JP3239712B2 - Heavy oil reforming method - Google Patents

Description

DETAILED DESCRIPTION OF THE INVENTION

[0001]

BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a method for reforming heavy oil, which makes it possible to improve the quality of heavy oil and, consequently, its economic efficiency. Heavy oil here means coal-based or petroleum-based heavy oil,
More specifically, it includes coke oven generated tar, heavy oil generated by a coal liquefaction, heavy oil in crude oil, heavy oil generated during petroleum naphtha cracking, and the like. In addition,
In the following, coke oven generated tar is a representative example of heavy oil,
That is, the present invention will be described using coal tar as an example.

[0002] Further, the present invention relates to secondary treatment of coke extracted from a coke oven, which makes it possible to improve the quality of coke and, consequently, to improve the economic efficiency of the coke oven.

[0003]

2. Description of the Related Art In a coke oven type coke oven, a coking chamber for carbonizing coal and a combustion chamber for supplying heat to the coking chamber are alternately arranged in a sandwich shape. The height is, for example, about 6 to 7 m, the length is about 15 to 17 m, and the width is about 0.45 m. In such a coke oven, for example, 20 to 40 tons of raw coal is charged into the coking chamber at one time, fired to about 1000 ° C. with a carbonization time of about 24 hours, and discharged from the coke oven. The red hot coke discharged from the coke oven is then extinguished and cooled by wet cooling with water spray or dry cooling with an inert gas.

On the other hand, during the period from the coal charging to the discharge, gas, light oil, tar, water, and the like are generated in the coking chamber, and after these are extracted from the coking chamber through the riser at the top of the furnace, they are respectively discharged. Separated and collected.

[0005] In such a coke oven, the carbonization temperature of the coke usually reaches about 1000 ° C as described above. This is because the quality of coke largely depends on the carbonization temperature, and the higher the carbonization temperature, the better the quality. In order to obtain the coke quality required by the current ordinary large blast furnace, a carbonization temperature of about 1000 ° C. is required. On the other hand, from the viewpoint of economy, the lower the carbonization temperature, the smaller the amount of heat input to the coke oven.
However, there is, of course, a lower limit of the carbonization temperature, and the temperature is determined depending on whether or not the coke cake can be extruded from the coke oven. In other words, the coke cake gradually tightens as the carbonization temperature rises,
As the strength is improved and the whole cake shrinks, the extruding and discharging from the coke oven becomes easier as the carbonization temperature increases. Although the absolute value differs slightly for each coke oven, it is generally difficult to discharge the coke cake when the temperature in the coal is lower than 700 ° C. Therefore, from the viewpoint of the extrudability of coke, the carbonization temperature is the
In other words, it should be about 700 ° C or more. But,
As already mentioned, a decrease in the carbonization temperature inevitably leads to a corresponding decrease in coke quality.

[0006] On the other hand, during the production of coke, liquid tar is formed as a by-product, and this amount is generally about several percent of the charged coal. However, in the case of coke for iron making, for example, the production volume is enormous (for example, the annual production volume in Japan is 40 to 50 million tons), and the production volume of tar also reaches a considerable scale.

Moreover, tar has a content of about 50% of heavy components such as pitch, and also contains a considerable amount of nitrogen, sulfur and the like, so that its properties are not very preferable. For this reason, this tar has not been said to be used effectively with sufficient economic value in the past.

[0008]

In order to use low-temperature carbonized coke produced at a reduced carbonization temperature in a blast furnace, it is essential to improve the quality and make up for it. There are several ways to improve coke quality. For example, a method for improving the quality of coal, which is a raw material for production, can be considered. It is also effective to secondarily reheat the low-temperature carbonized coke, but it is difficult to expect a significant improvement in quality by this method.

On the other hand, there is an example in which pyrolytic carbon is adhered to the surface of coke to improve coke quality. This method may achieve a significant improvement in coke quality, but coke dry fire (CDQ)
When carrying out this pyrolytic carbon deposition method using such methods, it is important that the pyrolytic carbon material to be added does not adversely affect the operation of CDQ. That is, for example, when a liquid material such as a coke oven tar is used as a raw material of pyrolytic carbon in this method, it is not easy to cause the raw material to react 100%, and generally, a part of the added raw material is converted as an unreacted material. Will remain. This unreacted material accompanies the flow of the circulating gas for heat exchange, and is cooled when heat is exchanged in the boiler section, and as a result, precipitates and accumulates on the surface of the boiler tube, etc.
Eventually, troubles such as a rise in pressure or poor heat exchange may be caused.

[0010] Incidentally, the coke oven tar is an organic mixture composed of a large number of components, and its main component is considered to be various aromatic compounds. Typical examples thereof include naphthalene, methylnaphthalene, phenol, cresol and quinoline. These components are generally separated and purified by a distillation operation or the like to obtain respective products. However, the proportion of these components contained in tar is at most about 10-30%, and conversely 70-90% of tar is still not fully utilized in terms of its effective utilization. I can not say.

For the purpose of effectively utilizing these ineffective components, tar or a part thereof is treated with an oxidizing gas to convert the tar or aromatization thereof to a heavier one (JP-A-1-294793). Gazettes etc.) are conventionally seen.

[0012] On the other hand, the case where the tar is lightened to improve the product value thereof is naturally considered, but unfortunately, there is no example in which an economic process has been conventionally constructed. This is a typical technology for lightening because tar contains a large amount of distillation residues (aromatic heavy components such as pitch) in the tar, and there are not a few heteroelements such as N and S. The biggest cause is that hydrocracking cannot be applied here due to catalyst poisoning due to harmful components in tar.

In addition, in lightening based on the thermal decomposition reaction, unless a means for controlling the simultaneously occurring heavy reaction is taken skillfully, a polymer such as coke is accelerated by accelerating the heavy treatment (coking) reaction. Precipitation in the reactor or piping,
A device trouble typified by blockage or the like will be induced.

That is, since the thermal decomposition is basically a reaction in which the component A becomes two components B and B ', the decomposition and lightening of the raw material proceed. However, since this reaction itself is a radical reaction,
The generated radical B immediately causes a chain reaction, for example, a reaction such as C and C 'may occur, which lowers the molecular weight. On the contrary, a polymerization reaction such as BA occurs. Also occurs at a probability almost the same as that of the low-molecular-weight reaction. Therefore, if the pyrolysis reaction is continued for a long time, the product will be light components (gas) and heavy components.
(Coke). Therefore, in order to make the thermal decomposition reaction practical, the reaction progress (product distribution)
It is essential to control the temperature or to overcome the problems associated with the formation and precipitation of the polymer in terms of equipment and process.

Accordingly, an object of the present invention is to eliminate the disadvantages of the prior art, suppress the production of a polymer, and economically realize the reforming for the purpose of lightening heavy oil such as tar. To develop technical methods to

[0016]

Means for Solving the Problems The present inventors have conducted various studies on a method for lightening heavy oil such as tar, for example, and have achieved a remarkable effect economically and without causing any equipment trouble. The present inventors have found that it is effective to use a coke preheated to the reaction temperature in advance, for example, red hot coke discharged from a coke oven, and to contact the heavy oil to be reformed for a short time, and completed the present invention.

Further, the present inventors have conducted various studies on the secondary treatment of the red hot coke extracted from the coke oven. If the reheating treatment is performed in combination with the above-described heavy oil reforming method, it is economical and economical. The inventor of the present invention has realized that a remarkable effect of improving the coke quality can be exerted without causing any equipment trouble.

That is, the gist of the present invention is as follows.
In the following points. (1) Coke removed from the coke oven and coke preheated to the reaction temperature is charged from the inlet of the reactor, and continuously withdrawn from the outlet of the reactor, while the heavy oil to be reformed is treated with the heavy oil. After continuously supplying the coke from the inlet of the reactor and contacting the coke, a high-temperature fluid mainly composed of heavy oil is extracted from the reactor and recovered in a flow different from the coke discharge flow. Quality oil reforming method.

(2) The coke has an average carbonization temperature of 900
℃ a red-hot coke from the chamber furnace-type coke oven to produce coke by dry distillation of coal in the following, the reactor is thermally decomposed
The heavy oil is composed of coke oven generated tar
Wherein the high-temperature fluid is cooled and separated into gas, light oil and unreacted tar (1).
The described method.

(3) The red-hot coke taken out of the pyrolysis zone is introduced into the heating zone and heated to a temperature higher than the average carbonization temperature, and the heated coke is discharged from the heating zone and cooled. (2) The method described.

[0021]

Next, an embodiment of the present invention will be described in more detail with reference to the drawings. FIG. 1 shows a reaction system diagram for carrying out the reforming method according to the present invention,
In this example, the present invention is described using tar as a heavy oil.

In the figure, coke 12 discharged from a coke oven (not shown) is continuously or intermittently charged into a reaction tower 10 constituting a reactor. At this time, a carrier gas 14 containing nitrogen or hydrogen as a main component is simultaneously introduced into the reaction tower 10 for adjusting the atmosphere and controlling the reaction time of tar. When these objects are achieved by the gas generated in the reaction tower 10, it is not necessary to introduce a carrier gas from the outside. The temperature of the coke 12 is not limited as long as the tar thermal decomposition reaction actively occurs, but is preferably 750 ° C. or more. In this case, of course, although not limited, it is desirable from the viewpoint of thermal efficiency that the red-hot coke immediately after being discharged from the coke oven is directly introduced into the reaction tower 10.

On the other hand, the tar 22 stored in the tar storage tank 20
Is continuously supplied to the reaction tower 10 through the liquid sending pump 24. In this case, the inside of the reaction tower is already filled with high-temperature coke, and most of the supplied tar 22 immediately undergoes a thermal decomposition reaction even if it comes into contact with these cokes 12 for a short time, for example. The structure in the reaction tower may be a coke packed bed structure as in a coke dry extinguishing system (CDQ), or may have a fluidized bed structure.

If the tar stays in the reaction system for a long time, both decomposition and polymerization reactions proceed extremely, which is not good. Under the reaction conditions in the present invention, such a decomposition reaction and a polymerization reaction are carried out for a short time so that the polymerization reaction does not excessively proceed, for example, the residence time of the tar 22 in the reaction tower 10 is within 1 minute, preferably within 10 seconds. The flow rate of the carrier gas is adjusted.

On the other hand, the supply amount of the tar 22 is not particularly limited. However, when no special heat source is provided other than the sensible heat of the high-temperature coke, the coke loading is performed in order to stably continue the reaction. It is preferable that the content is not more than 10 wt% with respect to the amount of input.

The high-temperature fluid 30 composed of the pyrolyzed tar and carrier gas is separated from the coke stream at the lower part of the reactor basically in the form of a side cut as shown in FIG.
Extract from 10. According to such a method, it is possible to efficiently separate solid coke and liquid tar without using a special separator or the like, and the economical efficiency of the process is greatly improved.

The high temperature fluid 30 extracted from the reaction tower 10
Tar through the coolers 32, 33 or the separators 34, 36
40 and gas 42. On the other hand, the coke 48 after the completion of the reaction is continuously extracted from the lower portion of the reaction tower, and then heat-exchanged and cooled by the cooler 50.

According to the method of the present invention, the thermal decomposition of tar can be stably continued for a long period of time, and the tar after the reaction is reformed into an oil mainly composed of light components, which has a low heavy content and a reduced amount of hetero elements. Is done.

[0029] Such excellent features of the present invention are brought about by finally interposing high-temperature coke in the reaction system through analysis of facts obtained through various trial and error. That is, in general, generation of heavy components (coke and the like) accompanying the polymerization reaction is inevitable in the thermal decomposition, but in the present invention, such a phenomenon peculiar to the thermal decomposition can be easily avoided. The reason for this is not clear, but it can also be inferred that coke functions as a polymerization terminator for radical polymerization in such a manner that the heavy material is trapped in, for example, its pores.

Accordingly, the coke used in the present invention is not particularly limited as long as it exerts such an effect, but preferably, the coke crushed to a particle size of 1 to 50 mm is used. In the present invention, coal tar reforming has been described, but the heavy oil to be treated according to the present invention also includes coal-based or petroleum-based heavy oil having substantially the same composition as coal tar, It should be understood that these modifications are equally applicable.

Next, the method for reforming heavy oil according to the present invention is implemented in combination with a coke oven to improve not only heavy oil such as tar but also low-temperature carbonized coke. Possible embodiments will be described.

In this embodiment, the present invention is carried out in accordance with a flow chart as shown in FIG. That is, coke carbonized at an average carbonization temperature not exceeding 900 ° C. in a coke oven is introduced together with tar and carrier gas into a pyrolysis zone at a temperature substantially equal to the coke temperature.

Here, the carbonization temperature of coke is 900
If the temperature is higher than ℃, the effect of the low-temperature kiln release (shortening of the carbonization time and reduction of the heat of carbonization) with respect to the normal high-temperature carbonization (about 1000 ° C) is not clear, which is not preferable.

On the other hand, tar is simultaneously supplied to the thermal decomposition zone. Here, a thermal decomposition reaction of the tar occurs, and the reforming of tar and the reforming of coke proceed simultaneously. That is, part of the tar is converted into light oil by the reaction and reformed. Another part of the tar adheres to the coke as pyrolytic carbon and contributes to coke reforming.

It is effective to blow carrier gas to control these reactions. In other words, in pyrolysis, the reaction basically progresses to both poles of gas and heavy components,
In order to reform tar, that is, to decompose tar and convert it to light oil, it is necessary to avoid excessive reaction of thermal decomposition. For this purpose, shortening the residence time in the pyrolysis zone is one effective means. For example, the residence time of the added tar in the thermal decomposition zone is preferably controlled to within about 1 minute. Since the pyrolysis zone is at a high temperature, most of the added tar exists as a vapor phase. Therefore, it can be controlled independently of the moving (falling) speed of solid coke.If the flow rate of the interposed carrier gas is small, the residence time of the tar vapor in the pyrolysis zone is long, and if the flow rate of the carrier gas is increased, Tar residence time is reduced. Although not essential in the method of the present invention, it is preferable to provide a coke supply tank in front of the thermal decomposition zone because the supply speed of coke to the thermal decomposition zone is stabilized.

The tar vapor phase reacted in the pyrolysis zone is separated from the coke stream at or at the exit of the pyrolysis zone, and after cooling, is separated into gas, light oil and tar fraction. The apparently unreacted tar fraction can, of course, be circulated and fed again to the pyrolysis zone. Similarly, the generated gas can be circulated for carrier gas or used as a heating source gas supplied to the heating zone.

On the other hand, coke discharged in different streams from the pyrolysis zone is then supplied to the heating zone. In this case, although not essential in the method of the present invention, if a coke receiving tank is provided between the thermal decomposition zone and the heating zone, the supply of coke to the heating zone is more preferably stabilized.

When coke is supplied to the heating zone, air, air and fuel gas or high-temperature combustion exhaust gas is supplied thereto, and the coke is heated and secondary-heated. Here, the secondary heating temperature is determined according to the desired coke quality. Incidentally, the secondary heating time is not particularly limited, but 10 minutes or more, preferably
If 30 minutes or more are secured, coke quality improvement will proceed sufficiently. It is also effective to use the pre-chamber part of the coke dry fire extinguishing system (CDQ) which is already in practical use as this heating zone. This is because the coke after heating can be smoothly cooled and supplied as blast furnace coke by ordinary CDQ operation.

According to the above embodiment of the present invention, the secondary treatment of coke and tar is simultaneously achieved, the low-temperature carbonized coke is reformed to the same or higher quality as ordinary high-temperature carbonized coke, and the tar The pyrolysis can be stably continued for a long period of time, and as a result, the tar is reformed into an oil mainly composed of light components having a reduced amount of heavy components and a reduced amount of hetero elements.

That is, in the method of the present invention, heavy oil such as tar is thermally decomposed in the presence of coke, so that heavy components produced by the polymerization reaction react with or accompany the intervening coke to form a system. Removed with coke outside. Therefore, in the thermal decomposition reaction, the precipitation of the polymerization reaction product on the wall of the reaction tube, the wall of the piping, and the like, which are generally observed, can be avoided. Further, the quality of the coke to which the heavy component adheres is improved by a subsequent heat treatment, and when the coke exits the pyrolysis zone, it is separated from unreacted tar vapor. Can be easily avoided. Hereinafter, the present invention will be described in more detail with reference to Examples.

[0041]

【Example】

(Example 1) In this example, the present invention was carried out by the reaction system shown in FIG. Blast furnace coke produced from coal at a carbonization temperature of 1000 ° C is pulverized to a particle size of 5 to 10 mm and sized.The same shape is used in advance (inner diameter 10 cm, effective length 100 cm, vertical empty tower type, with external heat heater). After filling into the preheater and reactor of
The temperature of the internal coke is 900 ℃ while flowing nitrogen gas
Temperature.

When the temperature rose, coke extraction (4000 g / h) was started from the lower part of the reactor into a closed receiving tank. At this time, coke was supplied to the reactor from the preheater in response to withdrawal from the reactor, and at the same time, coke at room temperature was supplied to the preheater from a coke storage tank installed above the preheater. Under a predetermined nitrogen gas flow rate, 100 g / h while coke is continuously extracted and the temperature inside the reactor is stable
At a constant rate, the supply of tar having the properties shown in Table 1 to the reactor was started.

The reaction continued for 5 hours from this point. On the other hand, the gas and the tar high-temperature fluid after the thermal decomposition were side-cut from the lower part of the reactor, immediately cooled, and separated into a gas and a liquid (tar after the reaction). The gas was then flow-measured with a flow meter, and then a portion of the gas was analyzed by gas chromatography to calculate the tar gasification rate. On the other hand, the whole liquid was collected and recovered after the reaction, weighed, and then subjected to property analysis. Then, the difference between the total amount of gas and liquid (tar) determined here and the supply amount of the raw material was evaluated as a polymer (coke or the like) and displayed as a heavy component. Table 2 summarizes the results of these series of studies.

As can be seen from these results, by changing the nitrogen flow rate of the carrier gas, the tar reaction time was 3 to 82 seconds. Looking at the product yield when the reaction time is changed in this way, the yield distribution does not differ significantly when the reaction time is short, whereas when the reaction time is shorter than 82 seconds, It is considered that the yield of gas or coke sharply increased and excessive thermal decomposition reaction occurred. Therefore, it is desirable that the reaction time does not exceed 1 minute. The distribution of tar fractions at this time shows that the weight of the tar is significantly reduced as compared with that of the raw material tar. Here, focusing on the yield of the light oil having a boiling point of 200 ° C. or less, there is almost no change between the reaction times of 8 seconds and 56 seconds. From this point, it is considered that the reaction time of about 10 seconds or less is sufficient.

Further, the content ratio of the hetero element in the light oil obtained here is smaller than that of the raw material tar, and it can be seen that the light oil having good properties is obtained by the reaction.

Example 2 A tar thermal decomposition test was carried out in the same manner as in Example 1 except that the reaction time of tar was fixed at 3 seconds and the reaction temperature was variously changed. The results are summarized in Table 3. As is clear from the table, the reaction is inactive at a temperature of 700 ° C., and it is preferable to employ a temperature of 750 ° C. or higher in the method of the present invention.

Comparative Example 1 A tar pyrolysis test was performed in the same manner as in Example 1 except that an iron ball having a diameter of 8 mm was used instead of the sized coke for a blast furnace. As a result, the withdrawal of iron balls from the lower part of the reactor stagnated approximately three hours after the start of the tar supply, making it impossible to continue the operation. It is assumed that the polymerization reaction accompanying the thermal decomposition became remarkable in the reactor. Therefore, it can be understood that interposing coke in the reaction system as in the method of the present invention is very effective for stably continuing the thermal decomposition reaction.

Comparative Example 2 A tar thermal decomposition test was carried out in the same manner as in Example 1 except that coke extraction from the lower part of the reactor was stopped. As a result, after the start of tar supply,
At 0.4 h, the pressure in the reactor increased rapidly, and it became impossible to continue the operation. After cooling, the reactor was opened and inspected. As a result, it was found that the upper portion of the reactor was tightly closed due to polymerization of tar and coking.

Example 3 Instead of tar, petroleum heavy oil and coal liquefied heavy oil whose properties are shown in Table 4 were used.
A thermal decomposition experiment was performed in the same manner as in Example 1. In addition,
Here, the reaction time was fixed at 3 seconds. The results are shown in Table 5, and it can be seen that the lightening of petroleum and coal liquefied heavy oil proceeds favorably by the present method as in the case of tar.

[0050]

[Table 1]

[0051]

[Table 2]

[0052]

[Table 3]

[0053]

[Table 4]

[0054]

[Table 5]

Example 4 In this example, the present invention was carried out using the reaction system shown in FIG. First, using a coke oven with a height of 7 m that is actually used for coke production, the coke is discharged from the coke oven at an average carbonization temperature of 850 ° C. It was stored in a coke supply tank where it could be stored. This supply tank was installed in two tanks in parallel, and alternately supplied red hot coke to the pyrolysis zone.

The pyrolysis zone has an inner diameter of 2 m and a height of 3 m, into which red hot coke is continuously supplied at a constant rate of 200 t / h, and coke oven tar is fed at 4 t / h.
And the circulating gas for CDQ heat exchange 3500Nm ³ / h
It was supplied preheated to ° C.

After staying in the pyrolysis zone for about 2 seconds, the tar was extracted out of the system together with gas through a side cut pipe located 0.8 m from the lower part of the pyrolysis zone. The extracted fluid was immediately cooled and then separated into gas, light oil having a boiling point of 160 ° C or lower, and heavy oil having a boiling point of 160 ° C or higher (tar fraction).

On the other hand, coke was extracted from the lower part of the pyrolysis zone and stored in a coke receiving tank having the same shape as the supply tank. The coke that reached one kiln here was then fed into a coke dry fire extinguishing system (CDQ) with a coke throughput of 200 t / h in the usual way.

However, in this example, the upper pre-chamber section of the CDQ is used as a heating zone, and the pre-chamber is charged with red-hot low-temperature carbonized coke and simultaneously supplied with hot-air exhaust gas produced by burning the CDQ circulating gas. Here, the coke temperature was increased to 1000 ° C. The heated coke was then exchanged with circulating gas in a cooling zone by ordinary CDQ operation, cooled to 200 ° C or less, and taken out from the lower part of the CDQ as cold coke.

Although such a series of operations was performed continuously for 12 hours, no trouble occurred during the operation.
The cold coke discharged from the lower part of the CDQ was measured for cold coke strength (drum rotation strength) according to a conventional method. As a result, the drum strength was 85.5. For comparison, the strength of the coke that was carbonized in a coke oven at 1000 ° C or 850 ° C, immediately put into CDQ without passing through the pyrolysis zone or heating zone, and cooled was measured in the same way.The values were 83.0 and 78.3. Met.

Accordingly, it can be seen that the quality of low-temperature carbonized coke is greatly improved by the method of the present invention, and that coke having higher quality than ordinary high-temperature carbonized carbon can be produced. In addition, each product recovered from the pyrolysis zone contained 0.39 t / h gas, 0.56 t / h light oil, and 2.20 t / h heavy oil.
t / h. Further, when elemental analysis of the light oil was performed, heteroelements such as S and N were significantly reduced as compared with the original tar, and the quality was good.

Accordingly, it can be seen that a large amount of light oil with high added value (about 15 wt% -tar in this example) can be produced from tar by a simple method such as the method of the present invention. In addition, in the method of the present invention, since the low-temperature kiln is discharged, the productivity of the coke oven is improved by about 10%.

Example 5 An experiment was conducted in the same manner as in Example 4 except that the heating temperature of coke in the heating zone was set at 900 ° C. or 850 ° C. The coke strength at this time is
They were 83.6 and 82.1, respectively. That is, if the quality is equivalent to that of ordinary high-temperature carbonized coke, the heating temperature of the present invention is 90.
It turns out that about 0 ° C. is sufficient. However, if the temperature in the heating zone is not higher than the average carbonization temperature, the quality of coke cannot be said to be good, and it is understood that the treatment temperature here should be higher than the average carbonization temperature.

(Comparative Example 3) An experiment was conducted in the same manner as in Example 4 except that gas and tar vapor were not side-cut in the pyrolysis zone and were supplied to the heating zone together with coke. However, approximately 5.5 hours after the start of the experiment, the pressure near the outlet of the CDQ boiler began to rise significantly, and the experiment was stopped. In this area where the temperature dropped, it was interpreted as a problem caused by the condensation of tars.

(Comparative Example 4) Instead of red hot coke, 850
An experiment was carried out in the same manner as in Example 4 except that alumina spheres having a diameter of 4 cm preheated to ° C were supplied to the pyrolysis zone. However, 10 hours after the start of the experiment, it became difficult to extract the alumina spheres from the pyrolysis zone, and the experiment was stopped. Polymerization products due to tar pyrolysis precipitate inside the pyrolysis zone,
This was due to accumulation. That is, it can be understood that the intervention of coke is very effective for the thermal decomposition of tar as in the method of the present invention.

[0066]

According to the present invention, it is possible to improve the quality of heavy oil such as tar produced in a coke oven, thereby enabling the economical use of heavy oil. Also,
The present invention improves the quality of coke and tar produced in a coke oven, and further improves the economics of the coke oven.

[Brief description of the drawings]

FIG. 1 is a process chart showing an example for carrying out the present invention.

FIG. 2 is a process chart showing another example for carrying out the present invention.

──────────────────────────────────────────────────続 き Continued on the front page (58) Fields surveyed (Int. Cl. ⁷ , DB name) C10C 1/19 C10B 55/04 C10C 3/10 C10G 9/28 C10G 9/30

Claims (3)

(57) [Claims] 1. A coke taken out of a coke oven.
The coke preheated to the reaction temperature was charged from the inlet of the reactor and continuously withdrawn from the outlet of the reactor, while the heavy oil to be reformed was continuously supplied from the inlet of the reactor. A method for reforming heavy oil, comprising extracting a high-temperature fluid containing heavy oil as a main component from the reactor in a flow different from the coke discharge flow after contacting the coke with the coke. 2. The coke is red-hot coke from an indoor coke oven for producing coke by carbonizing coal at an average carbonization temperature of 900 ° C. or lower, wherein the reactor is constituted by a pyrolysis zone, The method according to claim 1, wherein the heavy oil is a coke oven generated tar, and the high-temperature fluid is separated into gas, light oil and unreacted tar while cooling. 3. The red-hot coke taken out of the pyrolysis zone is introduced into the heating zone and heated to a temperature higher than the average carbonization temperature, and the heated coke is discharged from the heating zone and cooled. 2. The method according to 2.