KR102556854B1 - Resource Circulation System - Google Patents

Abstract

The present invention relates to a resource circulation system, which allows efficient reuse of resources such as carbon dioxide absorber, comprising: a pretreatment unit which receives exhaust gas from an exhaust gas emission source and removes pollutants from the exhaust gas; a desulfurization unit which receives the exhaust gas from the pretreatment unit, removes sulfur oxides from the exhaust gas, and discharges the exhaust gas; a carbon dioxide absorption tank which receives the exhaust gas from a front end or rear end of the desulfurization unit, removes carbon dioxide and sulfur oxides from the exhaust gas by reaction with a carbon dioxide absorber, and discharges the treated gas; a primary precipitation tank which receives a reaction solution from the carbon dioxide absorption tank and precipitates foreign matter by coagulation with a coagulant; a secondary precipitation tank which receives the reaction solution from the primary precipitation tank, produces calcium carbonate by reaction with calcium oxide, and simultaneously removes carbon dioxide captured from the reaction solution to regenerate the carbon dioxide absorber; a receiving tank which receives the calcium carbonate from the secondary precipitation tank and stores the same; and a regenerated carbon dioxide absorber storage tank which receives the regenerated carbon dioxide absorber from the secondary precipitation tank and circulates the same to the carbon dioxide absorption tank.

Description

Resource Circulation System {Resource Circulation System}

The present invention relates to a system for recycling resources such as a carbon dioxide absorbent in the process of purifying exhaust gas discharged from a power plant.

In power plants using fossil fuels, a large amount of carbon dioxide is included in exhaust gas after combustion. At this time, the generation of nitrogen oxides (NOx) due to the high-temperature combustion process is removed with a denitrification facility (SCR or SNCR), and even if the case of relatively expensive LNG power generation is excluded, depending on the type of fossil fuel used as fuel, Sulfur oxide (SOx) is generated after combustion due to the sulfur component in the fuel, and dust containing ash and heavy metals is removed by an electric precipitator (EP).

A large-scale desulfurization facility (FGD) is operated to suppress the emission of SOx into the atmosphere, and sulfur components are removed in the form of CaSO ₄ from a huge absorption tower using limestone as an absorbent. Among these flue gases, CO ₂ (366 ton/hr, based on one 500 MWH power plant) is more than 100 times greater than the amount of SOx generated and removed. *Based on 300 days).

In order to remove or reduce such a huge amount of CO ₂ , it is predicted that the facility and operation will be impossible from the scale and the generation of wastewater will be enormous with an absorbent method such as limestone.

Therefore, it is required to develop an adsorbent capable of excellent adsorption capacity for carbon dioxide and low-cost CO ₂ degassing or easy resource conversion from a feasible facility in terms of economic feasibility and scale. It is desirable to suppress the occurrence.

Republic of Korea Patent Registration No. 10-1938424

The present invention has been made to solve the above problems, and is intended to provide a system that efficiently reuses resources such as a carbon dioxide absorbent in the process of treating pollutants including carbon dioxide in exhaust gas.

The resource circulation system according to the present invention (hereinafter referred to as "the system of the present invention") for achieving the above object is a preprocessing unit that receives exhaust gas discharged from an exhaust gas emission source and removes pollutants from the exhaust gas. ; a desulfurization unit receiving exhaust gas from the preprocessing unit and removing and discharging sulfur oxides from the exhaust gas; a carbon dioxide absorption tank receiving exhaust gas from the front or rear end of the desulfurization unit, reacting with the carbon dioxide absorbent to remove carbon dioxide and sulfur oxides from the exhaust gas, and discharging processed gas; a primary precipitation tank receiving the reaction liquid from the carbon dioxide absorption tank and precipitating foreign substances by a flocculation reaction with a coagulant; a second precipitation tank in which the reaction solution is introduced from the first precipitation tank and reacted with calcium oxide to produce calcium carbonate and the carbon dioxide absorbent is regenerated by removing carbon dioxide captured from the reaction solution; an acquisition tank for receiving and storing calcium carbonate from the secondary precipitation tank; and a regenerated carbon dioxide absorbent storage tank for receiving the regenerated carbon dioxide absorbent from the secondary precipitation tank and circulating it to the carbon dioxide absorbent tank.

As an example, the processing gas discharged from the desulfurization unit or the processing gas discharged through the carbon dioxide absorption tank is discharged to the outside through a heat exchanger.

As an example, a carbon dioxide absorbent is prepared by mixing an aqueous solution of sodium hydroxide, illite extract, sodium tetraborate, and water glass, and a manufacturing unit for supplying the prepared carbon dioxide absorbent to the carbon dioxide absorption tank is further included.

As an example, the carbon dioxide absorbent may further contain hydrogen peroxide.

As an example, a coal crushing unit for crushing fossil fuel supplied as a fuel source of the emission source is further configured at the front end of the emission source, and in the manufacturing unit, the precipitate generated during the manufacturing process of the carbon dioxide absorbent is converted into a desulfurization catalyst before combustion in the coal crushing unit. characterized by supplying

As an example, the calcium carbonate stored in the obtaining tank is transferred to the desulfurization unit to remove sulfur oxides from the exhaust gas.

As described above, the present invention efficiently operates the system without a desulfurization facility or without a load on the desulfurization facility by using a carbon dioxide absorbent capable of simultaneously treating carbon dioxide and sulfur oxides in the treatment of pollutants including carbon dioxide in exhaust gas. In addition, the carbon dioxide captured in the carbon dioxide absorbent can be recovered as high-purity precipitated calcium carbonate without impurities, and at the same time, the carbon dioxide absorbent can be recycled and circulated, which is environmentally friendly.

In addition, the system of the present invention can be used as a desulfurization catalyst added before combustion of fossil fuel used in the emission source in the case of not only the production liquid but also the precipitate generated during the manufacturing process of the carbon dioxide absorbent, thereby circulating resources while controlling the generation of waste There are advantages.

In addition, the system of the present invention has the advantage of recycling resources because a portion of the obtained calcium carbonate can be used to remove sulfur oxides in the desulfurization unit.

1 is a block diagram showing the system of the present invention;
2 is a diagram showing the carbon dioxide absorption mechanism of the carbon dioxide absorbent applied to the present invention,
Figure 3 is a graph showing the experimental results on the removal of sulfur oxides,
4 is a graph showing experimental results regarding the removal of carbon dioxide.

In the following, preferred embodiments according to the present invention will be described in detail.

As shown in FIG. 1, the system 1 of the present invention includes a pre-processing unit 5 for receiving exhaust gas discharged from an exhaust gas emission source 4 and removing pollutants from the exhaust gas; a desulfurization unit 6 that receives exhaust gas from the preprocessing unit 5 and removes and discharges sulfur oxides from the exhaust gas; a carbon dioxide absorption tank (8) receiving exhaust gas from the front or rear end of the desulfurization unit (6), removing carbon dioxide and sulfur oxides from the exhaust gas by reaction with the carbon dioxide absorbent, and discharging processed gas; a primary precipitation tank (9) receiving the reaction solution from the carbon dioxide absorption tank (8) and precipitating foreign substances by coagulant reaction with the coagulant; a secondary precipitation tank (10) in which the reaction liquid is introduced from the primary precipitation tank (9) and reacted with calcium oxide to produce calcium carbonate and the carbon dioxide absorbent is regenerated by removing carbon dioxide captured from the reaction liquid; an acquisition tank 11 for receiving and storing calcium carbonate from the secondary precipitation tank 10; and a regenerated carbon dioxide absorbent storage tank 12 for receiving the regenerated carbon dioxide absorbent from the secondary precipitation tank 10 and circulating it to the carbon dioxide absorbent tank 8.

The preprocessing unit 4 receives the exhaust gas discharged from the emission source 4 and removes pollutants from the exhaust gas, and the pollutants may be nitrogen oxides and dust. An oxide removal device, a dust collector, and the like may be configured.

The emission source 4 is a concept that collectively refers to a place, facility, etc. that emits exhaust gas mixed with nitrogen oxides, sulfur oxides, and carbon dioxide as various pollutants such as a power plant.

The desulfurization unit 6 is configured to remove sulfur oxides from exhaust gas, and in the system 1 of the present invention, a carbon dioxide absorbent capable of simultaneously removing sulfur oxides and carbon dioxide from the carbon dioxide absorption tank 8 described below is used. As it is used, the desulfurization unit 6 can be selectively bypassed, thereby simplifying the system and controlling the load of the desulfurization unit 6.

Various known techniques can be applied to the removal of sulfur oxides in the desulfurization unit 5, and for example, a mechanism for removing sulfur oxides by contacting a calcium carbonate slurry with exhaust gas can be applied. A portion of the calcium carbonate obtained in the obtaining tank 11 is supplied to the desulfurization unit 5 so that desulfurization can be performed from the exhaust gas.

That is, the calcium carbonate generated in the system can be reused as a catalyst for desulfurization in the system. Here, since the operating mechanism for desulfurization by calcium carbonate is a well-known operating mechanism, its detailed description will be omitted.

The heat exchanger 7 allows heat exchange while passing the processed gas through the desulfurization unit 6 or the carbon dioxide absorption tank 8, and various known technologies exist in the case of the heat exchanger 7. , its detailed description is omitted.

The carbon dioxide absorption tank 8 receives exhaust gas from the front or rear end of the desulfurization unit 6, and reacts with the carbon dioxide absorbent containing sodium hydroxide solution to remove carbon dioxide and sulfur oxides from the exhaust gas. It corresponds to a configuration in which the process gas is discharged to the heat exchanger (7) after removing the heat exchanger (7).

As mentioned above, the carbon dioxide absorbing tank 8 uses a carbon dioxide absorbent that simultaneously removes carbon dioxide and sulfur oxides, so that the exhaust gas that has not passed through the desulfurization unit 6 can flow in, as shown in the drawing. Although it has not been done, the reaction can be performed by introducing the exhaust gas that has passed through the desulfurization unit 6.

As shown in FIG. 1, the carbon dioxide absorbent is manufactured in the manufacturing unit 2, and the carbon dioxide absorbent is characterized in that it includes an aqueous solution of sodium hydroxide, illite extract, sodium tetraborate, and water glass.

In the manufacturing unit 2, precipitate is produced as a carbon dioxide absorbent and a desulfurization catalyst by a method described below.

In the manufacturing method, the illite powder is added to a reaction tank in which water heated to 40 to 100 ° C. is stored and stirred (S10); Stirring by adding sodium hydroxide to the reactor (S20); Separating and filtering the supernatant in the reactor (S30); Separating the precipitate from the reactor (S40); characterized in that it comprises a.

First, in step S10, the illite powder is put into a reaction tank in which water heated to 40 to 100 ° C. is stored and stirred.

An illite extract is obtained through this step (S10), and the illite is expressed as {K _0.75 [Al _1.75 (Mg Fe ₂ +) _0.25 ] (Si _3.50 Al _0.50 )O ₁₀ (OH) ₂ } It is a mineral that has been found to be buried in large quantities in the Yeongdong region of Korea. The layer charge is lower than that of muscovite mica, and the charge is due to isomorphic substitution reduction of Al ³⁺ and Si ⁴⁺ in the tetrahedral plate. Some isomorphic substitutions occur in the octahedral plate.

Illite is non-expandable due to the strong bonding force by K + existing between layers, and the layer spacing is 10 Å. Therefore, it is a mineral that is extracted from the liquid phase, has a total cationic charge, and is easily converted into a chelation compound, and in the present invention, it is appropriate to use undifferentiated illite to easily extract such a metal foreign material.

The extract extracted from illite is an extract containing various metal oxides such as potassium oxide, and provides minerals that are easily converted into chelation compounds in the liquid phase in the carbon dioxide and sulfur oxides absorption reaction of sodium hydroxide aqueous solution described below. It acts as a reaction enhancer.

That is, in the absorption of carbon dioxide containing SOx in the sodium hydroxide aqueous solution, the illite extract is further added to increase the absorption efficiency.

Next, it has a step (S20) of stirring by adding sodium hydroxide to the reaction tank.

In this way, the illite extract is mixed with an aqueous solution of sodium hydroxide, which is characterized in that it simultaneously removes a mixed gas containing high-temperature, high-concentration carbon dioxide and COS (hydrocarbon, O ₂ , SOx) there is. That is, sulfur oxides (SOx) as well as carbon dioxide are simultaneously absorbed from power plant exhaust gas.

The principle of removing sulfur oxides and carbon dioxide from the sodium hydroxide aqueous solution is shown in the following reaction formula. That is, sulfur trioxide (sulfurous acid) and sulfur dioxide are removed by reacting with sodium hydroxide and being extracted with anhydrous sodium sulfate and sodium sulfite, respectively, as shown below.

And carbon dioxide is removed by reacting with sodium hydroxide to produce sodium carbonate as shown in the following reaction formula. In addition, the generated sodium carbonate reacts with excess sulfur oxides to further increase the sulfur oxide removal effect, and the produced carbon dioxide is removed by sodium hydroxide.

1) 2NaOH + SO ₃ = Na ₂ SO ₄ + H ₂ O

2) 2NaOH + SO ₂ = Na ₂ SO ₃ + H ₂ O

3) 2NaOH + CO ₂ = Na ₂ CO ₃ + H ₂ O

4) NaOH + CO ₂ = NaHCO ₃

In addition to this, as mentioned above, the reaction formula with sodium hydroxide of illite extract as a reaction enhancer is as shown below. Only the main components of illite have been described, and oxides of minor components such as Ca, Fe, Mg, Mn, Ti and P ₂ O ₅ also contribute to the formation of stable metal chelation compounds in the liquid phase.

1) 2NaOH + SiO ₂ = Na ₂ O. SiO ₂ + H ₂ O

2) 2NaOH + K ₂ O = Na ₂ O + 2KOH

3) Na ₂ O + Al ₂ O ₃ + H ₂ O = 2NaAlO ₂ + H ₂ O

In addition to this, the present invention presents an example in which a step (S10-1) of adding sodium tetraborate to the reaction tank and stirring it before the step S20 is further included. In addition to this, an example in which a step (S20-1) of stirring by adding water glass to the reaction tank is further included after the step S20.

That is, an example in which sodium tetraborate (Na ₂ B ₄ O ₇ .10H ₂ O) and water glass (Na ₂ SiO ₃ ) are further included in the illite extract and the aqueous sodium hydroxide solution is presented.

In addition to the illite extract, the sodium hydroxide aqueous solution is to further include sodium tetraborate and water glass. As sodium tetraborate and water glass are further added in this way, carbon dioxide and the absorbent component react directly, so the reaction rate is much faster and the mass transfer coefficient is increased.

Moreover, since sodium tetraborate and water glass have high viscosities, absorbed gaseous carbon dioxide cannot escape and quickly melts into a liquid state and reacts with carbonic acid, thereby doubling the absorption rate of carbon dioxide.

In addition to this, the present invention suggests an example in which, after the step S20-1, a step (S20-2) of adding hydrogen peroxide to the reaction tank and stirring it (S20-2) is further included. That is, an example in which hydrogen peroxide (H ₂ O ₂ ) is further added as a reaction-promoting additive is presented.

The reaction formula of sodium tetraborate and hydrogen peroxide in aqueous sodium hydroxide solution is as follows.

1) Na ₂ B ₄ O ₇ + H ₂ O = Na ₂ O + 2B ₂ O ₃

2) 2NaOH + H ₂ O ₂ = Na ₂ O + H ₂ O + 0.5O ₂

Therefore, the carbon dioxide absorption mechanism is shown in FIG. 2 and the following reaction formula.

1) CO ₂ (g) + CO ₂ (aq) + Na ₂ O + 2OH- = CO ₂ (g) + CO ₃ -- + 2NaOH = CO ₂ (aq) + CO ₃ --

2) CO ₃ -- + H ₂ O + CO ₂ (aq) = 2HCO ₃ -

3) CO ₂ (aq) + OH- = HCO ₃ -

4) HCO ₃ - + OH- = CO ₃ - + H ₂ O

When the reaction is completed in this way, the next step is to separate and filter the supernatant in the reaction tank (S30). Separating the supernatant in the reaction tank and removing foreign substances contained in the supernatant to prepare a carbon dioxide absorbent.

Next, it has a step (S40) of separating the precipitate from the reactor. By separating these precipitates, a desulfurization catalyst, which is a fuel additive, is produced.

The precipitate in the reaction tank contains components extracted from illite and the like, and includes various types of metal salts such as Ca, Fe, Mg, Mn, and Ti.

Therefore, with these active ingredients, a pre-combustion desulfurization catalyst, which is another use of the prepared liquid, is possible, and the separated precipitate as described above can also be used as a desulfurization catalyst with the remaining active ingredients.

In addition, after S40, a step (S40-1) of mixing an additive including a surfactant and an oxyacid with the separated precipitate may be further included.

The precipitate separated as described above, that is, the metal salt aqueous solution is to include an additive including a surfactant and an oxyacid.

The surfactant acts as a dispersant so that the desulfurization catalyst has a large surface area, and it is preferable to use a nonionic surfactant. The nonionic surfactant is a surfactant that does not have a group that dissociates into ions in an aqueous solution and has an -OH group. Although relatively hydrophilic, it has ester, acid amide, and ether bonds in the molecule. The nonionic surfactant includes an ether type, an ester ether type, an ester type, and a nitrogen-containing type.

Examples of the ether-type surfactant include alkyl and alkylaryl polyoxyethylene ethers, alkylarylformaldehyde condensed polyoxyethylene ethers, block polymers and polyoxyethylene-polyoxypropylene copolymers having polyoxypropylene as a lipophilic group, and the like. .

The oxyacid is used to increase the dissolution stability of the metal compound in the metal salt aqueous solution.

The oxyacid is a hydroxycarboxylic acid, and specific examples thereof include citric acid, malic acid, tartaric acid, tartronic acid, glyceric acid, hydroxybutyric acid, hydroxyacrylic acid, lactic acid, and glycolic acid.

On the other hand, in order to improve the desulfurization activity, it is necessary to control the aggregation between the metal components and increase the degree of dispersion. For this purpose, the stability of the aqueous metal salt solution can be improved to some extent by adding oxyacid to the additive, but the cohesiveness between the metal components can be sufficiently improved. The problem of uncontrollable degradation of catalytic performance still exists.

Accordingly, in the step S40-1, an example in which the precipitated carbonate is further included in the additive is presented.

By adding the precipitated carbonate, a fine coating film is formed on the metal salt, so that the repulsive force between the metal salts increases and the aggregation phenomenon is controlled. Preferably, the metal salt and the precipitated carbonate are stored as a mixture and added to the mixture to form an aqueous solution, so that it is reasonable to play a role in preventing aggregation between particles even during the storage process.

The precipitated carbonate includes precipitated crystalline and/or amorphous carbonate compounds with metastable carbonate compounds precipitated from water, such as alkaline earth metal-containing water, such as brine.

This desulfurization catalyst stabilizes the composition by precipitating for a certain period of time after mixing the precipitates without separating and drying the precipitates, and is not shown in the drawing by separating and drying the precipitates, but in a solid form added during combustion in the emission source (4). It can be used as a desulfurization catalyst, and the composition in liquid form remaining after separating the sediment is put into the coal crushing unit 3 for crushing the fossil fuel used as fuel in the emission source 4, as shown in FIG. to be used as a liquid desulfurization catalyst applied to the surface of coal.

The primary precipitation tank 9 receives the reaction solution from the carbon dioxide absorption tank 8 and precipitates foreign substances by coagulant reaction with the coagulant, so that foreign substances such as heavy metals, ash, and SS are removed from the reaction solution by coagulation. This is to increase the purity of calcium carbonate obtained in the secondary precipitation tank 10 at the rear, and to regenerate a regenerated carbon dioxide absorbent free of impurities when regenerating the reaction solution.

The type of coagulant is not limited, and for example, calcium hydroxide (Ca(OH) ₂ ) may be applied.

The secondary precipitation tank 10 receives the reaction solution from the primary precipitation tank 9 and reacts with calcium oxide to produce calcium carbonate and at the same time removes the carbon dioxide captured from the reaction solution so that the carbon dioxide absorbent is regenerated. corresponds to

Here, the reaction liquid is a carbon dioxide absorbent in which carbon dioxide is captured, and in the secondary precipitation tank 10, the carbon dioxide captured in the reaction liquid is converted into calcium carbonate by dropping calcium oxide so that the carbon dioxide absorbent is regenerated at the same time.

That is, by adding CaO according to the equivalent number of carbon dioxide captured in the reaction solution in the secondary precipitation tank 10, high-purity, high-value-added precipitated calcium carbonate, which is a useful resource, is produced.

In addition, the reaction liquid from which foreign substances and captured carbon dioxide are removed through the first precipitation tank 9 and the second precipitation tank 10 can be reused as a regenerated carbon dioxide absorbent.

In order to achieve the purpose of reducing carbon dioxide, costs such as the size of additional facilities or absorbents and operational convenience must be considered, and the cost of energy input is also one of the important items.

Therefore, the cost of the carbon dioxide absorbent provided according to the present invention has a mechanism for recovering the absorption capacity by precipitating it again as calcium carbonate after the chemical absorption reaction of carbon dioxide, and there is no cost other than a slight loss in the piping and absorption tower through the circulation system. In the secondary precipitation tank 10, the temperature of the filtrate is maintained at 60 ° C or higher after calcium carbonate is precipitated by the heat of dilution generated when CaO is added, and an exothermic reaction develops with little heat energy loss. Of course, calcium carbonate has almost no solubility in alkaline water even at a high temperature of 60 ℃ or higher, but only affects the size or crystal form of the precipitate according to the temperature.

The calcium carbonate obtained in the secondary precipitation tank 10 is stored in the obtaining tank 11, and some of the calcium carbonate stored in the obtaining tank 11 is used as a catalyst in the desulfurization unit 6 as mentioned above. to be reused.

Since the obtained calcium carbonate has a very high impurity-free purity, it can be used by itself throughout the industry, such as papermaking, construction, and steelmaking, without any restrictions on demand sources, and through the sintering process, high-purity carbon dioxide and slaked lime are produced to produce resources. can be recycled In addition, such pure calcium carbonate can be used at least in landfills of abandoned mines as a pollution-free resource that is not affected by the natural world.

In addition, the system (1) of the present invention does not directly capture and then store or recycle carbon dioxide, does not require large-scale facilities, does not generate wastewater or has few factors, and produces calcium carbonate of very low solubility by a 1: 1 reaction with carbonic acid quickly. As the entire amount is precipitated at a high rate, the conversion energy cost in a small-scale sedimentation tank is rather converted into heat energy by the exothermic reaction of calcium carbonate. It becomes.

High-purity precipitated calcium carbonate, also a conversion product, can be expected to have high added value in terms of market size and price.

A preferred embodiment of the carbon dioxide absorbent will be described based on experimental examples below.

1,350 g of yellow-phase illite pulverized with 1,000 mesh was added to 15 L of RO water heated to 60 ° C and stirred for 30 minutes. Then, 150 g of sodium tetraborate was added and stirred for 10 minutes to dissolve well (temperature drop of about 10 ° C), and then 300 g of sodium hydroxide was slowly added and stirred. Stir. The temperature of the reaction solution naturally dropped and was stirred until it reached room temperature. Stirring was stopped at room temperature and allowed to stand overnight, and the supernatant was filtered to prepare an adsorbent.

540 g of illite of the yellow phase pulverized with 325 mesh was put into 6 L of RO water heated to 60 ° C. and stirred for 30 minutes. Add 300g of sodium tetraborate and stir for 30 minutes (temperature drop of about 20℃ in the reaction solution). When it was, 300 g of water glass was added and stirred for 1 hour.

After the temperature of the reaction solution naturally dropped to below 60 ° C, 90 g of hydrogen peroxide was added and stirred until the reaction solution reached room temperature. Stirring was stopped at room temperature and allowed to stand overnight, and the supernatant was filtered to prepare an adsorbent.

<Exhaust gas analysis equipment>

NOVA 9K (MRU Emission Monitoring System, Germany) was used, and the sensor, measurement range, and resolution for each measurement object are as follows.

- O ₂ (EC) : 0 ~ 21 Vol% / 0.2%

- CO ₂ (NDIR) : 0 ~ 40 Vol% / 0.3%

- SO ₂ (EC) : 0 ~ 2,000 ppm / 5ppm

* E.C: electrochemical sensor, NDIR: non-dispersive infrared sensor

<Exhaust gas analysis method>

-. SO ₂ analysis

Ignition coal was put in the meseta dissociation firewood stove and ignited, and after 5 minutes, lignite was raised by 1Kg to start combustion. After about 15 minutes, 3 kg of lignite, which had been evenly sprayed with 100 g of the liquid desulfurization catalyst prepared in Example 1, was further raised and combustion was started in earnest.

In order to suck in some of the exhaust gas exhausted through the flue, make a hole in the middle of the flue, connect a silicone hose, completely seal the gap with silicone, and inhale the exhaust gas through a diaphragm pump to adjust the flow meter to 35L/min and experiment. The reactor was blown into the reactor through the In-Let pipe of the gas trap adapter. The exhaust gas discharged through the Out-Let pipe of the gas trap adapter was connected to NOVA 9K, and the amount of SO ₂ was measured.

-. CO ₂ analysis

After preparing an N ₂ bombe and a CO ₂ bombe with a heating device, adjust the flow meter to 30L/min of N ₂ and 5L/min of CO ₂ , respectively, and mix the gas through the Y-shaped adapter to in-let pipe of the gas trap adapter. was blown into the reactor through The CO ₂ concentration was measured at the Out-Let of the gas trap adapter, and 1 L of the CO ₂ chemical adsorbent prepared in Example 2 was introduced into the reaction tank through the dropping funnel, and then the CO ₂ concentration was measured.

<Experimental Example 1> SOx removal performance measurement

After burning lignite in a firewood stove, the amount of SOx generated in exhaust gas was measured and the amount of SOx reduction was measured through the above experimental device.

The experimental results are shown in FIG. 3, and as shown in the graph, it can be seen that the SOx reducing ability is expressed by the action of the absorbent of Example 1 from approximately 37 minutes to 91 minutes.

<Experimental Example 2> CO ₂ Removal Ability Measurement

In the above experimental device, 14% CO ₂ Gas was injected into the main reactor through N ₂ Bombe and CO ₂ Bombe, and then 1L of CO ₂ chemical absorbent prepared in Example 2 was put in and passed through the input gas to reduce CO ₂ was measured.

As the experimental results are shown in FIG. 3, the first descending curve on the graph indicates that Example 2 is injected and CO ₂ is reduced, and while the CO ₂ is reduced, the rising curve shows that the lid of the reactor is opened and the outside air is released. It can be seen that CO ₂ is reduced again as a result of introducing a regenerated absorbent obtained by regenerating the previously used absorbent of Example 2 after allowing CO ₂ to rise.

<Experimental Example 3> Production of CaCO ₃ and Regeneration of CO ₂ Absorbent

In Experimental Example 2, 1L of the absorbent that absorbed CO ₂ (solution temperature: 32°C) was transferred to a 2L Beaker, and 62.16 g of CaO (assay 90%) was added while stirring. As was precipitated, gray brown CaO particles were quickly dissolved, and then the solid was filtered and dried with hot air to obtain 100.1 g of white CaCO ₃ . The filtrate was again used as the CO ₂ absorption regeneration solution of Experimental Example 2.

As described above, although the present invention has been described with limited embodiments and drawings, the present invention is not limited to the above embodiments, of course, from the above description by a person having ordinary technical knowledge in the field to which the present invention belongs. Of course, various modifications and variations may be possible.

1: system of the present invention 2: manufacturing unit
3: coal crushing unit 4: emission source
5: pretreatment unit 6: desulfurization unit
7: heat exchanger 8: carbon dioxide absorption tank
9: 1st precipitation tank 10: 2nd precipitation tank
11: harvesting tank 12: regenerated carbon dioxide absorbent storage tank

Claims (6)

a pre-processing unit receiving the exhaust gas discharged from the exhaust gas source and removing pollutants from the exhaust gas;
a desulfurization unit receiving exhaust gas from the preprocessing unit and removing and discharging sulfur oxides from the exhaust gas;
a carbon dioxide absorption tank receiving exhaust gas from the front or rear end of the desulfurization unit, reacting with the carbon dioxide absorbent to remove carbon dioxide and sulfur oxides from the exhaust gas, and discharging processed gas;
aqueous sodium hydroxide solution; an illite extract prepared by adding illite powder to water heated to 40 to 100° C. and stirring; Sodium tetraborate and water glass, which doubles the absorption rate of carbon dioxide by reacting with carbonic acid while the absorbed gaseous carbon dioxide cannot escape and melts into a liquid state; It is composed of hydrogen peroxide, but the illite powder is added to water heated to 40 to 100 ° C. and stirred, then sodium tetraborate is sequentially added and stirred, sodium hydroxide is added and stirred, and water glass is added and stirred a production unit for preparing a carbon dioxide absorbent by adding hydrogen peroxide, stirring, filtering the supernatant, and supplying the carbon dioxide absorbent to the carbon dioxide absorption tank;
a primary precipitation tank receiving the reaction liquid from the carbon dioxide absorption tank and precipitating foreign substances by a flocculation reaction with a coagulant;
a second precipitation tank in which the reaction solution is introduced from the first precipitation tank and reacted with calcium oxide to produce calcium carbonate and the carbon dioxide absorbent is regenerated by removing carbon dioxide captured from the reaction solution;
an acquisition tank for receiving and storing calcium carbonate from the secondary precipitation tank;
a regenerated carbon dioxide absorbent storage tank for receiving the regenerated carbon dioxide absorbent from the secondary precipitation tank and circulating it to the carbon dioxide absorbent;
A resource circulation system comprising a.
According to claim 1,
The resource circulation system, characterized in that the processing gas discharged from the desulfurization unit or the processing gas discharged through the carbon dioxide absorption tank is discharged to the outside through a heat exchanger.
delete delete According to claim 1,
In front of the emission source, a coal crushing unit for crushing fossil fuel supplied as a fuel source of the emission source is further configured, and in the manufacturing unit, the precipitate generated during the manufacturing process of the carbon dioxide absorbent is supplied to the coal crushing unit as a desulfurization catalyst. resource circulation system.
According to claim 1,
The calcium carbonate stored in the harvesting tank is transferred to the desulfurization unit to remove sulfur oxides from the exhaust gas.