-called oily substances that are easily vaporized by temperature and can be separated by the difference in specific gravity when liquefied.Therefore, we centrifuged the oily substance in the liquid that liquefied in cooler I. The specific gravity is separated in machine J, and the remaining waste water K is removed from the system.

Furthermore, it is believed that the produced asphalt components are attached to the solids in the reactant slurry G that did not evaporate in the gas-liquid separator H, so the asphalt components are collected together with the solids in the centrifuge M, and the same In this way, wastewater N is removed from the system. However, according to experiments conducted by the present inventors, there is a flammable liquid in the reactant slurry G that does not vaporize at low temperatures, is easily soluble in water, unlike asphalt components, and can be used satisfactorily as a fuel. We found that there are flammable liquids that exist in large amounts and that even if they are vaporized, it is difficult to separate them by specific gravity difference after liquefaction. In an example in which the sludge was dehydrated to some extent, 5% by weight of sodium carbonate based on dry solids was added as an alkaline component, and the reaction was carried out in a sealed autoclave at 320°C for 1 hour. After the reaction, the reactants were cooled to room temperature. When this is collected in a separatory funnel and left to stand for a day and night, a small amount of oily substance will float to the surface, but methylene chloride is added as an organic solvent to the remaining reactant to extract the remaining flammable liquid. Then, the above-mentioned floating oily substance accounts for about 17% of the total flammable liquid.
Experiments have shown that approximately 83% of the other combustible liquid does not float to the surface and remains in the reaction solution. It has been certified. Therefore, in the conventional flow shown in Figure 5, such flammable liquids that do not easily vaporize and are easily soluble in water cannot be separated by centrifuge M, and migrate into wastewater N. In addition, even if it is vaporized, flammable liquids that are difficult to separate by specific gravity after liquefaction cannot be separated by centrifuge J, and are transferred to wastewater and discharged from the system. It will be done. Furthermore, although it is an oily substance that is easily separated from water by specific gravity, if it exists in an emulsified state in water, it is impossible to separate it using a centrifuge J. Oily substances will also migrate into the wastewater and be discharged.

The main purpose of the conventionally proposed flow is to produce asphalt from organic sludge, and obtaining fuel oil is considered to be a secondary purpose. The fact that there is a large amount of flammable liquid that can be recovered as waste is completely overlooked.

In addition, in the conventional flow shown in Figure 5, only the reaction residue W is used as the heat source for the reactor F, but even if it is sufficiently dehydrated until it self-combusts, it is completely insufficient in terms of heat balance to be used as fuel. Therefore, it is not profitable from the viewpoint of treating organic sludge. Furthermore, even if the produced asphalt L-T and fuel oil are recovered as a heat source, the heat balance is still insufficient. In other words, in order to economically treat organic sludge using sludge oil technology, it is essential to recover the flammable liquid present in the aforementioned wastewater and N and actively use it as a heat source. be.

In addition, in the conventional flow, the mixture slurry 〇 is transferred to the gas-liquid separator H.
This consumes extra latent heat of vaporization, and when the steam generated from the gas-liquid separator H is cooled and liquefied in the cooler I, the heat released by liquefaction is consumed. Conventional flows have various drawbacks with respect to heat recovery. Furthermore, as a heat source for preheater E,
Since the slurry-like reactant produced in the reactor F is used as it is, there is also a drawback that the structure of the preheater E is restricted and it is difficult to manufacture.

The present invention has been made in view of the above points, and its purpose is to remove flammable substances, especially flammable liquids, from the reactants obtained by reacting organic sludge under high temperature and high pressure conditions. The object of the present invention is to provide a sludge oil processing apparatus that processes organic sludge most economically by recovering organic sludge, reusing it as an energy source, and efficiently using the generated thermal energy.

Means for Solving the Problems> The present invention provides a dewatering device for dewatering organic sludge in advance, a press-in device for press-fitting the dehydrated sludge in series into a preheater, a reactor, and a cooler, which will be described later. A preheater that indirectly preheats dehydrated sludge using a heat medium heated in a subsequent cooler, and a preheater that indirectly heats dehydrated sludge preheated in the preheater with a heat medium to a temperature of 250°C or higher and steam at that temperature. A reactor in which the reaction is carried out at a pressure higher than the above pressure, a reactant reacted in the reactor is indirectly cooled by a heat medium, and the heat medium heated by cooling the reactant is used as a heat source for the preheater. A cooler, an air release device that releases the reactant cooled by the cooler to atmospheric pressure, a recovery device that recovers the flammable liquid in the reactant released from the air release device, and a combustion device that collects the flammable liquid from the recovery device. The present invention relates to a sludge oil converting apparatus characterized by comprising a heating furnace that indirectly heats a heat medium by heating the heat medium and uses the heating heat medium as a heat source for the reactor.

<Effect> The present invention will be explained in detail below with reference to the drawings.

FIG. 1 is an explanatory diagram showing the flow of the present invention. First, organic sludge 1 is dehydrated in advance using a dewatering device such as a centrifuge or a belt press type dehydrator, and the dehydrated sludge 3 is preheated by a press-in device 4. Supply to vessel 5. Note that if the organic sludge contains too much water, a large amount of heat will be consumed in the thermochemical reaction described below, so it is desirable to dehydrate the organic sludge to a water content of 80% or less in the dehydrator 2.

Furthermore, in the thermochemical reaction described below, the reaction proceeds more efficiently when an alkaline component is present in the organic sludge, so sodium carbonate, potassium carbonate,
It is preferable to add an alkaline component such as sodium formate, potassium formate, potassium hydroxide, sodium hydroxide, and lime. Of course, a high-pressure slurry pump can be used as the above-mentioned press-in device 4, but since dehydrated sludge must be supplied under considerably high pressure, it is preferable to use a press-in device that combines a cylinder and a piston as described below.

That is, as shown in FIG. 2, a cylinder 33 containing a piston 32 is installed, and water level gauges 34A, 34 are installed.
A water tank 35 equipped with a cylinder B is installed, and the lower part of the water tank 35 and the upper part of the cylinder 33 are connected, for example, to a reciprocating pump 3.
A supply pipe 38 and a discharge pipe 39 for dehydrated sludge are connected to the lower part of the cylinder 33 through a pipe 37 .

The operation of the press-fitting device 4 shown in FIG.
．． 4I is opened and the supply pump 42 is driven to supply dehydrated sludge 3.
flows from the lower part of the cylinder 33 through the supply pipe 38. With this inflow, the piston 32 rises, and the water above the piston 32 flows into the water tank 35 via the pipe 37 and the valve 41. Since the water level in the water tank 35 rises according to the volume of the supplied dehydrated sludge 3, the water level in the water tank 35 increases according to the volume of the supplied dehydrated sludge 3.
When point A is reached, the supply of dehydrated sludge 3 is stopped.

Next, the valves 41 and 40 are closed and the reciprocating pump 36 is driven to compress the water in the water tank 35 and pressurize the inside of the cylinder 33 via the piston 32. Next, after the pressure inside the cylinder 33 is sufficiently increased, the valve 43 is opened and the dehydrated sludge 3 inside the cylinder 33 is forced into the cylinder 33 via water and the piston 32. The piston 32 descends with the press-fitting, and the dehydrated sludge 3 in the cylinder is supplied to the preheater 5, which will be described later. Note that when the water level in the water tank reaches the water level gauge 34B, the press-fitting is stopped and the above-described operation is repeated.

If the above-described device is used as the press-in device 4, it has the advantage of being able to supply dehydrated sludge at high pressure, being inexpensive to manufacture, easy to operate, and easy to automatically control.

The preheater 5 indirectly preheats the dehydrated sludge 3 using a heat medium 8 that has been given heat by a cooler 7, which will be described later.
The dehydrated sludge 3 is passed through the inside of a stirring type heat exchanger and heat is applied from the outside by the heat medium 8, or the dehydrated sludge 3 is passed through the inside of the tubes using a so-called shell-and-tube heat exchanger. , one that applies heat from the outside of the tube using a heat medium 8, etc. can be used.

The dehydrated sludge 3 preheated by the preheater 5 is then supplied to the reactor 6, where the organic sludge 3 is thermochemically reacted under high temperature and high pressure conditions. The reactor 6 uses the same stirring type heat exchanger or multi-tube type heat exchanger as the preheater 5 described above, and dehydrated sludge 3 is indirectly heated by the heat medium 8 heated by the first heat exchanger 24 described later. It heats the temperature, usually 250°
The reaction is carried out at a temperature of C to 350''C and a pressure corresponding to or higher than the water vapor pressure at the temperature.

Note that the dehydrated sludge 3 is still in the form of a slurry with poor fluidity in the preheater 5 and before and during the reaction in the reactor 6, so it is preferable to use a stirring type heat exchanger rather than a shell-and-tube type heat exchanger. It is desirable to use it. Also, in the drawing, the preheater 5 and the reactor 6 are installed separately, but the preheater 5
The reactor 6 and the reactor 6 may be integrated, and the first half of the inflow side of the dehydrated sludge can be used as the preheating section, and the second half of the outflow side can be used as the reaction section.

When organic sludge is treated at high temperature and pressure in this way, the biomass is thermochemically transformed, producing various flammable liquids and at the same time changing into liquids with extremely good fluidity. Next, the slurry 9 of the mixture of solids, combustible liquid, and water that has passed through the reactor 6 is supplied in a pressurized state to the cooler 7 and cooled indirectly by the heat medium 8 . Note that by using the heat medium 8 that has been given heat by cooling as a heat source for the preheater 5, the heat given by the reactor 6 can be effectively recovered.

Note that as the cooler 7, a thin film falling type heat exchanger, a full tube heat exchanger, a stirring type heat exchanger, etc. can be used, but since the mixture slurry 9 has extremely good fluidity, it has the highest thermal efficiency. It is preferable to use a falling film heat exchanger.

The mixture slurry 9 cooled in this manner is then supplied to an atmosphere opening device 10, and brought from a pressurized state to a normal pressure state.

The atmosphere opening device 10 used in the present invention may include, for example, a receiving tank that receives the mixture slurry 9 from the cooler 7 and a red down valve provided at the bottom of the receiving tank.
It is preferable to use a device like the one shown in the figure.

That is, for example, ball valves 44A, 4 are installed in the upper and lower parts.
Multiple receiving tanks 45A, 4 with 4B, 44C, 144D
5B, an inert gas cylinder 46 such as nitrogen, argon, helium, etc., and a gas storage tank 47, and as shown in FIG. This is what I did.

The operation of the atmospheric release device 10 shown in FIG.
Then, the valve 49 is opened to allow inert gas to flow from the inert gas cylinder 46 into the receiving tank 45A, and the pressure of the receiving tank 45 is made approximately equal to the pressure of the cooler 7. Note that this operation is necessary only at the beginning, and is not necessary thereafter as will be described later. Next, the ball valve 44A, the valve 48, and the valve 52 are opened to receive the mixture slurry 9 from the cooler 7 into the receiving tank 45A.

The inert gas discharged from the receiving tank 45A due to the reception is transferred to the receiving tank 45 via the valve 48, the back pressure valve 56, and the valve 52.
Flows into B. Furthermore, since the inert gas passes through the back pressure valve 56 at this time, by making the operating pressure of the back pressure valve 56 equal to the pressure of the cooler 7, the inert gas can gradually flow into the receiving tank 45B. can.

After receiving a specified amount of the mixture slurry 9 into the receiving tank 45A through such an operation, the Pall valve 44A1 valve 52 is closed while the valve 48 remains open, and the valve 51 is opened. In this way, the pressure in the receiving tank 45A and the receiving tank 45B is reduced by the valve 48,
Since the inert gas communicates with each other via the valve 51, it becomes equal.

Next, the ball valve 44C is opened to begin receiving the mixture slurry 9 into the receiving tank 45B. -Force receiving tank 4
On the 5A side, the valve 48 is closed, the valve 50 is opened, and the receiving tank 45 is opened.
A small amount of pressurized inert gas remaining in the upper part of A flows into the storage tank 47, and excess inert gas is discharged to the outside via the back pressure valve 57. Note that when the dehydrated sludge is reacted in the reactor 6, various gases are also generated, so it is desirable to perform a deodorizing treatment as necessary at the time of the above-mentioned discharge. The operating pressure of the back pressure valve 57 is set to, for example, 5 kg/crA.
If G, then 5 kg/cniG of pressurized inert gas will remain in the upper part of the receiving tank 45A due to this step. Next, by opening the ball valve 44B, the mixture slurry 9 can be fed to the outside, that is, to the flotation tank 11, which will be described later, by the pressure of the residual gas of 5 kg/cm G.

When the discharge of the mixture slurry 9 from the receiving tank 45A is completed,
The valve 50 is closed, the valve 49 is opened, and the inert gas discharged from the receiving tank 45B as the mixed slurry 9 is received in the receiving tank 45B is transferred to the valve 51, the back pressure valve 56, and the valve 49.
It flows into the receiving tank 45A through the. Moreover, since the inert gas also passes through the back pressure valve 56 at this time, it can be made to gradually flow into the receiving tank 45A as described above.

Next, in the same manner as described above, the pressures in both tanks are equalized by opening the valves 48 and 51, and then the valve 53 is opened to open the receiving tank 4.
A small amount of pressurized inert gas remaining in the upper part of 5B flows into the storage tank 47, and the excess gas is released to the outside via the back pressure valve 57. Then, the ball valve 44D is opened to release the mixture slurry 9. It is fed to a flotation separation tank 11 which will be described later. As described above, the atmosphere opening device 10 shown in FIG. 3 sequentially receives the mixture slurry 9 into a plurality of receiving tanks, and collects the inert gas discharged as a result of the receiving tank in other receiving tanks.

If the above-described atmospheric release device 10 is used, the mixture slurry 9 in the cooler 7 under high pressure can be reduced to atmospheric pressure with a relatively simple structure, and the amount of inert gas consumed can be reduced. There are also very few.

The mixture slurry 9 fed by the atmosphere release device 10 is then fed to the flotation tank 11, and the flammable liquid in the mixture slurry 9 is separated from the oily substance, which is a part of the flammable liquid that floats on water. 12 is selectively recovered. Note that if some flammable liquid floating on water is attached to solid matter in the liquid, it is recommended to stir it before supplying it to the flotation tank 11.

As the flotation separation tank 11, it is possible to use a tank in which the mixture slurry 9 is simply retained for a certain period of time and the floating oily substance t12 is scraped off with a skimmer, or a so-called oil separator with a simple structure. Flotation separation tank 1
The mixture slurry 9 from which the oily substance 12 has been removed in step 1 is then sent to the extraction tank 13, and the solvent 14 recovered by a solvent recovery device 20 (to be described later) is added thereto and sufficiently stirred to form the mixture slurry 9.
Extract the flammable liquid inside. The extraction tank 13 may be of any type as long as it can bring the mixture slurry 9 and the solvent 14 into necessary and sufficient contact, and the mixture of the mixture slurry 9 and the solvent 14 is stirred in the tank using a stirrer. It doesn't matter if it's something simple.

The solvent 14 used is preferably one that can extract as much of the flammable liquid as possible in the mixture slurry 9 and easily recover it by evaporation, and usually benzene, toluene, acetone, methylene chloride, etc. are used.

The mixture 15 obtained batchwise or continuously from the extraction tank 13 is then fed to a three-phase separator 16 where it is separated into waste water 17, solids 18 and extract 19. The three-phase separator 16 is a so-called centrifugal separator, which separates waste water 17, solid matter 18, and extract 19 having different specific gravity by centrifugal action, and a known one can be used.

The extract 19 obtained by the three-phase separator 16 is then sent to a solvent recovery device 20, where it is indirectly heated with a heat medium 8 heated by a second heat exchanger 25, which will be described later, to recover the solvent 1.
4 is evaporated, and the evaporation residue, flammable liquid 21, is recovered. In addition, in the drawing, the solvent 1 recovered from the solvent recovery device 20 is
4 is directly supplied to the extraction tank 13, but in reality, the gaseous solvent obtained from the solvent recovery device 20 is cooled and liquefied in a cooler (not shown) and recovered as the liquid solvent 14.

22 is a heating furnace that uses as fuel the flammable liquid 21 recovered from the solvent recovery device 2o or the oily substance 12 recovered from the flotation tank 1, and hot air obtained by burning these fuels. 23 is supplied to the first heat exchanger 24 to heat the heat medium 8 used in the reactor 6, and then the hot air 23 is subsequently supplied to the second heat exchanger 25 to be used in the solvent recovery device 20. The heat medium 8 is heated. Note that 26 is exhaust gas, 27 is combustion air, and 2
8 indicates combustion ash.

In addition, in the flow shown in FIG. 1, the mixture slurry 9 obtained from the atmosphere opening device 10 is supplied to the flotation separation tank 11, and the oily substance 12 is selectively recovered in advance.
This step may be omitted and the mixture slurry 9 obtained from the atmosphere opening device 10 may be directly supplied to the extraction tank 13 to extract all of the flammable liquid present. Note that if the step of collecting the oily substance f12 is omitted in this way, the amount of the solvent 14 used will increase slightly, and the flammable liquid 21 obtained from the solvent recovery device 20 will also contain the above-mentioned oily substance 12.

FIG. 4 is an explanatory diagram showing the flow of another embodiment of the present invention, and since the steps up to the step of recovering the oily substance 12 by the flotation separation tank 11 are completely the same as in FIG. 1, the explanation will be omitted. The mixture slurry 9 from which the oily substance 12 has been removed by the flotation tank 11 is then sent to a solid-liquid separator 29 such as a centrifuge, where the solid matter 18 in the mixture slurry 9 is removed.

The mixed solution 30 from which solids have been removed is then supplied to an extraction device 31, and the solvent 14 recovered by the solvent recovery device 20 is added thereto to extract the flammable liquid in the mixed solution 30. The solid material 18 is used as the extraction device 31 in the flow shown in FIG.
has been removed in advance, so solvent 14 and mixed solution 3
It is more efficient to use a solvent that makes countercurrent contact with the mixed solution 30. When using a solvent with a higher specific gravity than the mixed solution 30, as shown in the figure, the solvent 14 is flowed down from above, and the mixed solution 30 is flowed downward. Flow the mixed solution in an upward flow from
When using a solvent with a lower specific gravity, it is preferable to reverse the direction of the top and bring them into countercurrent contact.

The extract 19 thus obtained is transferred to a solvent recovery device 20.
The rest of the flow is the same as that in FIG. 1, so the explanation will be omitted. Note that in the flow shown in FIG. 4, some flammable liquid adheres to the solid material 18 obtained in the solid-liquid separator 29, so it is preferable that the solid material 18 is also used as fuel for the heating furnace 22. Further, as in FIG. 1, the flotation separation tank 11 can be omitted.

As explained above (in the present invention, a slurry of a mixture of solids, a flammable liquid, and water obtained by thermochemically reacting organic sludge under high temperature and high pressure conditions, or solids from the slurry of the mixture) An organic solvent is added to the mixed solution from which the Even if a large amount of flammable liquid is contained, it can be recovered as much as possible, and by using the recovered flammable liquid as a source of thermal energy or electrical energy, it is possible to economically convert organic sludge. can be processed.

Further, in the present invention, a cooler 7 is installed after the reactor 6, and the mixture slurry 9 obtained from the reactor 6 is indirectly cooled by the heating medium 8 without boiling, and heat is given by the cooling. Since the heat medium 8 is used as a heat source for the preheater 5 used at the front stage of the reactor 6, the thermal energy cost can be surely reduced by the amount of latent heat of vaporization consumed when boiling the mixture slurry as in the conventional flow. Furthermore, since the heat medium heated by the cooler 7 is used as the heat source of the preheater, the cost of thermal energy can be reduced in this respect as well. Further, unlike in the conventional flow, the high temperature mixture slurry 9 obtained from the reactor 6 is not directly used in the preheater 5, so there is no particular restriction on the structure of the preheater.

[Brief explanation of the drawing]

1 to 4 are drawings showing embodiments of the present invention, and FIG. 1 is an explanatory diagram showing the flow of the present invention,
FIG. 2 is an explanatory diagram showing the flow of the press-fitting device used in the present invention, FIG. 3 is an explanatory diagram showing the flow of the atmosphere release device used in the present invention, and FIG. 4 is an explanatory diagram showing the flow of the press-fitting device used in the present invention. It is an explanatory diagram showing a flow. Moreover, FIG. 5 shows a flow in a conventional method for obtaining asphalt and fuel oil from sewage sludge. 1...Organic sludge 2...Dewatering device 3...
・Dehydrated sludge 4...Press injection device 5...Preheater 6...Reactor 7...Cooler
8...Heating medium 9...Mixture slurry 1
0...Atmospheric release device] l...Flotation separation tank 1
2... Oily substance 13... Extraction tank 14.
...Solvent 15...Mixture Process 6...Three-phase separator 17...Wastewater 18...Solid matter 19...Extract 20...Solvent recovery device 21...Heatable liquid 22.・Heating furnace 23・
...Hot air 24...First heat exchanger 25.
... Second heat exchanger 26 ... Exhaust gas 27 ... Air for combustion 28 ... Combustion ash 29 ... Solid-liquid separator 30 ... Mixed solution 31 ... Extraction device
32... Piston 33... Cylinder
34... Water level gauge 35... Water tank 36
... Reciprocating pump 37 ... Piping 38
... Supply pipe 39 ... Discharge pipe 40.41
... Valve 42 ... Supply pump 43 ... Valve 4
4... Pole valve 45... Receiving tank 46...
・Inert gas cylinder 47...Gas storage tank 48.
49.50.51.52.53.54.55...Valve
56.57... Back pressure valve procedure amendment (
Spontaneous) July 8, 1985 Michibe Uga, Commissioner of the Patent Office1, Indication of the case: Patent Application No. 78393, filed in 19852, Name of the invention: Sludge oil converting device 3, Person making the amendment Relationship to the case: Patent Applicant Address: 5-5-16 Hongo, Bunkyo-ku, Tokyo Name:
(440) Organo Co., Ltd. Representative Nagai
Kunio Ii 4, Agent 113 Address 5-5-16 Hongo, Bunkyo-ku, Tokyo <77゛” 7) Inside Organo Co., Ltd. Name (6376) Patent Attorney Akishi Takahashi-6-Device;
812-5151 5. Column for detailed description of the invention in the specification subject to amendment 14 Te P1 side ≧)
. 6. Please correct the following items in the detailed statement of amendment. 1゜Insert the following sentence between the 3rd and 4th lines on page 22. "In this embodiment, the flotation tank 11 and the extraction tank 1 described above are
3. The three-phase separator 16, the solvent recovery device 20, etc. correspond to devices for recovering flammable liquid from the reactants, but the combination is not limited to these, and in short, the combustible liquid is recovered from the reactants. Any material can be used as long as it can effectively recover. ” 2. Insert the following sentence between lines 10 and 11 on page 23. [In this embodiment, the flotation tank 11, solid-liquid separator 29, extraction device 31, solvent recovery device 20, etc. correspond to devices for recovering the flammable liquid in the reactant, but the combination is particularly limited to these. In short, any material may be used as long as it can effectively recover the flammable liquid from the reactants. "that's all

Claims (1)

[Scope of Claims] 1. A dewatering device for pre-dehydrating organic sludge, a press-in device for press-fitting the dehydrated sludge in series into a preheater, a reactor, and a cooler described later, and dehydrated sludge pressurized from the press-in device A preheater that indirectly preheats the dehydrated sludge using a heat medium heated in a downstream cooler, and indirectly heats the dehydrated sludge preheated in the preheater with a heat medium to a temperature of 250°C or higher and a water vapor pressure higher than the water vapor pressure at that temperature. A reactor for reacting under pressure; a cooler for indirectly cooling the reactant reacted in the reactor with a heat medium, and using the heat medium heated by cooling the reactant as a heat source for the preheater; An atmosphere release device that releases the reactants cooled by a cooler to atmospheric pressure; a recovery device that recovers the flammable liquid in the reactants released from the atmosphere release device; and a recovery device that burns the flammable liquid recovered from the recovery device to generate heat. A sludge oil converting apparatus comprising a heating furnace that indirectly heats a medium and uses the heating heat medium as a heat source for the reactor. 2. The press-in device connects the upper part of the cylinder containing the piston and the lower part of the water tank containing the water level gauge with piping via a pump, and connects the supply pipe and discharge pipe for dehydrated sludge to the lower part of the cylinder. The sludge oil conversion apparatus according to claim 1, which is connected to the sludge oil converting apparatus. 3. The atmosphere release device connects multiple receiving tanks having valves at the upper and lower parts with the upper part of each receiving tank via a back pressure valve, and the reactants are discharged when receiving reactants into one receiving tank. 3. The sludge converting apparatus according to claim 1, wherein the gas is recovered into the other receiving tank via the back pressure valve.