KR101254977B1 - Apparatus and Method for Treating Coke Oven Gas - Google Patents

Abstract

The present invention relates to a COG treatment apparatus and method for treating the COG generated during the coal distillation in the carbonization chamber of the coke oven to improve the reusability.
The COG treatment apparatus of the present invention, as an example of the configuration, the first COG processing unit connected to the upstream pipe downstream of the coke oven carbonization chamber COG is generated; And a second COG processing unit connected to the riser, wherein the first and second COG processing units may be configured to process COG while being selectively operated based on the carbonization chamber temperature.
According to the present invention, in consideration of the generation characteristics such as components and tar content distribution according to the temperature of the carbonization chamber, the fuel of the H ₂ / CO-rich gas and the heating furnace utilized from the COG to the blast furnace or the flow flue gas at low cost The high efficiency CH ₄ -rich gas can be separated and collected, and in particular, the sensible heat recovery from the high temperature COG can be achieved, and ultimately, the COG recyclability can be improved.

Description

Apparatus and Method for Treating Coke Oven Gas}

The present invention relates to a coke oven gas treatment apparatus and method generated upon coal drying in a carbonization chamber of a coke oven.

More specifically, the present invention, in consideration of the generation characteristics such as components and tar content distribution according to the temperature of the coke oven carbonization chamber, from the coke oven gas (hereinafter referred to as 'COG') at low cost (B) gas containing a large amount of hydrogen / carbon monoxide (hereinafter referred to as 'H ₂ / CO-rich gas') used as a flue gas and a large amount of methane (referred to as 'CH ₄ -rich') Gas'), and particularly to a COG treatment apparatus and method that enables effective sensible heat recovery from high temperature COG, thereby ultimately increasing COG reusability.

The coke oven having a large number of carbonization chambers is charged with coal using a charging car, and then the outside air is blocked and heated for 19 hours at a temperature of about 1240 ° C. or more, thereby removing the grayish coke from which volatile matters contained in coal are removed. It is a kind of coal distillation work. And, after the drying operation, the coke is discharged from the carbonization chamber using an extruder, and is transferred to a digestion tower for extinguishing.

On the other hand, although not shown in a separate drawing, the COG is generated by the thermal decomposition during the drying of the coal charged in the carbonization chamber, such COG is purified through the riser disposed above each carbonization chamber (Hwaseong plant) Will be sent to.

However, the rising pipe is sprayed with high pressure ordination to remove the smooth flow of COG and dust and backflow of the gas, or to remove the tar (also referred to as tar mist in the form of fine droplets) contained in the COG.

Therefore, since the maximum combustion temperature of the carbonization chamber is 1200 ° C. or more, the COG discharged from the carbonization chamber at a high temperature drops to 80-90 ° C. while passing through the ordinal injection zone of the riser.

That is, the COG temperature immediately after occurrence in the carbonization chamber is 700 to 1100 ° C., which contains a lot of sensible heat as a high temperature state, but removes tar while going through the high pressure ordination injection zone in the riser. Due to the COG temperature is lowered to 80 ~ 90 ℃.

As a result, in the present form of COG treatment, cooling of COG by ordination is accompanied, so that sensible heat recovery contained in COG is difficult. Only COG is used as combustion energy (fuel) of the furnace.

On the other hand, many studies have been made on the reduction of carbon dioxide (CO ₂ ), which is a major cause of global warming, at home and abroad, and because the coke process generates a large amount of COG or dust, it is highly interested in its treatment. There is a high interest in the removal of CO2 as well as in particular COG recycling.

For example, as shown in Table 1 below, it can be seen that COG, which is a combustible mixed gas generated during coke production, mainly contains hydrogen (H ₂ ), methane (CH ₄ ) _{, and} carbon monoxide (CO) in a large amount.

COG Ingredients ingredient Fraction (%) H ₂ 50-60 CH ₄ 20 to 30 CO 5 to 15 CO ₂ 0 to 5 CnHm 0 to 5 N ₂ 0 to 5 O ₂ 0 to 0.5

However, in order to achieve a low carbon steelmaking process in a steel mill, hydrogen (H ₂ ), carbon monoxide (CO), and the like are blown into the blast furnace or (Finex process) flow furnace.

However, as can be seen in Table 1, COG contains a large amount of hydrogen or carbon monoxide, and does not require a separate high purity COG purification process for blowing the blast furnace or the fluidized furnace, but such COG inhibits the reduction reaction or the reducing agent. Nitrogen (N ₂ ), methane (CH ₄ ), which do not play a direct role in the furnace, and tar, which causes a big problem in the gas transfer line, should be preceded.

Therefore, in order to blow hydrogen or carbon monoxide into the blast furnace or the flow furnace, it is necessary to remove the problematic components, so it is important to enable blast furnace and flow furnace gas injection at a low cost.

Of course, COG is currently being processed through a refining plant to contain methane, and to be reused as fuel gas as a renewable energy source in a furnace.

On the other hand, a related art for recovering the sensible heat of COG generated when coal is dried in the carbonization chamber of the coke oven is disclosed in Japanese Patent Laid-Open No. 59-44346 or Japanese Patent Laid-Open No. 58-76487, for example, a carbonization chamber. The heat pipe is installed in the riser, and the heat medium is circulated in the heat pipe to recover the sensible heat.

However, in this case, if the temperature of the riser changes suddenly with the operation, the temperature of the circulating heat medium rises more than the boiling point, and the circulation system may be ruptured. Had a poor problem.

In addition, since a large number of carbonization chambers and rising tubes are provided in each carbonization chamber in one coke oven, the installation cost of installing heat transfer tubes in each of the rising tubes increases considerably, and in particular, tar, carbon, etc. contained in the COG are inside the rising tubes. And since it adheres and grows in a heat exchanger tube, it reduces the sensible heat recovery ability very much.

In addition, since the purification process (chemical conversion process) for the existing COG treatment is purified through primary cooling, electrostatic precipitating, secondary cooling, and multistage scrubber stages, hydrogen is separated from the COG only after compression and cooling. There is a significant problem in the cost of hydrogen separation, and the amount of hydrogen separated is not enough.

Accordingly, the applicant of the present invention, in consideration of the COG generation characteristics that the tar content is rapidly reduced when the carbonization chamber temperature (temperature near the coal bed) is higher than the set temperature, by diversifying the COG treatment line economical and recovery of blood count The present invention has been proposed to increase the collection efficiency of H ₂ / CO-rich gas or CH ₄ -rich gas and ultimately improve COG recyclability.

The present invention has been proposed in order to solve the conventional problems as described above, the object of the present invention, in consideration of the generation characteristics such as components and tar content distribution according to the temperature of the carbonization chamber, utilized from COG to blast furnace or flow furnace blow gas at low cost It enables the separate collection of the H ₂ / CO-rich gas and the high-efficiency CH ₄ -rich gas used as fuel for the furnace, and in particular enables the recovery of sensible heat from the high temperature COG, ultimately reducing the COG reusability. It is to provide an improved COG treatment apparatus and method.

As one technical aspect for achieving the above object, the present invention, the first COG processing unit is connected to the downstream side of the riser of the coke oven carbonization chamber COG is generated; And

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A second COG processor associated with the riser;

It is configured to include, wherein the first and second COG processing unit provides a COG processing apparatus configured to process the COG while being selectively operated based on the carbonization chamber temperature.
Preferably, the second COG treatment unit is connected to an upstream side of the riser 30 to enable at least sensible heat recovery of sensible heat recovery and H ₂ / CO-rich gas collection, or to collect H ₂ / CO-rich gas. It is connected to the downstream side of the riser as much as possible.

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Next, the present invention as another technical aspect, the first COG treatment step of detecting the carbonization chamber temperature of the coke oven to collect the COG downstream of the ordinal spray downstream of the riser if the set temperature; And

When senses the carbonization chamber temperature of the coke oven is higher than the preset temperature at least of the uprising pipe for ordination injected upstream or downstream to collect COG sensible heat recovery and H ₂ / CO-rich gas collected by the COG H ₂ / CO-rich A second COG treatment step of collecting and processing gases;

Provides a COG treatment method configured to include.

Preferably, in the second COG treatment step, the temperature of the carbonization chamber of the coke oven is sensed and when the temperature is higher than the set temperature, the COG is collected upstream of the ordinal spray of the riser to recover sensible heat from the high temperature COG and H ₂ / CO-rich. To recover at least sensible heat during gas collection.

According to the present invention as described above, it is possible to effectively and economically implement sensible heat recovery and H ₂ / CO-rich gas contained in the COG, and to increase the COG reusability to improve the competitiveness of the steel industry.

In other words, it is possible to reduce the amount of coke by injecting the reducing gas into the blast furnace or the flow furnace of the steelmaking process to reduce the carbon dioxide which is a major factor of global warming.

In addition, it is possible to separate the gas having a high calorific value, which makes it possible to reuse it for various uses for liquefied gas (LNG) replacement.

1 is a block diagram showing the overall configuration of the carbonization chamber and the riser of the coke oven COG is generated and the COG treatment apparatus of the present invention,
2 is a process chart showing a COG treatment step of the present invention,
3 is a graph showing the flow rate of the major components contained in the COG according to the carbonization chamber temperature and the drying time,
4 is a graph showing the tar generation amount according to the carbonization chamber temperature and the drying time.

Hereinafter, the present invention will be described in detail with reference to the accompanying drawings.

One embodiment of the COG treatment apparatus and method of the present invention, by selectively operating (operating) the first and second COG treatment unit H ₂ / CO-rich gas and CH ₄ -among the COG generated in the carbonization chamber (10) to separate the rich gas.

In addition, according to another embodiment of the present invention, in consideration of the tar content relationship of COG according to the carbonization chamber temperature, the second COG processing unit 200 which is less likely to be attached to a line (pipe) or a valve of the COG processing unit may be provided. In this case, the COG sensible heat recovery rate is increased.

First, in FIG. 1, the first COG processing unit 100 and the second COG processing unit (described in detail below), which are associated with the riser 30 of the upper part of the carbonization chamber 10 of the coke oven 1 according to the present invention ( 200 is shown.

For example, as shown in FIG. 1, when coal is charged into the carbonization chamber of the coke oven 1, the gas is combusted in the combustion chamber and heat is applied, the coal charged into the carbonization chamber is carbonized, and at this time, by the pyrolysis action The generated COG is discharged through the rising pipe 30 provided at the upper portion of each carbonization chamber 10, and at this time, the purification process (through the curved pipe part 32 and the main collection pipe 34) is carried out to the rising pipe 30. Chemistry process).

On the other hand, in the curved portion 32 of the ascending pipe 30, when COG or dust blows to the main collection pipe, the flow (pressure application) is smoothed, and the backflow of the gas is also prevented, while it is included in the COG. In order to impregnate tar or dust, high pressure ordination is sprayed through a spray nozzle (not shown).

Therefore, since the temperature of COG generated in the carbonization chamber is 700 to 1000 ° C., it has a high sensible heat because it is a high temperature state, but because of spraying high pressure ordination for the above reason, the ordinal injection zone (curve part 32 downstream of the rising pipe) COG passing through) decreases the sensible heat recovery since the temperature drops to 80 ~ 90 ℃.

The COG treatment of the present invention allows the sensible heat to be recovered as much as possible from the high temperature COG by branching before passing through the ordinal spray zone using the second COG treatment unit 200 described in detail below.

On the other hand, as shown in Figure 1, the COG contains a large amount of tar (tar) generated during the coal distillation process, and thus the injected ordination contains a large amount of tar, so the collected ordination is decanted (ordination / tar) The tar is separated from the ordination through the specific gravity separator 50, the pumping tank 52, and the filter 54.

Next, FIG. 3 and FIG. 4 graphically show the relationship between the generation characteristics of COG according to the present invention and the carbonization chamber temperature of tar. In addition, Table 2 below shows numerical values. At this time, in the following description of the embodiment of the carbonization chamber temperature, since the temperature deviation may occur depending on the measurement position (point), although not shown in a separate drawing, the position of the coal bed (coal bed) in which coal is placed in the carbonization chamber It means the measured temperature at. In the following description, however, the temperature is referred to collectively as carbonization chamber temperature.

For example, as can be seen in Figure 3 and Table 2 below, in the carbon dry distillation ultra-second, the medium temperature of the carbonization chamber 10 is 900 ° C or less, in the medium to coal dust, water, tar, methane (CH ₄ ), hydrogen sulfide (H ₂ S) It can be seen that various components such as COG are contained in the COG. On the contrary, it can be seen that hydrogen (H ₂ ) and carbon monoxide (CO) are mainly included in a region where the temperature of the carbonization chamber 10 in the late dry distillation exceeds 900 ° C.

And, as shown in Figure 4, it can be seen that the tar content is rapidly reduced when the carbonization chamber temperature of late dry, exceeds 900 ℃.

For example, the numerical values of Table 2 related to FIGS. 3 and 4 may be obtained through the following examples.

(Example)

20 kg of coal with 8% water content and 90% carbon content was placed in a distillation unit, and the temperature of the carbonization chamber was raised to 1000 ° C. over 10 hours. .

Therefore, as shown in FIG. 3, the gas containing methane (CH ₄ ) is significantly generated at temperatures up to 9 hours of dry distillation in the early stages of dry distillation and 900 ℃ or less. In the above, it can be seen that hydrogen occupies most of COG.

In this case, when the gas generated after 9 hours (COG) collected and evaluated, the average concentration of the gas is hydrogen (H ₂ ) 70%, carbon monoxide (CO) 24%, carbon dioxide (CO ₂ ) 2%, methane (CH ₄ ) was 3%, wherein the temperature of the gas was found to be more than 900 ℃.

The flow rate of the collected gas was 40% of the total COG, and the average concentration of the collected gas before 9 hours was 54% for hydrogen, 6% for carbon monoxide, 4% for carbon dioxide, and 36% for methane (CH ₄ ). It was confirmed that the calorific value (average calorific value of the gas) is 4,675 Kcal / N㎥ 20% higher than the COG calorific value 3,875 Kcal / N㎥ obtained in the experiment.

(COG component according to carbonization chamber temperature) Carbonization chamber temperature below 900 ℃ Carbonization chamber temperature over 900 ℃ ingredient density(%) ingredient density(%) Hydrogen (H ₂ ) 54 Hydrogen (H ₂ ) 70 Carbon monoxide (CO) 6 Carbon monoxide (CO) 24 Carbon dioxide (CO ₂ ) 4 Carbon dioxide (CO ₂ ) 2 Methane (CH ₄ ) 36 Methane (CH ₄ ) 3 Calorific value 4,675 Kcal / N㎥ Calorific value 3,875 Kcal / N㎥

Therefore, in the present invention, the COG generation characteristics, that is, the carbonization chamber temperature of 900 ° C. or less, which is the dry distillation and medium periods, are treated with the COG using the first COG treatment unit 100 described in detail below, In the region above 900 ° C, the COG is treated through the second COG treatment unit 200 of the present invention to separate H ₂ / CO-rich gas, which can be used as sensible heat recovery and blast furnace and flow gas, at low cost. It is possible to collect.

On the other hand, in the present invention, preferably, the carbonization chamber set temperature for selectively operating the first and second COG processing units 100 and 200 during the COG treatment, for example, the carbonization chamber temperature range of the treatment unit selection is 700 to 1100 ° C, Preferably it is 900 degreeC.

That is, as shown in FIGS. 3, 4 and Table 2, the carbonization chamber reference (set) temperature for selecting and operating the first and second COG treatment units is most preferably 900 ° C, but the actual operating environment of the carbonization chamber and the quality of coal. Or considering the combustion conditions and the like based on the temperature range, it may be appropriately adjusted the set temperature in accordance with the operating conditions. However, when the temperature is outside the above range, that is, the carbonization chamber temperature is less than 700 ℃, the tar is contained in the COG in fact makes it difficult to recover the sensible heat of the present invention through heat exchange (piping), the second COG processing unit 200 of the present invention Is difficult to apply, and when the carbonization chamber temperature exceeds 1100 ° C., a problem of low effectiveness due to a small operation remaining time may occur.

Next, as shown in FIGS. 1 and 2, the first and second COG processing units 100 and 200 of the present invention selectively operating in consideration of the carbonization chamber temperature (drying time) and the like will be described in detail. Take a look.

However, the first COG processing unit 100 corresponds to the existing COG treatment process (chemical conversion process), but will be described in detail as it is a basic component of the present invention.

For example, as illustrated in FIGS. 1 and 2, the first and second COG processing units 100 and 200 of the present invention, which are selectively operated in consideration of the carbonization chamber temperature (drying time) and the like, may include the first COG processing unit 100. ) Is operated and the second COG processing unit 200 may be sequentially operated when the temperature is higher than the carbonization chamber set temperature.

In order to selectively operate the first and second COG processing units 100 and 200 as described above, in the COG processing apparatus of the present invention, first, as illustrated in FIGS. 1 and 2, the internal temperature of the carbonization chamber 10, for example, as described above. In order to measure the carbonization chamber temperature based on the call bed (coal bed), one or more temperature sensing means (S), that is, thermocouples (heat thermocouples) are installed around the call bed, such a thermocouple device control unit (C) (The position of the thermocouple, the temperature sensing means, also changes when the temperature of the carbonization chamber changes, of course).

At the same time, as shown in FIG. 2, a control valve V electrically connected to the apparatus control unit C in the first linking line L1 and the second linking line L2 of the second COG processing unit 200 which is connected to the carbonization chamber. (Distribution and open / close control valves) can be installed.

For example, in FIG. 2, a distributing control valve V is installed upstream of the rising pipe 30 and an upstream ordination spraying region, and an opening and closing control valve is disposed in the second linking line L2 of the second COG processing unit 200. When V) is installed, branch supply to the first COG processing unit 100 or the second COG processing unit 200 may be controlled through the device control unit of the control valves.

Of course, such an arrangement of the control valve (V) can of course be adjusted appropriately.

Therefore, when the temperature of the thermocouple, which is the temperature sensing means S, is sensed based on the call bed point of the carbonization chamber and transmitted to the device control unit C, the device control unit is higher or lower than the previously set temperature. The COG is supplied to the first COG processing unit or the second COG processing unit through branching and opening and closing of the control valve V.

In this case, as shown in FIGS. 1 and 2, the first COG processing unit 100 (existing) which processes the COG downstream of the carbonization chamber rising pipe 30, that is, the high pressure water spraying zone is processed. It is associated with the first linkage line (L1) of the pipes connected to the downstream pipe, the first linkage line (L1) associated with each carbonization chamber riser is linked to the collection tank 102 to collect the COG.

Similarly, the second linkage line L2 (L2 ') associated with the second COG processing unit 200 is connected upstream or downstream of each carbonization chamber riser, for example, upstream or downstream of the ordinal spray zone. In addition, these second link lines are also connected to the collection tank 202 associated with the second COG processing unit 200 to collect and process the COG.

In this case, in FIG. 1 and 2, L2 is a second linkage line upstream of the ordination spray zone, and L2 'represents a second linkage line downstream of the ordination spray zone.

That is, since the second COG processing unit 200 associated with the second linking line is basically a case where the carbonization chamber temperature is higher than 900 ° C. in Table 2, since the COG temperature is mainly high, it contains H ₂ / CO-rich gas. In the case of sensible heat recovery, the second connecting line of the upstream L2 is connected before the ordination injection zone, but when collecting only H ₂ / CO-rich gas, COG may pass through the ordination injection zone. It is also possible to link to the second linking line (downstream of the rising pipe) of L2 '.

Therefore, the second COG processing unit 200 of the present invention, the second linkage line of L2 in consideration of sensible heat recovery and H ₂ / CO-rich gas collection and the second linkage of L2 'in consideration of H ₂ / CO-rich gas collection. It can consist of lines. However, in the present embodiment, a description will be given mainly on the second link line of L2.

Also, in the case of the second linkage line of L2 'in FIG. 2, a separate control valve is not specifically illustrated, but appropriate control valves for implementing a COG supply line may be arranged.

Meanwhile, in FIG. 2, the link line of L3 is a line connected to the tar processing unit 50 described above. Therefore, of the first and second link lines of the COG processing apparatus of the present invention, the known open / close control valve V, which is operated based on the electrical control through the device control unit of the second link line, is closed, and the upstream distribution control. The operation of the valve (V) COG is supplied to the first linkage line, on the contrary, the on-off valve is opened and the bonsai control valve is operated so that the COG can be branched to the second linkage line.

However, it should be appreciated that the selective distribution supply of the first and second link lines L1, L2, and L2 'of the COG is not limited to FIGS.

Next, as shown in FIG. 1 and FIG. 2, the first COG processing unit 100 of the COG processing apparatus of the present invention is connected to the downstream side of the ordination injection region (curved pipe portion 32) of the carbonization chamber riser. Primary cooler (tower) 110, electric dust collector 120, gas blower 130, secondary cooler (tower) 140, hydrogen sulfide (H) sequentially connected to the first linkage line (L1) ₂ S) and ammonium (NH ₃ ), and first to third scrubbers (SCRUBBER) 150, 160, 170 to remove tar-based by-products (BTX), and COG holders to collect and store the final COG ( 180).

Therefore, the first COG processing unit 100 of the present invention may correspond to the existing COG processing process, and because the processing of the COG through the ordinal spray zone, that is, the COG is lowered temperature, the amount of sensible heat recovery is small.

As described above, since the first COG processing unit 100 of the present invention processes the COG generated during the dry and early drying periods in the carbonization chamber having a carbonization chamber temperature lower than 900 ° C, as shown in FIG. 4. Since tar, dust sulfur hydrogen, etc. are contained in COG and tar adheres to piping and facilities, it is difficult to use a heat exchanger like the 2nd COG treatment part 200 of this invention.

However, as can be seen in FIGS. 1,2 and Table 2 above, in the case of the final COG passed through the first COG treatment unit 100, the temperature of the COG itself is low through the ordination zone, but a large amount of CH ₄ − Since rich gas is contained and the calorific value is high as 4,675 Kcal / Nm 3, there is no problem in reusing the combustion gas in the furnace.

Thus, COG subjected to claim 1 COG processing unit 100 of the present invention can be recycled by itself because the temperature of the sensible heat recovered amount is low but ever contained a large volume of CH ₄ -rich gas, the combustion energy.

Next, as shown in FIGS. 1 and 2, the second COG processing unit 200 according to the present invention is connected to an upstream side of the carbonization chamber riser 30, that is, an upstream side of the ordination injection region and a control valve ( It includes a heat exchanger 210 connected to the second linkage line (L2) is installed V).

On the other hand, in the case of the second COG processing unit 200 of the present invention, the COG is supplied only when the on-off valve V is opened in conjunction with the device control unit, so that the carbonization chamber temperature is set at a set temperature, for example, 900, during the dry time. When it exceeds ℃, as shown in Figure 4, since the tar content is rapidly reduced, it is possible to recover the sensible heat in the state of high COG itself without passing through the ordination injection zone using the heat exchanger 210, in this case sensible heat recovery Efficiency is maximized.

Next, more preferably, as shown in Figures 1 and 2, the heat exchanger 210 is connected to the collection tank 202 second linkage lines (L2) connected to the upstream side of each carbonization chamber riser And collect a large amount of COG in the second COG processing unit. The second COG processing unit 200 includes a purification tank (tower) 220 and a gas blower 230 for removing the impurities or other unnecessary components of the COG gas associated with the heat exchanger 210, and finally processed. It may further include a COG holder 240 for collecting and storing the COG.

On the other hand, as shown in Table 2 above, since the COG treated through the second COG treatment unit 200 of the present invention as described above contains 70% hydrogen and 24% carbon monoxide, the treated COG contains a large amount of H _2. Contains / CO-rich gas.

Therefore, the second COG processing unit 200 of the present invention can be collected separately from the COG as a gas containing a large amount of hydrogen that can be provided as the blowing gas of the blast furnace or the flow path.

Of course, as described above, when only the collection of the H ₂ / CO-rich gas is taken into consideration, it is possible to process not only on the upstream side of the ordinal injection zone but also on the downstream side.

On the other hand, in order to separate the high purity of the hydrogen, it may further include a water gas (WGS) reactor 250 connected to the upstream side of the heat exchanger (210) (indicated by a dotted line).

At this time, as shown in FIG. 2, the first and second COG treatment units of the present invention are sequentially operated according to the carbonization chamber temperature, and the heat exchanger 210 is operated by the electrostatic precipitator of the first COG treatment unit 100. 120 to recover the sensible heat from the high temperature COG first, and then, as described above in the first COG processing unit 100, the CH ₄ -rich gas having excellent calorific value as the combustion gas of the heating furnace. Treatment with COG included is also possible.

Therefore, in this case, since the first and second COG treatments are performed in parallel, the COG can be treated for various purposes, which is preferable.

On the other hand, although schematically shown in the drawings, since the heat exchanger 210 of the second COG processing unit 200 has substantially no tar content in COG, there is no problem of tar sticking and the like. Heat exchangers may optionally be used.

On the other hand, it is also possible to amplify hydrogen using the high temperature H ₂ / CO-rich gas separated by the COG treatment of the present invention.

For example, a high-pressure reducing gas is introduced into a CO reactor (shift reactor), amplified hydrogen, and recovered sensible heat of the gas, as shown in Equation 1 below. High purity hydrogen can be obtained from

[Equation 1]

CO + H ₂ O → H ₂ + CO ₂

Next, as shown in Equation 2 below, the CH ₄ -rich gas passed through the first COG processing unit 100 may be prepared as hydrogen through a reforming reaction.

&Quot; (2) "

CH ₄ + H ₂ O → CO + 3H ₂

CH ₄ + CO ₂ → 2CO + 2H ₂

CH4 + 1 / 2O ₂ → CO + 2H ₂

Accordingly, using the COG treatment apparatus and method of the present invention, when the carbonization chamber is lower than the set temperature of the carbonization chamber, that is, approximately 700 to 1100 ° C, preferably 900 ° C, the first COG treatment line is used. However, since COG itself temperature is low due to ordinal injection, but the methane gas contains a large amount of combustion calorific value, it is used as a combustion energy source. It is possible to increase the recovery rate of sensible heat in the heat exchanger and to collect only H ₂ / CO-rich gas with high hydrogen and carbon monoxide content in the blast furnace and flow furnace, or H ₂ / CO-rich gas regardless of sensible heat. .

As a result, the present invention enables optimum multi-stage treatment of COG in consideration of COG components, generation characteristics or tar content, and is capable of separating and collecting all possible recycling elements, thereby reusing the COG generated in a large amount in the coke process step. To maximize.

While the invention has been shown and described in connection with specific embodiments so far, it will be appreciated that the invention can be varied and modified without departing from the spirit or scope of the invention as set forth in the claims below. It will be appreciated that those skilled in the art can easily know.

1 .... coke oven 10 .... carbonization chamber
30 .... riser 50 .... tar treatment
100 .... First COG treatment unit 102,202 .... Collector
110,140..Cooler 120 .... Dust Collector
150,160,170 .... Screwer 180,240 .... COG Holder
200 .. 2nd COG treatment part 210 .... heat exchanger
220 .... Refinery 250 .... Water Gas (WGS) Reactor
L1, L2 .... 1st, 2nd connection line S .... Temperature sensing means
V ... control valve

Claims (17)

delete A first COG processing unit connected to a downstream side of a rising pipe of the coke oven carbonization chamber in which COG is generated; And
A second COG processor associated with the riser;
, ≪ / RTI >
And the first and second COG processing units are configured to process the COG while being selectively operated based on the carbonization chamber temperature. The method of claim 2,
The second COG treatment unit is connected to an upstream side of the riser tube to enable at least sensible heat recovery of sensible heat recovery and H ₂ / CO-rich gas collection, or a downstream side of the riser tube to enable H ₂ / CO-rich gas collection. COG processing apparatus, characterized in that connected to. The method of claim 3,
The carbonization chamber is provided with one or more temperature sensing means associated with the apparatus control unit, and one or more control valves provided in the linking line connected between the carbonization chamber and the first and second COG processing units are connected to the apparatus control unit to control the temperature of the carbonization chamber. Accordingly, the COG is supplied to the first or second COG processing unit. The method of claim 2,
The first COG processing unit includes one or more coolers, dust collectors, one or more screwers, and a COG holder associated with a first linking line connected to a downstream side of an ordinal spray zone of the carbonization chamber riser, and a large amount of COG holders in the COG. COG processing apparatus, characterized in that configured to collect CH ₄ -rich gas. The method of claim 3,
And the second COG processing unit is configured to recover the sensible heat of the high temperature COG, including a heat exchanger provided in a second linking line connected to an upstream side of the ordinal spray zone of the carbonization chamber riser. The method according to claim 6,
COG treatment, characterized in that configured to further collect a large amount of H ₂ / CO-rich gas from the COG further comprising a refinery, a gas blower and a COG holder connected to the heat exchanger provided in the second linkage line of the second COG processing unit. Device. The method of claim 3,
The second COG processing unit includes a refinery and a gas blower and a COG holder connected to a second linking line connected to a downstream side of an ordinal injection zone of the carbonization chamber uppipe, thereby providing a large amount of H ₂ / CO-rich. COG processing apparatus, characterized in that configured to collect the gas. The method according to claim 6,
And the heat exchanger further processes the sensible heat recovered COG in a first COG processing unit in connection with a dust collector provided in the first COG processing unit. The method of claim 2,
The carbonization chamber temperature, which is a reference for selectively operating the first and second COG treatment units, is 700 to 1100 ° C. The method of claim 10,
The temperature of the carbonization chamber is a temperature near a coal bed of the carbonization chamber, characterized in that 900 ℃. A first COG treatment step of detecting a carbonization chamber temperature of the coke oven and collecting COG at a downstream side of the ordinal injection of the riser when the temperature is lower than the set temperature; And
When senses the carbonization chamber temperature of the coke oven is higher than the preset temperature at least of the uprising pipe for ordination injected upstream or downstream to collect COG sensible heat recovery and H ₂ / CO-rich gas collected by the COG H ₂ / CO-rich A second COG treatment step of collecting and processing gases;
COG processing method configured to include. The method of claim 12,
In the second COG treatment step, when the temperature of the carbonization chamber of the coke oven is sensed and higher than the set temperature, the COG is collected upstream of the ordinal spray of the riser, thereby recovering sensible heat from the hot COG and collecting H ₂ / CO-rich gas. COG treatment method characterized by recovering sensible heat. The method according to claim 12 or 13,
The carbonization chamber set temperature is 700 ~ 1100 ℃, the set temperature is COG processing method characterized in that the real-time sensing through the temperature sensing means provided in the carbonization chamber. The method according to claim 12 or 13,
In the first COG treatment step, the COG is cooled, the impurities removed through the scrubbers, the final COG treatment method characterized in that it comprises a large amount of CH ₄ -rich gas. The method of claim 13,
In the second COG treatment step, the sensible heat is recovered from the high temperature COG collected before passing through the ascending ordinal injection zone through a heat exchanger, and then, the COG treated through the purification step contains a large amount of H ₂ / CO-rich gas. COG treatment method characterized in that it is included. 17. The method of claim 16,
In the second COG processing step, the heat exchanger in conjunction with the first COG processing step, the COG treatment method characterized in that the sensible heat recovery COG in the first COG processing step.

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