JP2006038439A - Waste fluid incineration method - Google Patents

Abstract

<P>PROBLEM TO BE SOLVED: To provide an incineration method allowing incineration of a waste liquid, using a retention heat of a solid waste, without lowering incineration performance for the solid waste, without remaining unburnt carbon, CO or the like in combustion exhaust gas, and without generating a toxic product, when treating the waste liquid of a low calorific value in an incineration process for the solid waste. <P>SOLUTION: In this incineration disposal method for the waste liquid, an evaporation decomposition means for the waste liquid is constituted of a first treatment process capable of feeding the waste liquid into a rotary kiln maintained at 800°C or more under reductive atmosphere of a furnace inside to be atomization-incinerated, and a second treatment process capable of feeding the waste liquid into a kiln furnace end fixing hood 41 and a secondary combustion furnace 49 for burning inflammable exhaust gas from the first process to be atomization-incinerated, in the gasification rotary kiln 36 for combustion-gasifying partially the solid waste. The feed of the waste liquid is carried out by single or combination of a waste liquid injection port of a waste feed hopper 31, a waste liquid spray nozzle 52 of a furnace front fixing hood 37, a waste liquid spray nozzle 52 of the furnace end fixing hood 41, and a waste liquid spray nozzle 53 of a secondary combustion furnace wall. <P>COPYRIGHT: (C)2006,JPO&NCIPI

Description

  The present invention generates the amount of heat necessary for high-temperature pyrolysis of the waste liquid to be treated by using the retained heat of solid waste discharged as general waste or industrial waste and burning the solid waste This is a waste liquid incineration method in which the waste liquid is thermally decomposed at a high temperature using thermal energy.

  Waste liquids generated by industrial activities are further classified into waste acids and waste alkalis. These are neutralized and then generally treated with wastewater such as coagulation sedimentation, activated sludge treatment, wet oxidation treatment, and dehydration treatment. Has been done. However, if the wastewater treatment is inappropriate due to the properties of the waste liquid, incineration is performed as a second option. The incineration targets include, for example, waste liquids with high concentrations of dissolved salts, highly hazardous waste liquids containing organic halogen compounds, or inorganic acids such as hydrogen chloride and hydrogen fluoride generated by high-temperature thermal decomposition of waste liquids. For example. In the case of such waste liquid incineration treatment, since the amount of heat of the waste liquid at the time of incineration is so low that it does not have self-combustibility, in general, liquid fuel or gas fuel is used as auxiliary fuel. The amount of heat necessary for the combustion is secured.

  Further, in the incineration treatment of waste liquid, the type of incinerator to be applied differs depending on the content of ash contained in the waste liquid and its properties. In cases where the ash content is high or the melting point of the ash is low, the ash that floats in the gas after the water in the effluent evaporates is fused to the furnace wall of the incinerator to prevent long-term operation. A type incinerator is adopted. On the contrary, when the problem of ash is not a problem, a horizontal incinerator is adopted. However, since both use a large amount of liquid fuel or gas fuel, considerable service costs are required. Accordingly, if incineration of waste liquid can be performed simultaneously in a solid waste incinerator, auxiliary fuel can be saved. Therefore, in many incinerators of solid waste, spray incineration of waste liquid is simultaneously performed (for example, non-patent literature). 1, Patent Document 1).

  However, even in this case, injecting waste liquid, which hardly generates heat, into the combustion space where the solid waste is originally combusted, will adversely affect the combustion operation. That is, there are problems such as remaining unburned matter in the combustion exhaust gas and low melting point ash fused to the furnace wall of the incinerator to reduce the operation rate. From the above, in the conventional method, it is natural that the amount of waste liquid blown is limited, in other words, the utilization rate of the ratio of effectively utilizing the amount of heat held by solid waste remains at a low level. It can be said that it was.

'96 Selection of Waste Processing and Recycling Technology, Print Issue Date October 20, 1996, p. 72, 91, 106, issued by Environmental Newspaper Co., Ltd. JP 11-182825 A

The following functions are required for a waste liquid incineration treatment facility that uses the heat retained by solid waste to thermally decompose low-temperature waste liquid at high temperature.
1. A large amount of waste liquid can be incinerated with the heat of solid waste alone.
2. To maintain the waste liquid incineration process stably by controlling the additional combustion of auxiliary fuel against fluctuations in the calorific value of solid waste.
3. Do not leave unburned matter containing harmful substances such as unburned carbon and unburned CO gas, which are intermediate products of combustion decomposition, in the exhaust gas at the outlet of the secondary combustion furnace.
4). The ash contained in the waste liquid must be fused and grown on the wall of the secondary combustion furnace and the wall of the rotary kiln bottom hood so that continuous operation is not hindered due to ash discharge failures.

  Conventionally, in many solid waste incinerators within the allowable range of the above constraints, waste liquid spray incineration is performed at the same time. The amount of sprayed incineration of waste liquid in conventional solid waste incinerators due to adverse effects on the combustion operation and low melting point ash fused to the incinerator furnace wall and lowering the operation rate, etc. However, there was a limit, and the heat retained in solid waste could not be fully utilized.

The reason why the conventional incinerator cannot sufficiently meet the above problems will be described below.
As a conventional incinerator, FIG. 1 shows a fluidized bed incinerator and FIG. 2 shows a rotary kiln incinerator.

In the fluidized bed incinerator of FIG. 1, the normal waste liquid is blown into the fluidized bed 2 or the space of the free board 7. Inside the fluidized bed 2, the solid waste is incinerated by the combustion air blown from the dispersion plate 8 in the thermal decomposition temperature region, and at the same time, rapidly decomposed by the combustion heat.
The characteristics of fluidized bed incinerators are that these operations are performed at high speed in a small space, but the waste liquid blown into the fluidized bed becomes an impediment to the combustion operation and thermal decomposition operation, and the amount blown into is small. Stay. In addition, when blowing into the freeboard 7, the blowing space is a sufficiently wide space, but the operating temperature is 1200 ° C or less at the maximum, and the outlet temperature needs to be stably controlled to about 850 ° C. If a large amount of waste liquid is sprayed into the freeboard on the premise, there is a risk that the lump portion of the sprayed low temperature gas may leave unburned components such as CO, char, hydrocarbons, etc. in the outlet exhaust gas due to incomplete combustion. Get higher.

  In the rotary kiln incinerator of FIG. 2, the waste liquid is blown into the rotary kiln combustion space 14 from the waste liquid spray nozzle 16 provided in the normal hood 10 fixed hood 10 or into the secondary combustion furnace combustion space 15 by the waste liquid spray nozzle 17. Infused. The combustion spaces 14 and 15 are oxidation combustion spaces in which combustion air exists excessively. When blowing waste liquid with a low calorific value, the amount of combustion air input is lowered to ensure the amount of heat required for incineration of the waste liquid. The outlet temperature of the secondary combustion furnace is maintained at 850 ° C. or higher. However, if the temperature in the rotary kiln is increased in order to incinerate the waste liquid in the rotary kiln, the ash contained in the solid waste melts and softens on the walls of the rotary kiln and grows by fusion. For this reason, an operation rate falls extremely. In addition, in the low temperature operation of the rotary kiln incinerator, the amount of waste liquid incinerated remains small. When the waste liquid is blown into the secondary combustion furnace, the combustion of the secondary combustion furnace is likely to be hindered for the same reason as when the waste liquid is blown into the freeboard of the fluidized bed incinerator described above.

  A method of generating high-temperature combustion exhaust gas and increasing the incineration amount of the waste liquid with the auxiliary combustion burner 20 provided in the rotary kiln bottom hood fixing hood 12 in FIG. 2 is also conceivable. The fact that the retained heat of waste cannot be used effectively is the same as described above. As described above, the prior art has many restrictions on incineration of waste liquid and is not suitable for large-scale treatment of waste liquid.

In order to achieve the function required for the above-mentioned waste liquid incineration treatment facility, the present invention of claim 1
(1) In a gasification rotary kiln that performs partial combustion gasification of solid waste, in order to evaporate and decompose waste liquid in a rotary kiln maintained at 800 ° C. or higher at a rotary kiln outlet in a reducing atmosphere inside the furnace, Waste liquid is supplied into the rotary kiln furnace by the waste liquid inlet provided on the waste charging hopper wall surface as the first waste liquid supply means or by the waste liquid spray nozzle provided in the fixed hood in front of the furnace as the second waste liquid supply means. A first treatment step capable of evaporative decomposition,
(2) In order to evaporate and decompose the waste liquid in the combustion space of the rotary kiln bottom fixing hood and the combustion space of the secondary combustion furnace for burning the combustible exhaust gas generated from the first treatment step, as a third supply means of waste liquid A second process capable of spraying and incinerating waste liquid into the rotary kiln bottom hood and / or secondary combustion furnace by a waste liquid spray nozzle provided on the rotary kiln bottom hood and / or secondary combustion furnace wall. The process constitutes the evaporative decomposition means of the waste liquid,
The waste liquid incineration method is characterized in that the waste liquid is supplied by any one or a combination of the first supply means, the second supply means, and the third supply means.

  According to the waste liquid incineration processing method of the present invention having the above configuration, first, in the first processing step, a small amount of combustion air necessary for burning a part of the solid waste is introduced into the rotary kiln, or the solid When it is difficult to maintain a reducing atmosphere by partial combustion gasification, such as when the heat generation amount of waste is extremely low, reducing combustion of the auxiliary burner with the combustion air ratio set to 0.5 to 0.9 Thus, the internal atmosphere of the rotary kiln is maintained in a high temperature reduced state. Under this condition, a waste liquid injection port provided on the wall surface of the waste hopper as the first supply means of the waste liquid in the rotary kiln or a waste liquid spray nozzle provided in the fixed hood before the furnace as the second supply means of the waste liquid The outlet exhaust gas temperature after the waste liquid is supplied and the incineration process in the rotary kiln is finished is maintained at 800 ° C. or higher.

  The waste liquid in the first treatment step is blown into the rotary kiln and incinerated, then the water evaporates, the combustible component is gasified, a part of the ash is sublimated gas, and a part is floated as free dust in the exhaust gas, The other part is mixed with the thermal decomposition residue generated in the rotary kiln and discharged from the rotary kiln. The product gas derived from the waste liquid and the product gas derived from the solid waste are introduced into the second treatment step as a combustible mixed gas.

In the second treatment step, waste liquid is further sprayed by the spray nozzles 52 and / or 53 in the combustion space 51 of the rotary kiln bottom hood 41 and / or the combustion space 48 of the secondary combustion furnace 49 shown in FIG. Do processing. In the secondary combustion furnace 49, it is necessary to introduce combustion air for combustion of the rotary kiln product gas, or to merge with the incineration exhaust gas of the stoker incinerator including surplus air installed for incineration of the rotary kiln pyrolysis residue In response to this, the auxiliary combustion burners 47 and 50 are burned to form a high-temperature combustion atmosphere of 800 ° C. or higher. In the high-temperature combustion atmosphere, while the temperature raising operation is performed in the combustion process of the rotary kiln product gas, the temperature lowering operation by blowing the waste liquid with a low calorific value proceeds at the same time, so that the combustion of the generated gas is not hindered. Incinerate by spraying waste liquid under operating conditions.
Since the product gas generated in the first treatment step has a high temperature of 800 ° C. or higher and sufficient flammability, the second treatment step is sufficiently effective up to a waste liquid treatment amount that does not inhibit combustion. The amount of processing can be increased to some extent.

  Regarding the distribution of the waste liquid incineration amount in the first processing step and the second processing step, since the first processing step sprays the waste liquid in the space in the rotary cylinder of the rotary kiln, the molten salt adhering to the furnace wall is a pyrolysis residue. In other words, it is desirable to treat the entire amount in the first treatment step according to more distribution or the amount of waste liquid generated. Furthermore, in the waste liquid spraying in the first treatment step, an effect of reforming the floating carbon present in the gasified gas to carbon monoxide and hydrogen by a water gas reaction can be expected.

  The waste liquid supplied into the rotary kiln has a high viscosity, is in a slurry state with a large amount of SS, or other factors, so that the waste liquid is supplied from the first supply means to the third supply means. When it is inappropriate to supply, it can be mixed with solid waste in the receiving pit in advance and mixed as adhering water, and the waste liquid can be supplied to the rotary kiln as the solid waste is charged.

  The waste liquid incineration treatment method according to claim 2 is a rotary kiln bottom hood fixing hood for peeling and removing a furnace wall-attached clinker to which fly ash derived from solid waste is added, centering on desorbed ash in the waste liquid. The furnace wall is generally covered with a refractory metal liner on the surface of the refractory wall located below the horizontal center line of the rotary kiln, and when the weight of the clinker exceeds the adhesion with the metal liner. A clinker removing and discharging step is provided which is naturally peeled and dropped, and further carried out of the furnace by a stalker furnace installed for incineration of thermal decomposition residue in the rotary kiln.

  The ash content in the waste liquid is generally composed mainly of a low-melting-point substance, and exists in the gas as softened dust or a gas body. Solid fly-derived fly ash is added to this, and dust tends to be fused on the rotary kiln, the furnace bottom fixing hood, and the furnace wall of the secondary combustion furnace, and easily grows in a short period of time. In particular, the connection between the rotary kiln bottom and the stoker furnace has an inclined throttle structure on the wall surface, and the peelability of the wall surface is small.Once attached, natural flaking cannot be expected, the incinerator is stopped, and the clinker is removed by in-furnace work. There is only a way to remove it. For this reason, the sedimentation dust is generally deposited on the surface of the refractory wall located below the horizontal center line of the rotary kiln, and the wall is corrosion-resistant so that it will peel off naturally even when softened and fused by high-temperature gas radiation from the top. Lined with refractory metal to give peelability.

  As described above, most of the dust floating in the gas and the dust deposited and deposited on the wall surface are softened and melted and tend to adhere and grow. If this deposition amount becomes a certain amount, the incinerator must be stopped for the removal operation, and the operating rate of the incinerator is deteriorated. In particular, the angle of the wall surface of the shell part connecting the rotary kiln and the stoker furnace is ideally vertical, but in reality it is almost as vertical as possible, but the outer diameter of the rotary kiln and the grate width of the stoker furnace In general, a case where a considerably narrowed structure is formed toward the lower part is common. Dust accumulates on the wall surface, and fusion growth occurs due to radiant heat from the gas body. The present invention attaches a corrosion-resistant and heat-resistant metal liner to the wall surface, and when a certain amount of deposit is reached, the dust lump is naturally separated from the wall surface by its own weight, and continuous operation is performed without stopping the incinerator. Is possible.

According to a third aspect of the present invention, the rotary kiln has a corrosion-resistant and heat-resistant metal lift pin inserted therein, and the leakage air into the furnace of the rotary kiln rotating sliding portion is suppressed to 200 Nm ³ / h or less per 1 m of seal length. It is characterized by being.

  The rotary kiln used for pyrolysis stirs the charged solid waste to constantly heat and heat the individual solids constituting the solid waste, and always keeps the solid waste inside the solid waste layer. Corrosion-resistant and heat-resistant metal lift pins 40a and 40b are inserted so as to generate a sliding surface, and the lift pins prevent the solid waste from slipping on the inner surface of the rotary kiln, and the solid waste lifted as the rotary kiln rotates. The object is slid and stirred on the inner surface of the layer. For this stirring device, for example, a device disclosed in JP-A-10-267239 is desirably used.

Although a minute gap is formed in the rotary sliding part of the rotary kiln, since the operating internal pressure of the rotary kiln is negative, air leaks from the outside into the furnace. If the leakage amount becomes large, the internal atmosphere of the rotary kiln cannot be maintained in a reducing atmosphere, and therefore, the leakage air of the rotary sliding portion needs to be suppressed to 200 Nm ³ / h or less per 1 m of seal length. .
For example, a device disclosed in Japanese Patent Application Laid-Open No. 2001-21046 is preferably used as the sealing device for the rotary sliding portion.
The amount of air leaking per meter length of a sealing device is generally

Formula 1

Q = α × A × √ (2 × g × (−P _i ) / γ) (1)
Where α: flow coefficient A: gap area per unit length m ² / m
P _i : Pressure inside the rotary kiln furnace kgf / m ² (mmH ₂ O, 9.80665 × Pa)
γ: apparent specific weight of air kgf / m ³ (kg × g / m ³ )
From the above equation (1), if the gap is simply measured, the amount of air leaking can be easily measured.

In the waste liquid incineration treatment method according to claim 4, when it is difficult to maintain the reducing atmosphere by partial combustion gasification of solid waste or by partial combustion gasification, the reducing kiln is fixed to the rotary kiln furnace fixed hood. The required amount of heat is added by reducing and burning the combustion air ratio of the attached auxiliary combustion burner in the range of 0.5 to 0.9, and the exhaust gas temperature at the bottom of the rotary kiln is maintained at least 800 ° C., and In the secondary combustion furnace, the lower heating value of the generated gas is at least 300 kcal / Nm ³ and the hydrogen gas concentration is maintained at 6% or more, and / or the combustion heat of the rotary kiln generated gas and char is used. The exhaust gas temperature after spray incineration of the waste liquid is characterized by being at least 1200 ° C. or higher during theoretical combustion with an air ratio of 1.0.

  In general, the combustion sustainability of a mixed gas of a combustible gas, a support gas, and an inert gas mainly composed of hydrocarbons is such that the exhaust gas temperature is at least 1250 to 1300 when the entire amount of the combustible gas is exhausted. Combustion continues at temperatures above ℃. The present invention indirectly defines the upper limit of the amount of waste liquid incineration by defining the properties of the generated gas and the exhaust gas temperature of the rotary kiln within the range of preconditions that combustion continues, and thereby the combustion process of the rotary kiln generated gas Waste liquid incineration is not an obstacle to sustaining combustion.

  At this time, hydrogen gas has a high risk level (= combustion upper / lower limit difference / combustion lower limit) of 17.7, and has sufficient combustion sustainability even if it is considerably below 1250 ° C. defined above. Therefore, although it is desirable that it exists in the rotary kiln generating gas as high as possible, it is set to 6% or more from the feasibility by operation control, and the waste liquid is spray incinerated in the secondary combustion furnace in the presence of hydrogen gas. The exhaust gas temperature afterwards was defined to be at least 1200 ° C. or higher during theoretical combustion with an air ratio of 1.0.

  Here, the hydrogen gas is generated as a reaction product mainly composed of the following water gas reaction.

Formula 2

C + H ₂ O⇔CO + H ₂ (2)

Formula 3

H ₂ O + CO⇔CO ₂ + H ₂ (3)
The lower calorific value and hydrogen concentration of the generated gas can be easily estimated from the supply amount of carbon, hydrogen and oxygen in the waste, the supply amount of combustion air to the rotary kiln and the partial pressure of water vapor in the rotary kiln. In the case of the equipment configuration of the present invention shown in FIG. 3, it is difficult to specify the location where the generated gas composition is detected, and thus the generated gas property can be generally estimated from the experience value.
That is, designation of hydrocarbon conversion rate (experience value that varies depending on the waste type, for example, 15%), designation of main component hydrocarbon (generally CH ₄ , C ₂ H ₄ , the production ratio thereof is, for example, 2 parts by volume: 1 volume part), and designation of the water gas reaction ratio by the above formula (2) of the amount of free carbon calculated in the material balance by the above designation (experience value, for example, 70%), the generated gas composition estimated from the above Assuming that the equilibrium state has been reached by the shift reaction of formula (3), the generated gas composition can be estimated finally.

  In the waste liquid incineration processing method according to claim 5, the rotary kiln has an upper semicircular part of the rotary kiln bottom end face 43 that is retreated from the rotary kiln bottom fixed hood furnace wall surface 42 a, and a lower semicircular part is the furnace Since the furnace bottom fixed hood furnace wall is formed in a stepped shape in the vicinity of the rotary kiln horizontal center line so as to protrude from the wall surface 42b, it is softened at a low temperature that flows down from the wall surface of the upper part of the secondary furnace. The rotary kiln bottom end face 43 is prevented from being contaminated by the accumulation of ash or ash that scatters in the space.

  In the space of the rotary kiln bottom, the rotary kiln generated gas and the stoker furnace combustion exhaust gas merge, combustion is started by residual oxygen in the stoker furnace combustion exhaust gas, and the temperature of the gas body in the combustion process becomes 1000 ° C. to 1300 ° C. . Therefore, most of the dust floating in the gas and the dust adhering and depositing on the wall is softened and melted, and if the rotary kiln furnace bottom forms the same plane as the wall of the furnace bottom fixed hood or protrudes The dust easily adheres to the bottom of the rotary kiln, and eventually the rotary operation of the rotary kiln becomes impossible, and it must be stopped. For this reason, when the rotary kiln bottom end surface is viewed from the top of the secondary combustion furnace space, it is configured to recede from the wall surface of the rotary kiln bottom bottom fixing hood so that even if molten dust flows down from the top, The end face of the furnace bottom of the rotary kiln was not contaminated.

The invention's effect

  The waste liquid incineration method according to claim 1 does not cause unburned carbon or unburned trace gas components to remain in the exhaust gas, and does not cause harmful substances such as dioxins or dioxin-related compounds to remain in the exhaust gas. Can be utilized to the maximum extent for the evaporative decomposition heat of the waste liquid, and fuel that has been used in large amounts can be saved.

  According to the waste liquid incineration processing method of claim 2, when a certain amount of dust accumulates on the wall surface of the furnace shell having a squeezed structure toward the lower portion, the rotary kiln furnace bottom fixed hood furnace wall surface Because the adhesion of the coated corrosion-resistant and heat-resistant metal liner surface is much smaller than that of refractory, the dust mass will easily peel off from the wall by its own weight, and the incinerator should be stopped. And continuous operation is possible.

In the waste liquid incineration processing method according to claim 3, the solid waste is uniformly heated by the corrosion-resistant and heat-resistant metal lift pins 40a and 40b inserted in the rotary kiln, so that the unreacted solid can be processed quickly. The atmosphere in the furnace can be maintained in a reducing atmosphere by applying the sealing devices 38 and 39 that can suppress the leakage air into the furnace of the rotary kiln rotary sliding part to 200 Nm ³ / h or less per 1 m of the seal length.

  Even when a waste liquid with a low calorific value is sprayed and incinerated in a rotary kiln, a secondary combustion furnace, and a rotary kiln bottom fixing hood by the waste liquid incineration processing method according to claim 4, the present invention is sufficient as a gas fuel. It is possible to generate the generated gas that maintains its quality, and it is possible to continue the stable combustion of the generated gas in the furnace bottom fixed hood and the secondary combustion furnace. The incineration amount of waste liquid can be used to incinerate the maximum amount of waste liquid by using the surplus heat of solid waste without using valuable auxiliary fuel, except in cases where the amount of heat held by solid waste is small. Is possible.

  According to the waste liquid incineration processing method according to claim 5, since the rotary kiln bottom is retracted from the wall surface of the furnace bottom fixing hood, it is difficult for the dust to be fused to the rotary kiln bottom, and the molten dust flows down from the top. Even in such a case, since the end face of the furnace bottom is not directly contaminated, the rotary operation of the rotary kiln is continuously stable and the operating rate of the incinerator is improved.

FIG. 1 is an explanatory diagram of a conventional fluidized bed incinerator. Moreover, FIG. 2 is explanatory drawing of the conventional rotary kiln incinerator.
Drawing 3 is an explanatory view about equipment of a rotary kiln, a stoker furnace, and a secondary combustion furnace showing an embodiment of the present invention. FIG. 4 is a structural diagram of a seal structure of a rotary kiln rotating part and a lift pin stirrer. FIG. 5 is a cross-sectional view taken along line AA shown in FIG. FIG. 6 is an attachment structure diagram of a corrosion-resistant and heat-resistant metal liner.

The best mode for carrying out the present invention will be described with reference to FIGS. 3, 4, 5 and 6.
The solid waste is once received by the input hopper 31 and is input into the rotary kiln 36 by the cutting conveyor 32. The charged solid waste is partially combusted by a small amount of combustion air having an air-fuel ratio of about 0.2 to 0.6, and the remaining combustible matter undergoes thermal decomposition to become pyrolysis gas and char. The waste liquid blown from the waste liquid spray nozzle 34b is heated by the combustion heat generated by the partial combustion of the solid waste, and is evaporated and decomposed.

The atmosphere of these mixed gases is maintained at a high temperature and in a reduced state. In order to prevent a large amount of air from leaking into the furnace, a high-performance kiln seal device (pre-furnace seal device 38, furnace bottom 39) capable of maintaining a leak amount of 200 Nm ³ / h or less per meter of seal length. Sealing device).

  The solid waste thrown into the furnace is provided with a plurality of stirrers 40a and 40b in the furnace in order to make sufficient contact with the high-temperature furnace atmosphere gas in a short time. The object is sufficiently agitated by an agitation lift pin driven with the rotation of the rotary kiln. The outlet temperature of this first treatment step is maintained at 800 ° C. or higher.

  The generated gas discharged from the first treatment step is introduced into the furnace bottom fixed hood 41 of the second treatment step, and the combustible gas contained in the generated gas is contained in the exhaust gas rising from the stoker incinerator 45 within the fixed hood. Burns in contact with oxygen. Further, the primary combustion air and the secondary combustion air are blown into the mixed gas rising to the secondary combustion furnace 49 from the lower part of the secondary combustion furnace, and the combustion continues. The secondary combustion furnace outlet temperature is controlled to an arbitrary temperature of 800 ° C. or higher by adjusting the secondary combustion air. The waste liquid is blown into the rotary kiln bottom fixed hood and / or the secondary combustion furnace by the spray nozzles 52 and 53, and is evaporated and decomposed in the combustion process of the rotary kiln generated gas in the blowing space maintained at about 1000 ° C. or more. . All the combustion exhaust gas stays in the combustion space 48 of the secondary combustion furnace for 2 seconds or more of the legal residence time, and is discharged as complete combustion exhaust gas from the outlet of the secondary combustion furnace.

  Most of the ash in the waste liquid blown from the waste liquid spray nozzle 34b into the rotary kiln, the spray nozzle 52 to the rotary kiln bottom fixing hood 41, and the spray nozzle 53 to the secondary combustion furnace 49 floats in the gas. And part of it evaporates into the gas. The ash floating in the gas is softened and melted in a high-temperature atmosphere and fused to the rotary kiln bottom hood and the wall of the secondary combustion furnace. Most of the fused dust flows down due to the radiant heat of the high-temperature gas. However, the furnace bottom end surface 43 of the rotary kiln is retreated relative to the fixed hood wall surface 42a in the upper semicircular portion, so that it flows down. Softening dust does not directly contaminate the rotary kiln bottom end face.

  In addition, the waste liquid spray nozzle 34b, which is the second supply means of the waste liquid, is blown into the rotary kiln, and the rotary kiln bottom fixed hood and the secondary combustion are supplied from the waste liquid spray nozzles 52, 53, which are the third supply means of the waste liquid. According to the blowing into the furnace, the ash content in the waste liquid blown out is dispersed in the space as the liquid waste evaporates, and further adheres to the wall surface, and the softened product of the attached ash is fused and grown together with solid waste-derived soot and dust. The risk of doing it increases. When this tendency becomes prominent, the waste liquid is injected into the solid waste before being charged into the rotary kiln from the waste liquid inlet 34a which is the first supply means of the waste liquid, and the waste liquid is put into the rotary kiln in a form in which the solid waste is wetted. Supply.

  The dust generated in the first processing step and the second processing step is discharged from the bottom of the fixed hood to the outside of the furnace through the clinker removal / discharge step. That is, from the spaces 51 and 48 where the waste liquid is sprayed / evaporated and combusted, the ash that melted and flowed down the wall and the dust that settled on the lower wall from the gas become clinker and accumulates on the lower wall. Due to the furnace shell structure covered with a corrosion-resistant and heat-resistant metal liner 54, after a certain amount of deposition, it naturally peels off due to its own weight, then falls onto the grate 44 of the stoker incinerator and is discharged outside the furnace by driving the grate. The

  In this case, as is apparent from FIG. 5, it is common from the dimensional relationship between the rotary kiln and the stoker furnace that the wall surface of the furnace shell connecting the rotary kiln and the stoker furnace has an inclined structure. It is desirable to design this inclined structure as close to vertical as possible in order to promote the accumulation growth of dust. However, in the arrangement of FIGS. 3 and 5, it is necessary to make the planar dimensions of the grate 44 of the stoker furnace larger than necessary, which increases the range in which the pyrolysis residue cannot cover the grate, High-temperature gas radiation from the top will also damage the grate life. From this point of view, if the flow direction of the stalker furnace shown in FIGS. 3 and 5 is rotated 90 degrees, the wall surface of the furnace shell connecting the fixed hood and the stalker furnace is planned vertically while maintaining the grate area appropriately. It becomes easy.

Next, the best mode for carrying out the present invention will be described with reference to FIG. 4 as a means for maintaining the inside of the rotary kiln in a reducing atmosphere and thermally decomposing the solid waste in the rotary kiln with high efficiency.
For the rotary kiln pre-sealing seal device 38, a pressing plate A65 is fixed to the roller chain 61, and a flexible joint sealing material is attached by a pressing bolt attached through the pressing plate A so as to seal the sliding portion. 64 is pressed through the pressing plate B63. Lubricating oil is supplied to the seal portion sliding seat 64 as necessary. One end of the joint seal material is fixed to the rotary kiln front fixed hood, and the other end is fixed to the roller chain pressing plate. The roller chain is wound around the rotary kiln body, and the rotation is restrained and all the rollers are in contact with the rotary kiln body so that the rotation of the roller chain is not synchronized with the rotation of the kiln. To clog up.

  In addition, the solid waste thrown into the furnace is uniformly stirred by a plurality of rows of stirring lift pins attached to the kiln body at intervals of about 1 m in the circumferential direction, and the solid waste is uniformly heated in the furnace in a short time. In response to the radiation heat from the gas, thermal decomposition proceeds rapidly. If the arrangement of the agitation lift pins is a reverse spiral arrangement, the agitation device row is preferable because the forward movement of the solid waste is hindered and the effect of increasing the residence time in the furnace appears.

  Using the solid waste incineration facility having the same configuration as in FIG. 3, the demonstration operation was performed for the two types of waste plastic-containing solids in Table 1.

  Although the actual machine operation results are shown in Table 2, it was not detected as a result of investigating CO as an unreacted gas remaining in the exhaust gas at the outlet of the secondary combustion furnace, and good processing performance was confirmed.

The present invention is a method for providing a means for effectively utilizing the heat retained in solid waste. Conventionally, a large amount of fossil fuel such as heavy oil is used when incinerating waste liquid with low calorific value and non-combustibility. It was. On the other hand, when the retained heat of solid waste is used as an alternative to heavy oil, the amount of incineration of waste liquid is limited due to the limitation of the complete combustion limit of solid waste. In the present invention, the conditions under which the waste liquid can be spray-incinerated in the combustion process of the gasification product gas of solid waste have been found, and according to the present invention, significant savings in fossil fuels such as heavy oil can be expected. In the past, recovery of retained heat from solid waste has been mainly focused on thermal recycling using a waste heat boiler and steam turbine power generation. The method of the present invention, which can save fossil fuels, can achieve substantial thermal recycling with higher efficiency than bad power generation.
According to the present invention, the retained heat of solid waste that is difficult to use can be easily used for waste liquid incineration, so that significant savings in fossil fuel can be achieved. It is.

It is explanatory drawing of the conventional fluidized bed incinerator. It is explanatory drawing of the conventional rotary kiln incinerator. It is explanatory drawing regarding the installation of the rotary kiln, the stoker furnace, and the secondary combustion furnace showing embodiment of this invention. It is a structure of the seal structure of a rotary kiln rotation part, and a lift pin stirrer. It is sectional drawing of the AA line shown in FIG. FIG. 6 is a detailed view of the part a shown in FIG.

Explanation of symbols

FIG.

DESCRIPTION OF SYMBOLS 1 Solid waste input hopper 1a Solid waste cutting conveyor 2 Fluid bed 3 Wind box 4 Residue discharge pipe 5 Waste liquid injection nozzle 6 Waste liquid spray nozzle 7 Free board 8 Dispersion plate 21 Fluidized bed furnace discharge thermometer

FIG.

9 Solid waste charging hopper 9a Solid waste cutting conveyor 10 Furnace front fixed hood 11 Rotary kiln 12 Furnace bottom fixed hood 13 Secondary combustion furnace 14 Rotary kiln combustion space 15 Secondary combustion furnace combustion space 16 Rotary kiln waste liquid spray nozzle 17 2 Secondary combustion furnace waste spray nozzle 18 Residue discharge chute 19 Secondary combustion furnace outlet thermometer 20 Auxiliary burner

FIG.

31 Solid waste charging hopper 32 Solid waste cutting conveyor 33 Rotary kiln auxiliary burner 34a Input hopper waste liquid injection port 34b Rotary kiln waste liquid spray nozzle 35 Rotary kiln combustion space 36 Rotary kiln 37 Pre-furnace fixed hood 38 Furnace sealing device 39 Furnace bottom Sealing device 40a First row waste agitating device 40b Second row waste agitating device 41 Furnace bottom fixing hood 42a Furnace bottom fixing hood side wall surface 42b of rotary kiln bottom upper half circle Rotary kiln bottom half bottom furnace Bottom hood side wall 43 Rotary kiln furnace bottom end face 44 Grate 45 Stoker furnace 46 Incineration ash discharge conveyor 47 Furnace bottom fixed hood combustion burner 48 Secondary combustion furnace combustion space 49 Secondary combustion furnace 50 Stoker furnace auxiliary burner 51 Furnace bottom fixation Hood combustion space 52 Furnace bottom fixed hood spray nozzle 53 Secondary combustion furnace spray Zur 54 corrosion resistant liner 55 liner mounting bolts 56 secondary combustion furnace outlet thermometer

FIG.

34b Rotary kiln waste liquid spray nozzle 35 Rotary kiln combustion space 38 Pre-furnace seal device 40a First row waste agitator 40b Second row waste agitator 60 Joint sheet 61 Roller chain 62 Retaining bolt 63 Retaining plate B
64 Sealing part sliding seat 65 Holding plate A

FIG.

42a Furnace bottom fixing hood side wall surface 42b of rotary kiln top bottom semicircle section Furnace bottom fixing hood side wall surface 43 of rotary kiln bottom bottom semicircular section 43 Rotary kiln bottom bottom end face 44 Grate 46 Incinerated ash discharge conveyor 52 Hood spray nozzle 53 Secondary combustion furnace spray nozzle 55 Liner mounting bolt

FIG.

54 Heat and corrosion resistant liner 55 Liner mounting bolt

Claims (5)

  In a gasification rotary kiln that performs partial combustion gasification of solid waste, the waste liquid is subjected to evaporative decomposition treatment in a rotary kiln maintained at a high temperature of 800 ° C. or higher at the rotary kiln outlet in a reducing atmosphere. The waste liquid is supplied into the rotary kiln by the waste liquid inlet provided on the wall surface of the waste charging hopper as the first supply means, or by the waste liquid spray nozzle provided in the fixed hood in front of the furnace as the second supply means of the waste liquid. In order to evaporate and decompose the waste liquid in the combustion space of the rotary kiln furnace bottom fixed hood and the combustion space of the secondary combustion furnace for burning the combustible exhaust gas generated from the first processing step and the combustion space of the secondary combustion furnace. As a third supply means of waste liquid, a rotary kiln bottom hood fixing hood and / or a waste liquid spray nozzle provided on the secondary combustion furnace furnace wall, the rotor The second liquid treatment step in which the waste liquid can be supplied to the kiln furnace bottom fixed hood and / or the secondary combustion furnace and spray incineration constitutes the evaporative decomposition means of the waste liquid, and the supply of the waste liquid is the first supply means and the second supply. The waste liquid incineration processing method is performed by any one or a combination of means and third supply means.   The furnace wall surface of the rotary kiln furnace bottom fixing hood is generally the horizontal center of the rotary kiln in order to peel and remove the clinker attached to the furnace wall, which is mainly composed of desorbed ash in the waste liquid and to which fly ash derived from solid waste is added. The surface of the wall of the refractory located below the line portion is covered with a corrosion-resistant and heat-resistant metal liner, and when the weight of the clinker exceeds the adhesion with the metal liner, it naturally peels and falls, and further in the rotary kiln The waste liquid incineration method according to claim 1, further comprising a clinker removal and discharge step for carrying out of the furnace by a stalker furnace installed for incineration of the pyrolysis residue. 2. The rotary kiln is provided with a corrosion-resistant and heat-resistant metal lift pin, and leakage air into the furnace of the rotary kiln rotary sliding portion is suppressed to 200 Nm ³ / h or less per 1 m of seal length. Or the waste liquid incineration processing method of 2. If the reducing atmosphere in the furnace is difficult to maintain due to partial combustion gasification of solid waste or partial combustion gasification, the combustion air of the auxiliary burner attached to the fixed hood in front of the kiln furnace The required amount of heat is added by reducing combustion in the range of 0.5 to 0.9, the exhaust gas temperature at the rotary kiln bottom is at least 800 ° C., and the lower heating value of the generated gas is at least 300 kcal / Nm ³ or more and the hydrogen gas concentration is maintained at 6% or more, and / or the exhaust gas temperature after incineration of the waste liquid in the secondary combustion furnace using the combustion heat of the rotary kiln generation gas and char is The waste liquid incineration method according to any one of claims 1 to 3, wherein the theoretical combustion is at least 1200 ° C or higher during theoretical combustion with an air ratio of 1.0. .   Of the end face of the rotary kiln furnace bottom, the rotary kiln has the furnace semi-fixed hood furnace wall approximately so that the upper semicircle moves backward from the rotary kiln furnace bottom fixed hood furnace wall and the lower semicircle projects from the furnace wall. The rotary kiln bottom end face is prevented from being contaminated by the ash that melts and flows from the wall surface of the upper part of the secondary furnace by being configured in steps at the horizontal center line of the rotary kiln. The waste liquid incineration processing method according to any one of the above.

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