JPH1077479A - Thermal decomposition reactor, reactor for partial oxidation and dry distillation, and apparatus for producing solid fuel and gaseous fuel - Google Patents

Abstract

PROBLEM TO BE SOLVED: To provide a thermal decomposition reactor suitable for use in producing a solid fuel and a gaseous fuel which reactor enables not only the production of a large amount of a middle calory gas, a high calory gas and a light oil, but also the production of a solid fuel having high quality. SOLUTION: This reactor is a counter-current double tube thermal decomposition reactor 17 and includes an inner tube 18 and an outer tube 19 which are arranged concentrically. The inner tube 18 has a portion of larger diameter 18a at the outlet side end. A space for heating 20 is present between the inner tube 18 and the outer tube 19. A gaseous fuel-feeding means 21 and an air- feeding means 22 are arranged in the vicinity of the outlet side end of outer tube 19 for feeding a gaseous fuel and air, respectively, to the space for heating 20. On the other hand, a flue gas-exhausting means 23 is disposed in the vicinity of the inlet side end. At the outlet side end of the inner tube 18 is disposed a shaft furnace type reactor 30 as a reactor for partial oxidation and dry distillation.

Description

DETAILED DESCRIPTION OF THE INVENTION

[0001]

BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a pyrolysis reactor, a partial oxidation / distillation reactor, and a solid fuel and fuel gas producing apparatus for producing solid fuel and fuel gas from coal.

[0002]

2. Description of the Related Art Conventionally, solid fuels such as coke have been produced from coal as a raw material. Coke is obtained by high-temperature carbonization of coal. Coal is a heterogeneous substance composed of various types of macerals. Therefore, during coke production, a mixture of the active component and the inactive component in the coal structure must be melt-bonded in the softening and melting temperature range of 350 to 500 ° C. There is. Therefore, in order to produce lump coke for iron making, what is called caking coal which softens and melts in the above-mentioned temperature range of the heating process and has a certain degree of coalification is required. Therefore, relatively expensive coal must be used as compared with coal used for power generation or fuel.

[0003] Furthermore, in view of the future depletion of coking coal and the resulting rise in price, the necessity of effective utilization of inferior coal will become increasingly important in the future. However, when poor quality coal having a small amount of active ingredients such as weathered or non-caking coal, slightly caking coal or weakly caking coal is used as a coke raw material, the adhesion of the active ingredients becomes insufficient. As a result, no coke mass is obtained, or even if it is obtained, the coke yield and coke strength are reduced.

[0004] Under these circumstances, for the purpose of producing coke for iron making, a coal-based pitch or a petroleum-based pitch is added as a binder to relatively inexpensive coal having low softening and melting properties to produce coke for metallurgy. A technique has been established (for example, JP-A-58-61177).

[0005] However, it is difficult to uniformly mix the coal and the binder by adding the binder to the coal for producing the metallurgical coke described above. In particular, it is impossible to infiltrate the coal-based pitch or the petroleum-based pitch into the fine voids inside the coal. For this reason, there arises a problem that the particles are not sufficiently bonded to each other during the carbonization of coal. For example, in the disclosed method, at most 3 to
It only binds particles of 50 μm and cannot bind to the level of maceral components in coal particles such as coking coal, which is the raw material of the original coke.

In addition, segregation occurs due to the flow of the binder, and the properties of the obtained coke become non-uniform.
For this reason, various inconveniences have occurred, such as a decrease in lump yield and a decrease in coke strength. In addition, there is also a problem that it is difficult to take out the furnace due to adhesion of carbon to the furnace wall due to segregation due to the flow of the binder and adhesion of pyrolytic carbon to the furnace wall due to volatilization.

[0007] Various coal gasification technologies have already been established with the background of effective utilization of coal resources. One of the evaluation criteria of such a coal gasification process is a carbon utilization rate. That is, in the coal gasification process, it is required that the carbon content remaining in the fly ash and main ash finally generated is low. For this reason, in many coal gasification processes, it is necessary to separately burn solid carbon components such as char generated by coal gasification.

In the conventional coal gasification technology, ash (inorganic impurities) in coal is melted as slag at an extremely high temperature of 1500 ° C. or more and discharged from the gasifier. For this reason, operational troubles such as clogging by the molten slag are likely to occur.

[0009] In addition to the use of coal as described above, in the field of petroleum refining, delayed oil distillation, as a heavy oil pyrolysis process to obtain light oil, gas, pitch, char or coke by pyrolysis, is used as a delayed cracking process. Various processes such as caulking, flexi caulking, EUREKA, CHERRY-P, and visbreaking are known. For example, a visbreaker for fuel oil production has a mild pyrolysis condition, so that heavy oil can be pyrolyzed in a coil in a liquid state, and has an advantage as a continuous process. Also,
Flexi coking aims to convert heavy oil as much as possible into gas, and gasifies coke produced by this method.

However, flexi coking, a pyrolysis process of petroleum heavy oil, recycles coke generated by pyrolysis in the process and partially gasifies it in order to increase the gas yield. It requires a good driving skill. In addition, visbreaking has mild pyrolysis conditions, but has a high yield of heavy fuel, and its utility value is small.

As a method of mixing coal and heavy oil to use as fuel, for example, Japanese Patent Application Laid-Open No. Sho 60-11596
No. 3 discloses a COM (Coal Oil Mixture). This method has an advantage in that it can be continuously subjected to a reaction process by slurrying coal, but it is intended for use as a fuel for combustion. Not applicable. Further, in the COM combustion process, heavy oil is simply used as fuel, so it cannot be said that heavy oil was effectively used. In addition, expensive additives are required to stably disperse the coal slurry during COM production.

As described above, various techniques for producing a solid fuel such as coke from coal, and techniques for gasifying coal have been studied and published. However, the yield of light oils and fuel gases such as medium and high calorie gases,
In addition, none of the properties required for solid fuel such as lump yield, drum strength, and post-reaction strength are satisfactory.

[0013]

SUMMARY OF THE INVENTION The present invention has been made in view of the above-mentioned circumstances, and it is possible to produce a large amount of medium-calorie gas, high-calorie gas and light oil using coal as a raw material, and to provide a high-quality solid fuel. The present invention provides a pyrolysis reactor, a partial oxidation and dry distillation reactor, and a solid fuel and fuel gas production apparatus for producing a solid fuel and a fuel gas, which can obtain a solid fuel and a fuel gas.

[0014]

SUMMARY OF THE INVENTION The present invention firstly provides a light oil, which is obtained by pyrolyzing a mixture of coal and a liquid carbon-containing substance.
A pyrolysis reactor for obtaining a high-calorie gas and a pyrolysis residue, an inner pipe part in which the mixture moves from an inlet side to an outlet side thereof, and provided so as to surround an outer periphery of the inner pipe part, An outer tube defining a heating space in which a heating gas flows from an outlet side to an inlet side of the inner tube between the inner tube and the inner tube. .

[0015] Second, the present invention provides a partial oxidation / dry distillation reaction in which a pyrolysis residue obtained by pyrolysis of a mixture of coal and a liquid carbon-containing substance is subjected to dry distillation and partial oxidation to obtain a medium calorie gas and a solid fuel. Vessel, a hollow body, a supply mechanism for supplying the pyrolysis residue into the main body provided at the upper end of the main body, and the solid fuel provided at the lower end of the main body. A reactor for partial oxidation and carbonization, comprising: a discharge mechanism for discharging, and an oxygen-containing gas supply means for supplying an oxygen-containing gas to a lower portion in the main body.

[0016] Thirdly, the present invention provides a method for producing a light oil, a high calorie gas and a pyrolysis residue by pyrolyzing a mixture of coal and a liquid carbon-containing substance, and then subjecting the pyrolysis residue to dry distillation and partial oxidation. A solid fuel and fuel gas producing apparatus for obtaining a medium calorie gas and a solid fuel, wherein an inner pipe part in which the mixture moves from an inlet side to an outlet side thereof, and an outer periphery of the inner pipe part. A pyrolysis reactor having an outer tube portion that defines a heating space in which a heating gas flows from the outlet side to the inlet side of the inner tube portion between the inner tube portion and a hollow space. A main body, a supply mechanism for supplying the pyrolysis residue into the main body provided at the upper end of the main body, and a discharge mechanism for discharging the solid fuel provided at the lower end of the main body. Oxygen at the bottom inside the body Yes gas oxygen-containing gas supply means and apparatus for producing a solid fuel and a fuel gas, characterized in that it comprises a reactor for partial oxidation and carbonization with for supplying. I will provide a.

[0017]

Embodiments of the present invention will be described below with reference to the drawings. FIG. 1 is a schematic diagram showing one embodiment of the solid fuel and fuel gas production apparatus of the present invention. In the figure, reference numeral 11 denotes a coal hopper. Coal hopper 1
A ball mill 12 is provided as a mixer on the discharge side of No. 1. Further, a tank 13 for a carbon-containing substance is connected to the ball mill 12 via a plunger pump 14. A service tank (capacity: 5 m ³ ) 15 is provided downstream of the ball mill 12. A twin screw pump 16 is provided downstream of the service tank 15. On the discharge side of the twin-screw pump 16, a countercurrent double-tube thermal decomposition reactor 17 is provided.

The countercurrent double tube type pyrolysis reactor 17 has an inner tube portion 18 and an outer tube portion 19 which are arranged concentrically with each other. The inner pipe portion 18 has a large-diameter portion 18a at the outlet end. A heating space 20 is provided between the inner tube 18 and the outer tube 19. Fuel gas supply means 21 and air supply means 22 for supplying fuel gas and air to the heating space 20 are provided near the outlet end of the outer tube portion 19.
Is provided. On the other hand, a combustion exhaust gas exhaust means 23 is provided near the inlet-side end of the outer pipe portion 19.

A gas / residue separation section 24 is provided at the outlet side of the inner pipe section 18 so as to communicate with the inner pipe section 18. At the top of the gas / residue separation section 24, a gas outlet pipe 2
5 is connected. The outlet side of the gas outlet pipe 25 branches into two branch pipes 26 and 27.

At the bottom of the gas residue separation section 24, two residue dampers 28, 29 are vertically stacked.
Below the lower residue damper 29, a shaft furnace type reactor 30 as a reactor for partial oxidation and dry distillation is arranged. A recovery pipe 31 for recovering medium calorie gas generated in the shaft furnace type reactor 30 is connected to an upper portion of the shaft furnace type reactor 30 as described later. Further, an oxygen-containing gas supply means 32 is attached to a lower portion of the shaft furnace type reactor 30. Shaft furnace type reaction vessel 30
Two solid fuel dampers 33 and 34 are vertically stacked at an outlet provided at the lower end of the solid fuel damper.

In the solid fuel / fuel gas producing apparatus 10 as described above, solid fuel and fuel gas are produced as follows. First, the raw coal stored in the coal hopper 11 is introduced into the ball mill 12. On the other hand, the liquid carbon-containing substance contained in the tank 13 is sent to the ball mill 12 by the plunger pump 14.

The raw material coal used in the present invention is not particularly limited, and for example, peat, lignite, sub-bituminous coal, bituminous coal and the like can be used. On the other hand, the liquid carbon-containing material 12
Is a liquid substance containing carbon. Liquid carbon-containing substance, for example, coal tar, tar pitch,
Tar distillation intermediate products, tar slag, heavy oil, waste oil, sludge,
It is at least one selected from the group consisting of a waste liquid and an organic waste solvent.

Here, the coal tar is not particularly limited, but those produced as a by-product from a coke oven in an iron making process can be suitably used. As the heavy oil, a straight-run type normal pressure residual oil, a vacuum residual oil, asphaltene, and a cracking type petroleum heavy oil such as ethylene tar and FCC decant oil are used. Further, coal-based coal liquefaction residual oil, oil sand-based orinoco tar, cold lake, and the like can also be used. Waste oil is waste oil generated in the rolling process,
Waste paint, tandem waste oil or waste grease. Also,
The sludge is, for example, activated sludge generated in a coke oven gas purification process, sludge-like oil sludge generated in a rolling process, sludge generated in papermaking, and other general sewage sludge.
The waste liquid is, for example, pulp waste liquid.

Next, the coal is pulverized and mixed with the liquid carbon-containing material by the ball mill 12 to obtain a slurry. The mixer is not particularly limited as long as it can uniformly mix both components, in addition to the ball mill 12, but a screw mixer, a ball mill, a rod mill, or the like can be used. Ball mills and rod mills are preferred because they can be ground simultaneously with mixing.

When a ball mill 12 or a rod mill is used as a mixer, the particle size of the coal powder is about 5 m in order to form a slurry by mixing with a liquid carbon-containing substance.
m or less, more preferably 100 μm or less.

When a ball mill or a rod mill is not used, the coal may be pulverized in advance. In order to pulverize coal, a mechanical shear pulverizer, a high-speed rotary impact pulverizer, a jet mill, or the like can be used.

The mixing time may be appropriately selected according to the mixing ratio. In the case where a ball mill or a rod mill or the like is used for pulverization, the mixing time is preferably from 5 minutes to 60 minutes, depending on the type of coal. Further, the mixing temperature must be kept below 100 ° C. in order to prevent the slurry from solidifying. The mixing ratio of the coal and the liquid carbon-containing substance is not particularly limited, but is preferably 1: 0.5 or more by weight.

The obtained slurry is guided to a service tank 15 such as a service tank by a pump such as a twin screw pump and stored therein. Also in this storage, the temperature in the tank needs to be kept below 100 ° C. so that solidification of the slurry does not occur. The slurry may be introduced into the next countercurrent double-tube thermal decomposition reactor 17 without being stored in the service tank 15.

The slurry stored in the service tank 15 is pushed by a twin screw pump 16 into an inner tube portion 18 of a countercurrent double-tube type pyrolysis reactor 17 as a pyrolysis reactor. The slurry is supplied to a twin screw pump 16
, The inner tube portion 18 gradually advances from the inlet side to the outlet side. In addition to the twin screw pump 16, a snake pump, an extrusion pump, a diagram hose pump, a plunger pump, or the like can be used.

On the other hand, fuel gas and air are supplied into the heating space 20 between the inner pipe section 18 and the outer pipe section 19 through the fuel gas supply means 21 and the air supply means 22. This fuel gas is burned near the outlet of the inner tube portion 18 in the heating space 20. The high-temperature combustion exhaust gas resulting from the combustion of the fuel gas flows through the heating space 20 toward the inlet side of the inner pipe portion 18 and is exhausted through the exhaust gas exhaust means 23.

Accordingly, the slurry slowly moving inside the inner pipe portion 18 is indirectly and continuously heated by the combustion exhaust gas generated by the combustion of the fuel gas. Further, the slurry is indirectly heated by the combustion of the combustion gas near the outlet side of the inner pipe portion 18.

In this embodiment, the combustion exhaust gas of the fuel gas is used as the gas for heating the slurry. Alternatively, high-temperature steam or an electric heater can be used. Also,
The combustion exhaust gas obtained by burning the dust generated from the latter partial oxidation and carbonization reactor can also be used.
In this case, there is an effect that the use amount of the fuel gas described above can be reduced. Further, combustion of the fuel gas in the vicinity of the outlet side of the inner pipe portion 18 is not always necessary, and a heating gas of a predetermined temperature may be introduced into the heating space 20 from another heat source.

The first heat treatment step is performed by heating the slurry in the above-described counter-flow double-tube thermal decomposition reactor 17.
That is, the slurry contains coal and carbon-containing material that has penetrated into the microstructure of the coal. By thermally decomposing this slurry in an inert atmosphere or a reducing atmosphere, a high calorie gas is generated. The high calorie gas is, for example, methane, carbon monoxide, carbon dioxide, ethane, ethylene, propane, propylene, n-butane, i-butane and the like. Further, light oil having a low boiling point contained in the slurry is also separated.

The processing temperature in the first thermal decomposition step is 600
It is below ° C. If the processing temperature exceeds 600 ° C,
This is because a low-calorie decomposition component gas such as hydrogen is generated from the slurry, and the calorie of the obtained gas is reduced.
The lower limit of the treatment temperature is not particularly limited because it can be selected in consideration of the properties of the raw material coal, coal tar, heavy oil, and the like. Specifically, the processing temperature of the first thermal decomposition step is appropriately selected from the range of 300 ° C to 600 ° C.

The mixture of high calorie gas and light oil generated here flows into the gas outlet pipe 25 through the gas / residue separation section 24. The mixture flowing into the gas outlet pipe 25 is cooled while flowing through the gas outlet pipe 25, and light oil having a relatively low boiling point is liquefied. The liquefied light oil is recovered by the decanter 35 through the lower branch pipe 27.
In addition, high calorie gas is recovered through the upper branch pipe 26. On the other hand, the pyrolysis residue is pushed out to the gas / residue separation unit 24 by the slurry fed sequentially, and is temporarily accumulated at the bottom.

In the above-described counterflow type double tube type pyrolysis reactor 17, the temperature distribution in the inner tube portion 18 is higher as it is closer to the outlet side of the inner tube portion 18. That is, the inner tube portion 18
The vicinity of the outlet is heated by combustion of the fuel gas in the heating space 20 and thus has the highest temperature. When approaching the inlet of the inner pipe section 18, the inside of the inner pipe section 18 is heated only by the sensible heat of the combustion exhaust gas of the fuel gas. The temperature of the combustion exhaust gas is controlled by the inner pipe section 18.
It gets lower near the entrance. As a result, the inner pipe 18
Inside, a temperature gradient is formed in which the temperature increases from the inlet side to the outlet side.

The inner tube portion 1 provided with such a temperature gradient
When the slurry is heated while being gradually fed in 8, the interaction between the coal and the liquid carbon-containing substance (swelling reaction) occurs sufficiently due to the low rate of temperature rise of the slurry, and finally the strength is high. There is an advantage that a solid fuel can be obtained.

In addition, pitch is contained in the slurry, that is, the mixture of coal and the liquid carbon-containing substance. When the coking for this pitch proceeds, the slurry is re-solidified, the fluidity of the slurry decreases, and in the worst case,
The so-called coking in which the slurry is clogged in the inner tube portion 18 may occur. When caulking occurs, operations need to be stopped. In order to prevent such coking of the slurry, a large-diameter portion 18a having an inner diameter larger than the inner diameter of the inlet-side end of the inner tube 18 is provided at the outlet-side end of the inner tube 18. For this reason, even if the processing temperature in the large diameter portion 18 exceeds the re-solidification temperature for the pitch and the slurry is re-solidified, coking is unlikely to occur.

As described above, in this countercurrent double-tube type pyrolysis reactor 17, the slurry moving from the inlet side to the outlet side of the inner pipe portion 18 in the inner pipe portion 18 is supplied to the heating space 2 as described above.
The fuel gas is burned in the vicinity of the outlet of the inner tube 18 and the heating space 20 is heated by the combustion exhaust gas flowing from the outlet to the inlet of the inner tube 18. Therefore, as described above, the temperature in the heating space 20 has a temperature gradient in which the temperature increases from the inlet side to the outlet side of the inner pipe portion 18. Therefore, resolidification of the slurry due to thermal decomposition of the pitch in the slurry is likely to occur on the outlet side of the inner tube portion 18 where the slurry is heated at a high temperature. Therefore, as shown in FIG. 2, by making the inner diameter D of the outlet end of the inner pipe 18 larger than the inner diameter d of the inlet end, the inner pipe 1
In this case, coking can be prevented from occurring due to the slurry re-solidified at the outlet end portion of FIG.

In order to make the inner diameter D of the outlet end of the inner pipe 18 larger than the inner diameter d of the inlet end, for example, the inner pipe 1
As shown in FIG. 3 (A), the inner tube 1
Either the large-diameter portion 40 having an inner diameter D larger than the inner diameter d of the inlet-side end of the inner tube portion 8 is formed, or as shown in FIG. An enlarged diameter portion 41 is formed.

The inner diameter D of the large diameter portion 40 and the large diameter portion 41 is
For example, it is set to 110 to 200% of the inner diameter d with respect to the inner diameter d of the inlet end of the inner pipe portion 18. More preferably, the large diameter portion 40 and the large diameter portion 41 are formed in a region of the heating space where the temperature of the slurry in the heating space 20 is equal to or higher than the re-solidification temperature of the pitch in the slurry. Resolidification of the slurry occurs by thermal decomposition of the pitch as described above.
Therefore, by increasing the inner diameter of the inner tube portion 19 in the region of the heating space 20 where resolidification of the slurry may occur, it is possible to further reduce the possibility of coking of the slurry. The resolidification temperature for the pitch is
It depends on the type of liquid carbon-containing material. For example, when coal tar is used as the liquid carbon-containing substance, the re-solidification temperature of the pitch is 490 ° C. Therefore, in this case, the temperature of the slurry in the heating space 20 is 490 ° C.
The large-diameter portion 40 or the large-diameter portion 41 is formed in the inner tube portion 18 in the above-described region.

Thus, as shown in FIGS. 3A and 3B, the inner pipe portion 18 has a large-diameter portion 40 or a large-diameter portion 41 and an inlet-side portion having an inner diameter smaller than these. Small diameter part 4
2, the large diameter portion 40 or the large diameter portion 41 and the small diameter portion 4
2 may be integral or may be connected to separate tubes. The inner tube 18 and the outer tube 19 are
For example, it is made of a stainless tube.

The pyrolysis residue obtained in the first heat treatment step described above is supplied from the bottom of the gas / residue separation section 24 into the shaft furnace type reactor 30 via the residue dampers 28 and 29. In the shaft furnace type reactor 30, as described below, a second heat treatment step of high-temperature carbonization of the pyrolysis residue and a third heat treatment step of partially oxidizing the carbonization residue generated in the second heat treatment step are performed.

In the shaft furnace type reactor 30, as shown in FIG. 4, a pyrolysis residue 50 before carbonization and a carbonization residue 51 after carbonization are deposited. In addition, for convenience of explanation, in FIG. 4, the pyrolysis residue 50 and the dry distillation residue 51 are partially omitted.

The lower portion of the shaft furnace type reaction vessel 30 is filled with a dry distillation residue 51 after the dry distillation, and an oxygen-containing gas is supplied through an oxygen-containing gas supply means 32 to form an oxidizing atmosphere ( Hereinafter, referred to as oxidation reaction zone 52).
In the oxidation reaction zone 52, the dry distillation residue 51 is partially oxidized, in other words, the dry distillation residue 51 is partially burned. Specifically, the partial oxidation of the carbonization residue is performed by supplying an oxygen-containing gas as a gasifying agent and partially oxidizing the carbonization residue in an oxygen atmosphere. Here, the partial oxidation is to partially oxidize or burn individual dry distillation residues. Medium calorie gas 53 is generated by burning the carbonization residue, and a solid fuel is obtained. The calorie gas 53 contains carbon monoxide and hydrogen. Carbon monoxide is carbon dioxide generated by the partial oxidation of the carbonization residue, that is, the carbon dioxide generated by combustion, reacts with carbon present in the surrounding carbonization residue to change.

The solid fuel obtained in the third heat treatment step is coke, bean charcoal, briquette, briquette fuel and the like. The type of the obtained solid fuel is determined by the quality of the raw coal, the amount of the caking component in the liquid carbon-containing substance, and the like.

The oxygen-containing gas used here is, for example, air, oxygen gas, a mixed gas of oxygen and water vapor, or a mixed gas of oxygen and carbon dioxide. The third heat treatment step needs to be performed at a temperature of 1200 ° C. or lower. If the processing temperature exceeds 1200 ° C., the strength of the obtained solid fuel decreases. The lower limit of the treatment temperature is not particularly limited because it can be selected in consideration of the properties of the raw material coal, the liquid carbon-containing substance, and the like. However, at processing temperatures below 800 ° C., partial oxidation is slow,
Since the desired medium calorie gas and solid fuel cannot be obtained efficiently, the temperature is preferably in the range of 800 ° C to 1200 ° C.

The ratio of the partial oxidation of the dry distillation residue in the third heat treatment step is selected, for example, within the range of 10 to 80%.
If the ratio of the partial oxidation is lower than 10%, the calorific value required for dry distillation of the pyrolysis residue cannot be obtained, and the amount of medium calorie gas generated may be reduced. On the other hand, 80%
If it is higher than this, the ash content in the solid fuel increases, and the calorific value of the solid fuel decreases. Further, the strength of the solid fuel may decrease, and the amount of dust generated in the third heat treatment step may increase.

It is preferable that the ratio of the partial oxidation is determined according to the ratio of the ash in the coal. The solid fuel has a lower strength as the ash content increases, and it becomes difficult to maintain the shape.
For example, when the proportion of ash in coal is 15% by weight, it is possible to set the proportion of partial oxidation of the dry distillation residue using coal tar 1.5 times that of coal to about 25%. On the other hand, when the ash content in the coal is 1 to 2% by weight, the ratio of partial oxidation can be set up to about 80%. The ratio of the partial oxidation can be changed by changing the supply amount of the oxygen-containing gas as a gasifying agent, or the amount of water vapor when the oxygen-containing gas is a mixed gas of oxygen and water vapor. Thereby, the amount of medium calorie gas generated can be adjusted arbitrarily.

The medium calorie gas 53 mainly composed of carbon monoxide and hydrogen generated in the oxidation reaction zone 52 is non-oxidizing and has a high temperature (800 to
1200 ° C). The middle calorie gas 53 rises, and the surroundings of the pyrolysis residue 50 before the dry distillation, which is deposited on the upper side of the dry distillation residue 51, becomes a non-oxidizing and high temperature medium calorie gas 53 atmosphere (hereinafter, non-oxidizing atmosphere). Oxidation reaction zone 54
). In the non-oxidation reaction zone 54, the pyrolysis residue 50 is heat-distilled by the sensible heat of the middle calorie gas 53, and the carbonization gas is generated and the carbonization residue 51 is obtained. The generated carbonized gas is recovered through the recovery pipe 31 shown in FIG. 1 together with the medium calorie gas 53 generated in the oxidation reaction zone. The dry distillation gas generated here is a high-concentration hydrogen gas containing hydrogen as a main component since the high calorie gas generated in the first heat treatment step has been generated.

The solid fuel obtained by the partial oxidation in the oxidation reaction zone 52 is supplied to the solid fuel dampers 33, 3 shown in FIG.
4 to recover the non-oxidation zone 5
The dry distillation residue 50 obtained in 4 gradually moves to the oxidation reaction zone 52 by its own weight. By supplying the pyrolysis residue 50 to the shaft furnace reactor 30 according to the amount of the collected solid fuel, dry distillation and partial oxidation can be continuously performed.

When the operation of the solid fuel / fuel gas producing apparatus 10 is started, the pyrolysis residue 50 is supplied and stored in the shaft furnace type reactor 30 in a fixed amount. At this stage, an oxygen-containing gas is supplied to a lower portion of the shaft furnace type reaction vessel 30 to partially oxidize the pyrolysis residue 50 and use a high-temperature non-oxidizing gas generated by combustion of the pyrolysis residue 50 to form a non-oxidizing gas. An oxidation reaction zone 54 is formed, and dry distillation of the pyrolysis residue 50 is started.

FIG. 5 is a schematic diagram showing a modification of the solid fuel / fuel gas producing apparatus 10 shown in FIG. In this modification, the bottom of the gas / residue separation unit 24 and the residue damper 2
Between the positions 8 and 29, a double-roll forming device 70 is arranged. After the pyrolysis residue obtained in the first heat treatment step is formed by the double roll type forming device 70, it is supplied to the shaft furnace type reactor 30 via the residue dampers 28 and 29. By forming the pyrolysis residue, the particle size of the pyrolysis residue is uniformed and the strength is enhanced, so that uniform partial oxidation can be performed in the third heat treatment step, and the particle size of the finally obtained solid fuel is reduced. It becomes uniform and easy to use. Also, since the strength of the solid fuel is increased by molding,
The grade of raw coal used to obtain a solid fuel having a desired strength can be reduced, and an economic effect can be obtained.

As described above, in the solid fuel and fuel gas production method using the solid fuel and fuel gas production apparatus 10 shown in FIG. 1, the non-oxidation reaction zone of the shaft furnace type reactor 30 is used as a partial oxidation and dry distillation reactor. The heating and dry distillation of the pyrolysis residue in the second heat treatment step at 54 uses the sensible heat of the medium calorie gas in the atmosphere of the non-oxidizing medium calorie gas generated in the third heat treatment step in the oxidation reaction zone 52. It is performed using.
That is, as described above, in the third heat treatment step of the present invention, the carbonized residue obtained in the second heat treatment step is partially oxidized, and a medium calorie gas rich in carbon monoxide is generated. The calorie gas is non-oxidizing and 80
It is a high temperature of 0 to 1200 ° C. The sensible heat of the calorie gas is used for dry distillation in the second heat treatment step. At the same time, the surrounding atmosphere of the dry distillation is made non-oxidizing by medium calorie gas. In this case, the medium calorie gas 20 generated in the third step is recovered after being used in the second heat treatment step. Carbon monoxide and hydrogen generated in the third heat treatment step occupy most of the recovered middle calorie gas 20. The generation of medium-calorie gas in the third heat treatment step is mainly caused by combustion of a part of the dry distillation residue and gasification by steam when the oxygen-containing gas contains steam. This is because the amount is larger than that of the carbonized gas generated by carbonization in the second heat treatment step without combustion.

[0055]

DESCRIPTION OF THE PREFERRED EMBODIMENTS An embodiment of the production of solid fuel and fuel gas using the apparatus for producing solid fuel and fuel gas of the present invention will be described below. Example 1 Production of coke, light tar, high calorie gas and medium calorie gas Using a solid fuel and fuel gas production apparatus 10 shown in FIG. 1, production of coke, light tar, high calorie gas and medium calorie gas was performed. . First, witbank coal as raw material coal at a rate of 100 kg per hour,
The coal was supplied from a coal hopper 11 to a ball mill 12. On the other hand, coal tar as a liquid carbon-containing substance was supplied from a tank 13 to a ball mill 12 by a plunger pump 14 at a rate of 150 kg per hour. In a ball mill 12, whitbank coal was pulverized and witbank coal and coal tar were mixed to obtain a slurry.

The obtained slurry was introduced into the service tank 15 by an extrusion pump and temporarily stored. The inside of the service tank 15 is set at 100 to prevent the coal from swelling and solidifying.
C. was maintained below.

Next, the slurry was supplied from the service tank 15 into the inner pipe portion 18 of the countercurrent double pipe type pyrolysis reactor 17 by the twin screw pump 16. The slurry was heated to 600 ° C. during the transfer in the inner pipe portion 18, and high calorie gas and light tar as light oil were generated. The mixture of high calorie gas and light oil generated here is
After flowing through the gas / residue separation section 24, the gas flowed into the gas outlet pipe 25, and was separately collected through the branch pipes 26 and 27.

On the other hand, the pyrolysis residue was pushed out to the gas / residue separation section 24 by the slurry fed sequentially, and was temporarily accumulated at the bottom. This pyrolysis residue is converted to gas /
From the bottom of the residue separation section 24, the mixture was supplied into a shaft furnace reactor 30 via residue dampers 28 and 29. In the shaft furnace reactor 30, as described above, oxygen and water vapor are supplied as oxygen-containing gases to the lower part of the shaft furnace reactor 30 to dry-dry the pyrolysis residue and partially oxidize the dry- distillation residue at 1200 ° C. went. As a result, medium calorie gas was recovered from the furnace top of the shaft furnace type reactor 30 and coke as a solid fuel was recovered from the bottom.

Comparative Examples 1 and 2 As Comparative Example 1, coke, light tar, and the like were prepared using a batch-type pyrolysis reactor 61 shown in FIG. 6 as a pyrolysis reactor.
Production of high calorie gas and medium calorie gas was performed.
6, the same reference numerals as those in FIG. 1 denote the same components as in FIG. First, in the same manner as in Example 1, witbank coal is supplied as a raw coal, a coal hopper 11 is supplied to a ball mill 12, coal tar is supplied as a liquid carbon-containing substance, and a ball mill 12 is supplied from a tank 13 by a plunger pump 14.
Supplied. In a ball mill 12, whitbank coal was pulverized and witbank coal and coal tar were mixed to obtain a slurry. This slurry was temporarily stored in the service tank 15.

Next, the slurry was supplied from the service tank 15 to a batch type (pot type) thermal decomposition reactor 61. The slurry processed 250 kg per batch. In this batch type pyrolysis reactor 61, the slurry was heated to 600 ° C., and high calorie gas and light tar as light oil were generated. The mixture of high-calorie gas and light oil generated here flows into the gas outlet pipe 62, and the branch pipe 63,
Through 64, high calorie gas and light tar were separately recovered.

On the other hand, the pyrolysis residue left in the batch type pyrolysis reactor 61 was taken out and supplied to the same shaft furnace type reactor 30 as in Example 1. Shaft furnace type reactor 30
In the same manner as in Example 1, the pyrolysis residue was subjected to dry distillation and 12
Partial oxidation of the dry distillation residue at 00 ° C. was performed. As a result, medium calorie gas was recovered from the furnace top of the shaft furnace type reactor 30 and coke as a solid fuel was recovered from the bottom.

As Comparative Example 2, coke, light tar, high calorie gas and medium calorie gas were produced using a semi-continuous (delayed coker type) thermal decomposition reactor 71 shown in FIG. In FIG. 7, the same reference numerals as those in FIG. 1 indicate the same components as those in FIG.

Whitbank coal was supplied as raw coal to a ball mill 12 from a coal hopper 11, and coal tar was supplied to the ball mill 12 from a tank 13 by a plunger pump 14 as a liquid carbon-containing substance. In a ball mill 12, whitbank coal was pulverized and witbank coal and coal tar were mixed to obtain a slurry. This slurry was temporarily stored in the service tank 15.

Next, the slurry from the service tank 15 is supplied to a semi-continuous (delayed coker type) thermal decomposition reactor 7.
The first reaction vessel 72 was supplied. The slurry was heated to 600 ° C. in the reaction vessel 72 to generate light tar and high calorie gas. The mixture of high calorie gas and light oil generated here flowed into the gas outlet pipe 73, and high calorie gas and light tar were separately collected through the branch pipes 74 and 75.

As described above, the slurry was supplied to the second reaction vessel 76 while the thermal decomposition treatment was being performed in the first reaction vessel 72. After the completion of the thermal decomposition treatment in the first reaction vessel 72, the same thermal decomposition treatment was performed in the second reaction vessel 76 to obtain a high calorie gas and light tar.

In this semi-continuous pyrolysis reactor 71, the slurry supply rate was 250 kg per hour. On the other hand, the pyrolysis residue left in the semi-continuous pyrolysis reactor 71 was taken out, and the same shaft furnace reactor 30 as in Example 1 was taken out.
Supplied within. In the shaft furnace type reactor 30, the first embodiment
Similarly to the above, the pyrolysis residue was subjected to dry distillation and the dry distillation residue was partially oxidized at 1200 ° C. As a result, medium calorie gas was recovered from the furnace top of the shaft furnace type reactor 30 and coke as a solid fuel was recovered from the bottom. Table 1 shows the supply rate, the throughput, the coal throughput, the coal tar throughput, the thermal decomposition temperature, and the total processing time of the slurry in Example 1 and Comparative Examples 1 and 2 described above.

[0067]

[Table 1] Table 2 shows the processing amount of the pyrolysis residue, the amount of oxygen blown, the amount of steam supplied, and the processing temperature in the shaft furnace reactor 30 in Example 1 and Comparative Examples 1 and 2.

[0068]

[Table 2]

Table 3 shows the amount of light tar, the amount of calorie gas generated and calorific value, the amount of medium calorie gas generated and calorific value, and the amount of coke generated in Example 1 and Comparative Examples 1 and 2. Show.

[0070]

[Table 3]

The unit heat input per unit in the pyrolysis process of Example 1 and Comparative Examples 1 and 2 was as follows. Example 1 290 Mcal / t-TCM ^* Comparative Example 1 350 Mcal / t-TCM Comparative Example 2 320 Mcal / t-TCM ^* TCM: Coal / tar mixture (Tar-Coal M)
Table 4 shows the variation in the drum strength of the coke obtained in Example 1 and Comparative Examples 1 and 2.

[0072]

[Table 4]

As described above, the production of coke, light tar, high-calorie gas and medium-calorie gas using the countercurrent double-tube pyrolysis reactor 17 of Example 1 has the following effects. It was confirmed that. That is, as is clear from Table 1, the total processing time was shorter than when the batch-type pyrolysis reactor 61 of Comparative Example 1 or the semi-continuous-type pyrolysis reactor 71 of Comparative Example 2 was used. In addition, the unit heat input in the thermal decomposition step in Example 1 was lower than Comparative Examples 1 and 2. Furthermore, the variation in drum strength of the obtained coke was smaller in Example 1 than in Comparative Examples 1 and 2.

Further, by using a continuous pyrolysis reactor, the sensible heat of the pyrolysis residue can be used more efficiently in the subsequent partial oxidation and dry distillation process than in a batch or semi-continuous system. Can be.

Examples 2 to 5 and Comparative Example 3 Coke, light tar, and the like were obtained in the same manner as in Example 1 except that the inner pipe portion 18 of the double-tube pyrolysis reactor 17 shown in FIG. Production of high calorie gas and medium calorie gas was performed.

As the second embodiment, the enlarged diameter portion 4 shown in FIG.
An inner tube portion (hereinafter, referred to as a tapered type) having a diameter of 1 and having a maximum inner diameter D of the enlarged diameter portion 41 equal to 1.1 times the inner diameter d of the small diameter portion 42 was used. As a third embodiment,
FIG. 3 (A) is an inner tube portion having a large diameter portion 40 (hereinafter, referred to as a different diameter tube connection type), and the inner diameter D of the large diameter portion 40 is
The diameter of the small diameter portion 42 was 1.1 times the inner diameter d. In the fourth embodiment, the inner diameter of the tapered inner tube is the same as that of the second embodiment.
2.0 times as large as the inner diameter d was used. Further, as Example 5, an inner tube portion of a different diameter pipe connection type similar to Example 3 in which the inner diameter D of the large diameter portion 40 is 2.0 times the inner diameter d of the small diameter portion 42 is used. Was. As Comparative Example 3, an inner tube portion composed of a straight pipe having an inner diameter equal to the inner diameter d of the small diameter portion of Examples 2 to 5 was used.

Table 5 shows Examples 2 to 5 and Comparative Example 3.
Temperature, light tar generation, stable operation at
The calorific value and calorific value of the high calorie gas and the calorific value of the pyrolysis residue are shown.

[0078]

[Table 5]

As is clear from Table 5, the maximum temperature at which the stable operation can be performed is reduced by the provision of the large diameter portion 40 and the large diameter portion 41 in the inner pipe portion 18 as in Examples 2 to 5. It was confirmed that it was higher than that of. Further, from Examples 2 and 3, it was confirmed that the inner diameter D of the large diameter portion 40 and the enlarged diameter portion 41 was sufficiently effective even when the inner diameter d of the small diameter portion 42 was 1.1 times, that is, 110%. Is the inner diameter D is the inner diameter d
It was confirmed that the effects of Examples 4 and 5, which are 2.0 times higher, were higher than those of Examples 4 and 5.

Further, the pyrolysis temperature in the countercurrent double-tube thermal decomposition reactor 17 using the inner tube of Examples 2 to 5 and Comparative Example 3 was set to 500 ° C. The number of clogging in the tubular pyrolysis reactor 17 and the number of shelving in the shaft furnace type reactor 30 as a partial oxidation / distillation furnace were examined.
Table 6 shows the results.

[0081]

[Table 6]

As is clear from Table 6, the provision of the large-diameter portion 40 and the large-diameter portion 41 in the inner pipe portion 18 as in Examples 2 to 5 makes the countercurrent type It was found that the number of clogging in the double tube type pyrolysis reactor 17 and the number of shelving in the shaft furnace type reactor 30 can be significantly reduced. Further, from Examples 2 and 3, the large diameter portion 4
It has been confirmed that the inner diameter D of the small-diameter portion 41 is 1.1 times the inner diameter d of the small-diameter portion 42, that is, 110%, but the inner diameter D is 2.0 times the inner diameter d. In Examples 4 and 5, the effect of reducing the number of clogging in the countercurrent double-tube thermal decomposition reactor 17 was confirmed to be higher.

Although Comparative Example 3 is inferior to Examples 2 to 5 at a high thermal decomposition temperature, it has no operational problems at a low thermal decomposition temperature and is included in the technical scope of the present invention. Needless to say.

[0084]

As described above, the pyrolysis reactor for producing a solid fuel and a fuel gas according to the present invention comprises a mixture of coal and a liquid carbon-containing substance moving inside an inner pipe.
Since the mixture is heated indirectly and continuously by the heating gas flowing through the heating space between the inner pipe and the outer pipe, the mixture is thermally decomposed in a short time and stably, and light oil and high calorie gas are removed. It can be obtained with high efficiency.

The reactor for partial oxidation and carbonization for the production of solid fuel and fuel gas according to the present invention supplies an oxygen-containing gas from the lower part to partially oxidize the carbonization residue, and partially oxidizes the carbonization residue at the upper part. Since the pyrolysis residue is carbonized in the atmosphere of the high-temperature and non-oxidizing medium-calorie gas generated in the above, a medium-calorie gas can be obtained with high efficiency and a high-quality solid fuel can be obtained.

Further, according to the solid fuel and fuel gas producing apparatus of the present invention, the mixture of the coal and the liquid carbon-containing substance moving in the inner pipe is moved between the inner pipe and the outer pipe in the pyrolysis reactor. Since the mixture is indirectly and continuously heated by the heating gas flowing through the heating space, the mixture can be thermally decomposed in a short time and stably, and light oil and high calorie gas can be obtained with high efficiency. Furthermore, the pyrolysis residue obtained in the pyrolysis reactor is introduced into a reactor for partial oxidation and dry distillation, and in the reactor for partial oxidation and dry distillation, an oxygen-containing gas is supplied from the lower part to partially oxidize the carbonization residue. In the upper part, the pyrolysis residue is carbonized in the atmosphere of high-temperature and non-oxidizing medium-calorie gas generated by partial oxidation, so that medium-calorie gas can be obtained with high efficiency and high quality solid fuel can be produced. Obtainable.

[Brief description of the drawings]

FIG. 1 is a schematic diagram showing a solid fuel and fuel gas production apparatus according to a first embodiment of the present invention.

FIG. 2 is a schematic diagram showing a countercurrent double-tube thermal cracking reactor of the solid fuel and fuel gas production apparatus shown in FIG.

FIGS. 3A and 3B are schematic diagrams each showing an example of an inner tube portion.

FIG. 4 is a schematic diagram showing a shaft furnace type reactor of the solid fuel and fuel gas production apparatus shown in FIG.

FIG. 5 is a schematic diagram showing a main part of a modified example of the solid fuel and fuel gas production apparatus shown in FIG. 1;

FIG. 6 is a schematic diagram showing a solid fuel and fuel gas production apparatus including a batch-type pyrolysis reactor according to Comparative Example 1.

FIG. 7 is a schematic diagram showing a solid fuel and fuel gas production apparatus including a semi-continuous pyrolysis reactor according to Comparative Example 2.

[Explanation of symbols]

11 ... Coal hopper, 12 ... Ball mill, 13 ... Tank, 14 ... Plunger pump, 15 ... Service tank, 16 ... Twin screw pump, 17 ... Counterflow type double tube type pyrolysis reactor, 18 ... Inner tube part , 19 ... outer tube part, 20 ...
Heating space, 30: shaft furnace type reactor.

──────────────────────────────────────────────────続 き Continued on the front page (51) Int.Cl. ⁶ Identification number Agency reference number FI Technical indication location C10J 3/46 C10J 3/46 M 3/48 3/48 3/50 3/50 3/72 3 / 72 C J C10K 3/00 C10K 3/00 C10L 3/06 C10L 5/00 5/00 6958-4H 3/00 A

Claims (10)

[Claims] 1. A pyrolysis reactor for pyrolyzing a mixture of coal and a liquid carbon-containing substance to obtain a light oil, a high calorie gas, and a pyrolysis residue, wherein the mixture flows from the inlet side to the outlet side. An inner pipe portion moving toward the inner pipe portion, a heating space is provided so as to surround an outer periphery of the inner pipe portion, and a heating space in which a heating gas flows from an outlet side to an inlet side of the inner pipe portion between the inner pipe portion. A pyrolysis reactor, comprising: 2. The thermal decomposition reactor according to claim 1, wherein the inner diameter of the outlet end of the inner pipe is larger than the inner diameter of the inlet end of the inner pipe. 3. The thermal decomposition reactor according to claim 1, wherein a large-diameter portion having an inner diameter larger than an inner diameter of an inlet-side end of the inner tube is formed at an outlet-side end of the inner tube. . 4. The thermal decomposition reactor according to claim 3, wherein a large diameter portion is formed in the inner pipe portion in a region of the heating space where the temperature of the mixture is equal to or higher than the resolidification temperature of the pitch in the mixture. 5. The thermal decomposition reactor according to claim 3, wherein the inner diameter of the large diameter portion is 110 to 200% of the inner diameter of the inlet end of the inner tube portion. 6. The thermal decomposition reaction according to claim 1, wherein an enlarged diameter portion whose inner diameter increases from an inlet side to an outlet side of the inner tube portion is formed at an outlet end of the inner tube portion. vessel. 7. The thermal decomposition reactor according to claim 6, wherein an enlarged diameter portion is formed in the inner pipe portion in a region of the heating space where the temperature of the mixture is equal to or higher than the re-solidification temperature of the pitch in the mixture. 8. The thermal decomposition reactor according to claim 6, wherein the maximum inner diameter of the enlarged diameter portion is 110 to 200% of the inner diameter of the inlet end of the inner pipe portion. 9. A reactor for partial oxidation and carbonization wherein a pyrolysis residue obtained by pyrolysis of a mixture of coal and a liquid carbon-containing substance is carbonized and partially oxidized to obtain a medium calorie gas and a solid fuel. A main body, a supply mechanism provided at an upper end of the main body for supplying the pyrolysis residue into the main body, and a discharge mechanism provided at a lower end of the main body for discharging the solid fuel. A partial oxidation and dry distillation reactor, comprising: an oxygen-containing gas supply means for supplying an oxygen-containing gas to a lower portion in the main body. 10. After pyrolyzing a mixture of coal and a liquid carbon-containing substance to obtain a light oil, a high calorie gas and a pyrolysis residue, the pyrolysis residue is subjected to dry distillation and partial oxidation to obtain a medium calorie gas and A solid fuel and fuel gas producing apparatus for obtaining a solid fuel, comprising: an inner pipe part in which the mixture moves from an inlet side to an outlet side thereof; and an inner pipe part provided around an outer periphery of the inner pipe part. A pyrolysis reactor having an outer tube defining a heating space in which a heating gas flows from the outlet side to the inlet side of the inner tube between the tube and the tube; and a hollow main body; and the main body. A supply mechanism provided at an upper end of the main body for supplying the pyrolysis residue into the main body, a discharge mechanism provided at a lower end of the main body for discharging the solid fuel, and a lower part in the main body. Supply oxygen-containing gas to Because of the oxygen-containing gas supply means and apparatus for producing a solid fuel and a fuel gas, characterized in that it comprises a reactor for partial oxidation and carbonization with.