KR20140139686A - The method for the two-step recovering sensible heat of red-hot cokes using carbon dioxide - Google Patents

Abstract

The present invention relates to a two-stage method for recovering sensible heat of red-hot cokes using carbon dioxide and, more particularly, to a two-stage method for recovering sensible heat of red-hot cokes using carbon dioxide, comprising the steps of: inputting red-hot cokes into a pre-chamber at the upper part of the main body of a coke dry quenching (CDQ) facility; primarily cooling the red-hot cokes by supplying carbon dioxide to the pre-chamber having the red-hot cokes input therein to recover sensible heat via reaction with carbon dioxide; moving the primarily cooled red-hot cokes to a cooling chamber at the lower part of the main body of the CDQ; and a secondarily cooling the red-hot cokes by injecting carbon dioxide into the cooling chamber to recover sensible heat via the reaction of the red-hot cokes with the carbon dioxide. The present invention can recover sensible heat of red-hot cokes safely and effectively by supplying carbon dioxide to the red-hot cokes in each of the upper pre-chamber and the lower cooling chamber of the coke dry quenching facility to cool the red-hot cokes, and can separate only carbon monoxide generated from the chemical reaction of the red-hot cokes with the carbon dioxide to be recycled as raw material gas in a iron-manufacturing or chemical process.

Description

BACKGROUND OF THE INVENTION 1. Field of the Invention [0001] The present invention relates to a method for recovering two-stage sensible heat of coke by using carbon dioxide,

The present invention relates to a method for efficiently recovering the sensible heat of a glow-colored coke by two-step heat recovery reaction of a gaseous coke and carbon dioxide.

Generally, in order to produce a blast furnace coke in a steelmaking process, a blend is put into a coke oven and the blast furnace is dried at a temperature of 1,000 ° C or higher for about 20 hours. The hot coke is discharged and cooled, And as a reducing agent. In this coke manufacturing process, the hot coke of high temperature discharged after the carburization has a high temperature of 1,000 ° C or more, so a wet or dry cooling method is used for cooling the coke.

In this case, in the case of the wet cooling method, it is difficult to recover sensible heat at a high temperature, and there are environmental problems such as generation of a large amount of wastewater and dust, and a dry cooling method is generally used.

The dry cooling method utilizes a coke dry quenching (CDQ) system, which generally comprises a CDQ main body 1, as shown in Fig. That is, the CDQ main body 1 of the coke dry type fire extinguishing system receives high temperature coke from the coke bucket 2 through the winch lift 3, recovers the high heat through the dry digestion of the coke heat, And the coke discharged in the CDQ main body 1 is discharged to the coke discharging device 4.

In the conventional coke dry fire extinguishing system, hydrogen (H ₂ ), carbon monoxide (CO), and carbon dioxide (CO ₂ ) are removed by moisture and oxygen introduced from the outside in the process of dry digesting the gypsum coke in the CDQ body 1, Gas is generated.

If the concentration of the gas becomes high, the operation and control of the coke dry type fire extinguishing system become unstable. Therefore, it is necessary to burn and remove the combustion air, and the combustion air required for combustion is supplied to the combustion air supply And supplies it through the device (5).

As described above, in the coke dry type fire extinguishing system, inert gas is applied to the coke to cool and extinguish high-temperature coke. When the gaseous coke put into the prechamber 1a of the CDQ main body 1 moves to the cooling chamber 1b, The inert gas and the gaseous coke are subjected to heat exchange by supplying the inert gas to the cooling chamber 1b through the heat exchanger 6 so that the gaseous coke is cooled and the heat recovered from the high temperature inert gas generated at this time is used for power generation systems and the like .

However, in the conventional coke dry fire extinguishing method, a large amount of inert gas must be circulated in order to sufficiently cool the gaseous coke and recover a large amount of heat. Therefore, the CDQ facility must be enlarged, and 30% Of the total amount of the waste water.

In order to solve the above problems, the present invention provides a coke oven which comprises a pre-chamber and a lower cooling chamber of a coke dry fire extinguishing facility, in which carbon dioxide is supplied to the glow-in-coke to cool the sensible heat of the glow- It can be recovered safely and effectively, and only the carbon monoxide generated by the chemical reaction of the red coke and carbon dioxide can be separated and recycled to steel or chemical processes.

According to an embodiment of the present invention, there is provided a method of manufacturing a CDQ body, comprising: injecting a glow coke into a prechamber above the CDQ body;

Supplying carbon dioxide to the prechamber into which the red gypsum coke has been introduced, thereby first cooling the gypsum coke through sensible heat recovery by reaction between the gypsum coke and carbon dioxide;

Moving the primary cooled gypsum coke to a cooling chamber below the CDQ body; And

And injecting carbon dioxide into the cooling chamber to secondarily cool the red coke through sensible heat recovery by the reaction of the red coke and the carbon dioxide. The present invention also provides a sensible heat recovery method using coke.

The carbon dioxide supplied to the prechamber may be the carbon dioxide injected into the cooling chamber transferred to the prechamber.

The carbon dioxide injected into the cooling chamber may be transferred to the prechamber by a blower.

The method may further include recovering carbon monoxide generated by the reaction with the carbon dioxide after the first cooling step, the second cooling step, or the first cooling step and the second cooling step.

The recovering step

Removing foreign matter contained in the carbon monoxide generated by using the dust collecting device; And

And cooling the carbon monoxide using a heat exchanger.

According to another embodiment of the present invention, there is provided a carbon monoxide recycling method characterized in that carbon monoxide recovered in the recovering step is recycled as a reducing gas in a steelmaking process or a raw material gas in a chemical process.

The present invention enables the sensible heat of the red coke to be recovered safely and effectively by supplying carbon dioxide to the red coke in the upper pre-chamber and the lower cooling chamber of the coke dry fire extinguishing system, Only the carbon monoxide generated by the chemical reaction of the red coke and carbon dioxide can be separated and recycled as the raw material gas for the steelmaking or chemical process.

1 schematically shows a conventional coke dry fire extinguishing facility.
2 is a schematic view showing an example of a dry fire extinguishing system of a red grit coke using carbon dioxide according to the present invention.
3 schematically shows another example of the dry fire extinguishing system of the red grit coke using carbon dioxide according to the present invention.

Hereinafter, preferred embodiments of the present invention will be described with reference to the accompanying drawings. However, the embodiments of the present invention can be modified into various other forms, and the scope of the present invention is not limited to the embodiments described below.

More particularly, the present invention relates to a method for recovering two-stage sensible heat of coke by using carbon dioxide. More specifically, the present invention relates to a method for recovering coke from a preheated coke in a preheater located above a CDQ body by supplying carbon dioxide to the prechamber into which the coke is injected, A first step of cooling the gypsum coke through sensible heat recovery by the reaction of carbon dioxide, a step of moving the first cooled gypsum coke to a cooling chamber below the CDQ body, and a step of injecting carbon dioxide into the cooling chamber, And recovering the sensible heat of the coke by using the carbon dioxide, which comprises the step of secondarily cooling the gypsum coke through the sensible heat recovery by the reaction.

In the present invention, the sensible heat recovery by the reaction between the gaseous coke and the carbon dioxide in the prechamber and the cooling chamber includes both the chemical and physical heat recovery of the gaseous coke and the carbon dioxide. The chemical heat recovery reaction is a reaction between the gaseous coke and carbon dioxide Means performing a Boudouard reaction as shown in Reaction Scheme 1 below.

[Reaction Scheme 1]

C (s) + CO ₂ ↔ 2CO H = + 172.5 KJ / mol

That is, the glowing coke (C) of the solid phase is a carbon monoxide (CO) generated by the reaction with carbon dioxide gas (CO _2), wherein the reaction enthalpy (ΔH) is a +172.5 KJ / mol, glowing coke _{(C (s))} and This corresponds to an endothermic reaction in which the enthalpy of carbon monoxide (CO) corresponding to the product increases from the reaction enthalpy of carbon dioxide (CO ₂ ). By this endothermic reaction, the temperature of the gypsum coke is lowered and cooled.

In the present invention, the sensible heat recovery includes a physical heat recovery reaction in addition to a chemical heat recovery reaction. The relatively low temperature carbon dioxide exchanges heat physically as compared to the high temperature cryogen, so that the heat of the cryogen is transferred to the carbon dioxide, the carbon dioxide is heated, and the gypsum coke is cooled.

In the present invention, the term " two-stage sensible heat recovery " means two stages of a physical heat recovery reaction and a chemical heat recovery reaction. However, by performing a heat recovery reaction in each of the prechamber and the cooling chamber, it means.

Hereinafter, the sensible heat recovery method of the present invention will be described in more detail.

The high temperature cryogenic coke, about 1100 ℃, which is discharged from the coke manufacturing process after being carburized, is put into the coke bucket and then put into the prechamber of the CDQ body by the winch lift.

After the red coke is introduced into the prechamber as described above, carbon dioxide is used as the cooling circulation gas for the dry cooling of the red coke, and the red coke is introduced into the free chamber through the carbon dioxide and the Boudouard reaction a chemical heat recovery reaction takes place, a physical heat recovery reaction takes place, and the gaseous coke is primarily cooled.

However, the carbon dioxide supplied to the prechamber may be directly injected into the prechamber, and part of the carbon dioxide injected into the cooling chamber may be transferred to the prechamber.

Specifically, in the former case, when a red coke is injected into the prechamber, carbon dioxide is directly injected into the prechamber, and the glow coke and the injected carbon dioxide can perform the sensible heat recovery reaction.

In the latter case, carbon dioxide is injected into the cooling chamber, and a part of the injected carbon dioxide is transferred to the prechamber through suction or the like, thereby performing the sensible heat recovery reaction with the glowing coke.

However, if the carbon dioxide supplied to the prechamber is the one in which the carbon dioxide supplied to the cooling chamber is moved to the prechamber, the apparatus necessary for the movement is not particularly limited, And sucking the carbon dioxide injected into the cooling chamber into the prechamber located at the top. The use of a blower for the movement of carbon dioxide is preferable because carbon dioxide can be supplied to the prechamber at a constant flow rate to the prechamber.

The glowing coke is cooled to about 750 to 900 DEG C through the physical and chemical heat recovery reaction with the carbon dioxide in the prechamber, although the temperature at the time of the first introduction into the prechamber corresponds to about 1100 DEG C or so.

The glowing coke which has been primarily cooled through the sensible heat recovery reaction in the prechamber is then moved to the cooling chamber which continues to the lower portion of the prechamber.

When the first cooled cooled coke reaches the cooling chamber, carbon dioxide is injected into the cooling chamber as a cooling circulating gas to cool the coke to a second degree.

The carbon dioxide injected into the cooling chamber may be cooled by using a cooling device such as a gas / steam heat exchanger or the like and then re-injecting the high temperature carbon dioxide obtained by the physical heat recovery reaction with the red coke in the cooling chamber, It may be directly injected directly, but it is more preferable to reinject in terms of economy.

Before the carbon dioxide is re-injected into the cooling chamber, it is preferable to remove foreign substances such as dust contained in the carbon dioxide by using a dust collecting apparatus (dust removing apparatus). In the prechamber, a considerable amount of carbon dioxide It is preferable to add fresh carbon dioxide and reinject.

Further, the high temperature carbon dioxide heated by the physical heat recovery reaction generates high temperature and high pressure steam by the gas / steam heat exchanger, and such steam can be used for direct process or for power generation for electric energy production.

In the cooling chamber, the glowing coke is subjected to a physical heat recovery reaction with the injected carbon dioxide as in the prechamber, and further, a chemical heat recovery reaction is performed through a partial reaction.

Meanwhile, in the prechamber, the temperature of the red coke participating in the puddle reaction is about 1100 ° C., whereas in the cooling chamber, the red coke participating in the puddle reaction is first cooled in the prechamber, ° C, the reactivity of the Buda reaction is somewhat reduced. In the prechamber, the chemical heat recovery reaction mainly occurs, while in the cooling chamber, the physical heat recovery reaction occurs mainly.

The gypsum coke is secondarily cooled by a physical and chemical heat recovery reaction in the cooling chamber and the temperature of the coke is about 750-900 ° C. when initially introduced into the cooling chamber, The temperature drops.

The present invention may further comprise the step of recovering the carbon monoxide generated by the puddle reaction after cooling the gypsum coke in each of the prechamber and the cooling chamber.

As described above, a large amount of carbon dioxide is converted into carbon monoxide by the reaction of Pb with carbon dioxide, and this carbon monoxide is removed by using a dust collector to remove foreign substances such as dust contained in the carbon monoxide, So that only the cooled pure carbon monoxide gas can be recovered.

According to another embodiment of the present invention, there is provided a method of recycling carbon monoxide recovered in the recovering step.

Since the recovered carbon monoxide is at a high temperature, it can be recovered as electric energy by supplying heat to the power generation system through a heat exchanger, and can be directly used as a reducing gas by being directly injected into a reducing furnace, It can also be used as raw material gas.

FIG. 2 is a schematic view showing an example of a dry fire extinguishing system using a carbon dioxide-containing dry powder in accordance with the present invention. A high-temperature glowing coke moves through a coke bucket 102 to a CDQ body having a space formed therein, The CDQ body is divided into a prechamber 101-1 located at the upper part and a cooling chamber 101-2 located at the lower part, and the glowing coke first moves to the prechamber 101-1.

When the heat coke reaches the prechamber 101-1, carbon dioxide is injected into the cooling chamber 101-2 through the carbon dioxide injection line 105 and the carbon monoxide / carbon dioxide discharge blower 110) to move a part of the carbon dioxide injected into the cooling chamber 101-2 to the prechamber 101-1.

Since some of the carbon dioxide transferred to the prechamber 101-1 is relatively low in temperature as compared with the infrared coke, the gypsum coke is cooled in the prechamber 101-1 through the physical heat recovery reaction with the carbon dioxide, Which is an endothermic reaction, and a large amount of carbon monoxide is generated.

The coke cooled primarily in the prechamber 101-1 moves to the cooling chamber 101-2 located in the lower portion of the prechamber 101-1 and the coke reaches the cooling chamber 101-2 The carbon dioxide is injected into the cooling chamber 101-2 through the carbon dioxide input line 105. [

In the cooling chamber 101-2, the coke is subjected to a physical and chemical heat recovery reaction with the injected carbon dioxide, and is secondarily cooled to about 200 ° C. The coke is discharged through the coke discharging device 107, Lt; / RTI >

The carbon monoxide generated by the reaction of the fused coke with the carbon dioxide has a small molecular weight and moves to the upper portion of the prechamber 101-2 and the carbon monoxide is removed through the dust removing unit 103 located at the upper portion of the prechamber 101-2. The foreign substance contained therein is removed, cooled by the heat exchanger 109, discharged through the carbon monoxide / carbon dioxide discharge blower 110, connected to the carbon monoxide transport line 111, and recycled where necessary.

The carbon monoxide / carbon dioxide discharge blower 110 is for discharging carbon monoxide generated in the Pudad reaction, but also discharges a small amount of carbon dioxide. As described above, the carbon monoxide / carbon dioxide discharge blower 110 is installed in the cooling chamber 101-2 And can also be used to move the injected carbon dioxide to the pre-chamber 101-1 located at the top.

On the other hand, the carbon dioxide heated through the glowing coke and the physical heat recovery reaction is removed from the carbon dioxide by the dust removing device 103, cooled by the gas / steam heat exchanger 104, 105, and then fed back to the cooling chamber 101-2 through the gas circulation blower 106. [

2, fresh carbon dioxide may be added to the recycled carbon dioxide to inject the carbon dioxide into the cooling chamber 101-2. Although not specifically shown, the carbon dioxide injection line 105 may be connected to the cooling chamber 101 -2) and inject only new carbon dioxide.

FIG. 3 schematically shows another example of a dry fire extinguishing system using a carbon dioxide-based dry coke of the present invention, wherein a hot cryogenic coke is introduced through a coke bucket 102 into a prechamber 101-1, . When the coke reaches the prechamber 101-1, carbon dioxide is injected into the prechamber 101-1 through the carbon dioxide injection line 105 connected to the prechamber 101-1, The hot coke of the high temperature is firstly cooled to about 750 to 900 ° C. through the physical and chemical heat recovery reaction with the injected carbon dioxide.

Thereafter, the primary cooled coke moves to the cooling chamber 101-2 located in the lower portion of the prechamber 101-1. When the coke reaches the cooling chamber 101-2, carbon dioxide is injected into the cooling chamber 101-2 through the carbon dioxide input line 105 connected to the cooling chamber 101-2, and the glow- And secondly to about 200 < 0 > C through physical and chemical heat recovery reactions.

The cooled glowing coke is discharged through the coke discharge device 107 and connected to the cooling coke discharge line 108.

3, the carbon dioxide injection line 105 may be directly connected to the cooling chamber 101-2 to be injected immediately, or alternatively, the carbon dioxide injection line 105 may be directly injected into the cooling chamber 101-2, The carbon dioxide heated by the glowing coke and the physical heat recovery reaction is removed through the dust removing device 103 and cooled by the gas / steam heat exchanger 104 and then passed through the carbon dioxide input line 105 New carbon dioxide can be added and supplied again to the cooling chamber 101-2 through the gas circulation blower 106. [

Example

Hereinafter, the present invention will be described more specifically by way of specific examples. The following examples are provided to aid understanding of the present invention, and the scope of the present invention is not limited thereto.

[Example 1]

1 ton of cryogenic coke at a temperature of 1,000 to 1,100 ° C was introduced into the CDQ prechamber and carbon dioxide was injected into the cooling chamber at a flow rate of 1,000 to 1,400 Nm ³ / hr as shown in Table 1 below.

Then, a portion of the carbon dioxide present in the lower cooling chamber was sucked into the prechamber at a flow rate of 50 to 100 Nm ³ / hr using a carbon monoxide / carbon dioxide discharge blower connected to the prechamber.

In the prechamber, the gypsum coke was subjected to physical and chemical heat recovery reaction with carbon dioxide, and the flow rate of the mixed gas of carbon monoxide and carbon dioxide discharged was 80 to 200 Nm ³ / hr. The concentration of carbon monoxide in the mixed gas was about 70 ~ 95% and the carbon dioxide was about 5 ~ 30%.

The red coke was firstly cooled to about 700 ~ 900 ℃ through the sensible heat recovery reaction in the prechamber and then moved to the cooling chamber.

When the first cooled cryogenically heated coke reaches the cooling chamber, carbon dioxide is further injected at a flow rate of 50 to 100 Nm ³ / hr, and the gypsum coke is subjected to a physical and chemical heat recovery reaction with the carbon dioxide, The total flow rate of the mixed gas of carbon monoxide and carbon dioxide was measured at 1,000 to 1,500 Nm ³ / hr.

The concentration of carbon monoxide in the mixed gas was about 0 ~ 10%, and the carbon dioxide was about 90 ~ 100%. In addition, the red gypsum coke was secondarily cooled to about 100 to 200 DEG C through a sensible heat recovery reaction in the cooling chamber.

equipment Condition unit range Top
Prechamber Lower CO ₂
Upper suction flow Nm ³ / hr 50-100 CO ₂ conversion rate % 70 ~ 95 CO / CO ₂ emission flow rate Nm ³ / hr 80 ~ 200  CO concentration in exhaust gas % 70 ~ 95 CO ₂ concentration in the exhaust gas % 5 to 30 Coke supply temperature ℃ 1,000-1,100 Coke discharge temperature ℃ 700 ~ 900 bottom
Cooling chamber CO ₂ circulation flow Nm ³ / hr 1,000 to 1,400 CO ₂ additional input Nm ³ / hr 50-100 CO ₂ conversion rate % 0-5 CO / CO2 Emission Flow Nm ³ / hr 1,000 to 1,500  CO concentration in exhaust gas % 0 to 10 CO ₂ concentration in the exhaust gas % 90-100 Coke supply temperature ℃ 700 ~ 900 Coke discharge temperature ℃ 100 to 200

As shown in Table 1, the ratio of the carbon dioxide absorbed into the prechamber to carbon monoxide through the booth reaction is about 70 to 95%, while the carbon dioxide injected from the cooling chamber is converted into carbon monoxide through the booth reaction The ratio is about 0 to 5%. Therefore, it can be seen that, in the prechamber, the gaseous coke and carbon dioxide mainly perform the chemical heat recovery reaction, whereas the cooling chamber mainly performs the physical heat recovery reaction.

[Example 2]

After the temperature In the glowing coke 1 ton corresponding to 1,000 ~ 1,100 ℃ the CDQ-free chamber, the carbon dioxide was injected at a flow rate of 50 ~ 100 Nm ³ / hr in the prechamber.

In the prechamber, the gypsum coke was subjected to physical and chemical heat recovery reactions with the injected carbon dioxide, and the total flow rate of the mixed gas of carbon monoxide and carbon dioxide was measured at 80 to 200 Nm ³ / hr.

The concentration of carbon monoxide in the mixed gas was about 70 ~ 95%, and carbon dioxide accounted for about 5 ~ 30%. Also, the red coke was first cooled to about 700-900 ° C. through the sensible heat recovery reaction in the prechamber, and then moved to the cooling chamber.

When the primary cooled cryogenically cooled coke reached the cooling chamber, carbon dioxide was injected at a flow rate of 1,000 to 1,400 Nm ³ / hr, and the gypsum coke performed a physical and chemical heat recovery reaction with the injected carbon dioxide in the cooling chamber . As a result of the sensible heat recovery reaction, the total flow rate of the mixed gas of carbon monoxide and carbon dioxide was measured at 1,000 to 1,500 Nm ³ / hr.

The concentration of carbon monoxide in the mixed gas was about 0 ~ 10%, and the carbon dioxide was about 90 ~ 100%. The gypsum coke was secondarily cooled to about 100 ~ 200 ℃ through the sensible heat recovery reaction in the cooling chamber.

equipment Condition unit range Top
Pre-Chamber CO ₂ top feed flow Nm ³ / hr 50-100 CO ₂ conversion rate % 70 ~ 95 CO / CO ₂ emission flow rate Nm ³ / hr 80 ~ 200  CO concentration in exhaust gas % 70 ~ 95 CO ₂ concentration in the exhaust gas % 5 to 30 Coke supply temperature ℃ 1,000-1,100 Coke discharge temperature ℃ 700 ~ 900 bottom
Cooling-Chamber CO ₂ circulation flow Nm ³ / hr 1,000 to 1,400 CO ₂ conversion rate % 0-5 CO / CO ₂ emission flow rate Nm ³ / hr 1,000 to 1,500  CO concentration in exhaust gas % 0 to 10 CO ₂ concentration in the exhaust gas % 90-100 Coke supply temperature ℃ 700 ~ 900 Coke discharge temperature ℃ 100 to 200

As shown in Table 2, the ratio of the carbon dioxide injected into the prechamber to the carbon monoxide through the puddle reaction is about 70 to 95%, while the carbon dioxide injected into the cooling chamber is converted into carbon monoxide through the puddle reaction The ratio is about 0 to 5%. Therefore, it can be seen that in the prechamber, the heat recovery coke and carbon dioxide mainly perform the chemical heat recovery reaction, whereas the physical heat recovery reaction occurs mainly in the cooling chamber.

In the first embodiment, carbon dioxide is injected into the cooling chamber, and then part of the carbon dioxide is sucked into the prechamber. In the second embodiment, carbon dioxide is separately injected into each of the prechamber and the cooling chamber. It can be seen that there is no difference in the sensible heat recovery efficiency because the flow rate of the gas and the temperature of the coke to be discharged by the second cooling are all the same. However, the suction structure of the first embodiment is preferable because it can be operated simply with a simpler structure in terms of actual process.

[Comparative Example 1]

One ton of cryogenic coke at a temperature of 1,000 to 1,100 ° C was introduced into the CDQ prechamber and then transferred to the cooling chamber and nitrogen gas was injected at a flow rate of 1,300 to 1,400 Nm ³ / hr to perform a physical heat recovery reaction . The temperature of the discharged coke was measured and found to be cooled to about 100 to 200 ° C.

equipment Condition unit range Top
Pre-Chamber Coke supply temperature ℃ 1,000-1,100 bottom
Cooling-Chamber N ₂ circulating flow Nm ³ / hr 1,300-1,400 Coke discharge temperature ℃ 100 to 200

The present invention uses carbon dioxide as the cooling circulation gas. However, compared to the case where nitrogen gas is used, since the temperature of the discharged coke is about 100 to 200 DEG C, the same sensible heat recovery effect Can be obtained. In addition, the present invention can recycle a large amount of carbon monoxide generated in a chemical heat recovery reaction in various directions, thereby improving energy efficiency.

[Comparative Example 2]

One ton of cryogenic coke at a temperature ranging from 1,000 to 1,100 ° C was introduced into the CDQ prechamber and then transferred to the cooling chamber and carbon dioxide was injected at a flow rate of 100 to 300 Nm ³ / hr to recover coke, physical and chemical heat The reaction was carried out. The temperature of the discharged coke was measured to be about 600 to 750 ° C.

equipment Condition unit range Top
Pre-Chamber Coke supply temperature ℃ 1,000-1,100 bottom
Cooling-Chamber CO ₂ circulation flow Nm ³ / hr 100 to 300 Coke discharge temperature ℃ 600 to 750

Unlike the present invention in which the heat recovery reaction is performed in both the prechamber and the cooling chamber, the process of recovering the sensible heat of the cryocooler using carbon dioxide has been carried out only in the cooling chamber as in Comparative Example 2, It can be seen that the discharged coke is cooled only to about 600 to 750 ° C and the sensible heat is not effectively recovered. In contrast, the present invention can cool the discharged coke to about 100 to 200 ° C by performing the sensible heat recovery reaction in both the prechamber and the cooling chamber, thereby cooling the glowing coke secondarily, and recovering sensible heat more effectively .

While the present invention has been particularly shown and described with reference to exemplary embodiments thereof, it is to be understood that the scope of the present invention is not limited to the disclosed exemplary embodiments, and that various modifications and changes may be made thereto without departing from the scope of the invention. To those of ordinary skill in the art.

1: CDQ body
1a, 101-1: Prechamber
1b, 101-2: cooling chamber
2, 102: Coke bucket
3: Winch lift
4: Coke discharge device
5: Air supply device for combustion
6: gas supply pipe
103: Dust removal device
104: Gas / steam heat exchanger
105: Carbon dioxide input line
106: gas circulation blower
107: Coke discharge device
108: Cooling coke discharge line
109: Heat exchanger
110: Carbon monoxide / carbon dioxide exhaust blower
111: Carbon monoxide transport line

Claims (6)

Injecting a glowing coke into the prechamber above the CDQ body;
Supplying carbon dioxide to the prechamber into which the red gypsum coke has been introduced, thereby first cooling the gypsum coke through sensible heat recovery by reaction between the gypsum coke and carbon dioxide;
Moving the primary cooled gypsum coke to a cooling chamber below the CDQ body; And
And injecting carbon dioxide into the cooling chamber to secondarily cool the red coke through sensible heat recovery by reaction between the red coke and the carbon dioxide.
The method of claim 1, wherein the carbon dioxide supplied to the prechamber is carbon dioxide injected into the cooling chamber, and the carbon dioxide injected into the cooling chamber is transferred to the prechamber.
The method of claim 2, wherein the carbon dioxide injected into the cooling chamber is transferred to the prechamber by a blower.
The method of claim 1, further comprising the step of recovering carbon monoxide generated by the reaction with the carbon dioxide after the first cooling step, the second cooling step, or the first cooling step and the second cooling step Method for recovering sensible heat of coke by using carbon dioxide.
5. The method of claim 4, wherein the recovering step
Removing foreign matter contained in the carbon monoxide generated by using the dust collecting device; And
A method of recovering sensible heat of a cured heat of a coke using carbon dioxide, comprising the step of cooling the carbon monoxide using a heat exchanger.
The method for recycling carbon monoxide as recited in claim 4 or 5, wherein the recovered carbon monoxide is recycled as a reducing gas in a steelmaking process or a raw material gas in a chemical process.

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