KR20130015330A - Method for control of gaseous hydrogen sulfide - Google Patents

Abstract

PURPOSE: A gaseous hydrogen sulfide processing method is provided to convert hydrogen sulfide into sulfur dioxide which easily dissolves in water, and to easily remove the converted sulfur dioxide using a wet scrubber. CONSTITUTION: A gaseous hydrogen sulfide processing method comprises the following steps. A gaseous hydrogen sulfide processing apparatus is prepared. Power is provided to a discharge electrode of the gaseous hydrogen sulfide processing apparatus. The gaseous hydrogen sulfide is passed through an accommodating chamber of the gaseous hydrogen sulfide processing apparatus. The gas passed through the accommodating chamber is post-processed to a scrubber for sulfur dioxide. The gaseous hydrogen sulfide processing apparatus comprises a main body, the discharge electrode, an outer electrode, a connecting part, a power supply unit, a carrier with a catalyst, and a heat resistance supporting unit. The reactor main body comprises the accommodating chamber, a gas inlet, and an gas outlet, and is comprised of dielectric materials. The discharge electrode is adapted to the accommodating chamber, and partially contacted to the inner part of the reactor main body. The outer electrode is contacted to the exterior of the reactor main body. The connecting part is connected to the outer electrode. The power supply unit supplies power to the discharge electrode. The carrier is adapted by the accommodating chamber, and is selected from aluminum oxide or zeolite with at least one catalyst of selected silver, copper, or manganese. The heat resistance supporting unit is formed at each of the gas inlet and the gas outlet of the accommodating chamber to close the accommodating chamber. The heat resistance supporting comprises the penetration hole with the hole perimeter of gas passage but not the carrier. [Reference numerals] (A) Preparing a hydrogen sulfide processing apparatus; (B) Providing power; (C) Passing hydrogen sulfide; (D) Post-processing

Description

Method for control of gaseous hydrogen sulfide

The present invention relates to a gaseous hydrogen sulfide treatment method, and more particularly to a method that can effectively treat gaseous hydrogen sulfide.

Gaseous hydrogen sulphide occurs in apartment septic tanks and sewer pipes, causing odor problems. In particular, it has a bad effect on the surrounding living environment as it occurs in the city center's restaurant area and apartment sewer line.

As a gaseous hydrogen sulfide treatment technology, Korean Patent No. 10-0653046 discloses a method of removing hydrogen sulfide by using iron hydroxide, zinc hydroxide, and iron as a catalyst.

Meanwhile, a method of treating air pollutants by generating plasma and accelerating electrons by a high electric field to oxidize and reduce molecules in a gas is known. Such a method is to oxidize and reduce molecules by forming a high electric field around the electrode by the high voltage applied to the discharge electrode at atmospheric pressure. Since the reaction using the plasma shows different results depending on the object to be treated and the operating conditions in the same reactor, it is difficult to predict the result.

In addition, even in the case of treating air pollutants using a catalyst, the function and performance of the catalyst vary depending on the type of material, carrier, and catalyst to be treated, and thus it is not easy to predict the result.

Republic of Korea Patent No. 10-0653046, Dec. 1, 2006, Summary

The problem to be solved by the present invention is to provide a method for effectively treating gaseous hydrogen sulfide.

Hereinafter, other technical problems not mentioned in the above technical problem will be clearly understood by those skilled in the art from the following description.

Gas phase hydrogen sulfide treatment method according to an embodiment of the present invention (A) the gas inlet and gas outflow consisting of a receiving portion that can accommodate the discharge electrode and the carrier on which the catalyst is carried, and the open portion formed at one end and the other end, respectively Reactor body comprising a portion, and made of a dielectric material; A discharge electrode accommodated in the accommodating part and disposed to be in contact with an inner surface of the reactor body; An external electrode disposed in contact with the outside of the reactor body; A ground part having one end connected to the external electrode; A power supply unit supplying power to the discharge electrode; At least one carrier selected from aluminum oxide (Al ₂ O ₃ ) or zeolite contained in the receiving part and supported with at least one catalyst selected from silver, copper or manganese; And a heat-resistant support part formed at each of the gas inlet side and the gas outlet side of the accommodation part to close the accommodation part, wherein the gas passage passes through the carrier and has a pore diameter that does not pass through the carrier. Preparing; (B) supplying power to the discharge electrode of step (A); And (C) passing gaseous hydrogen sulfide through the receiving portion of step (A).

The gaseous hydrogen sulfide treatment method of the present invention can effectively treat gaseous hydrogen sulfide.

1 is a flow chart showing a processing method according to an embodiment of the present invention.
2 is a view showing a gaseous hydrogen sulfide treatment apparatus used in an embodiment of the present invention.
3 is a partial cutaway view of the gaseous hydrogen sulfide treatment apparatus of FIG. 2.
4 is a view showing a modification of the gaseous hydrogen sulfide treatment apparatus used in one embodiment of the present invention.
5 is a conceptual diagram illustrating an example of a scrubber applicable to the apparatus of FIG. 4.
6 is a diagram schematically showing the configuration of an experimental apparatus applied to an experimental example of the present invention.
7 is a photograph showing an SEM surface shape analysis result of each carrier on which a catalyst is supported in an experimental example of the present invention.
FIG. 8 is a graph showing a change in concentration of hydrogen sulfide and its product dioxide dioxide in the effluent gas for each elapsed time in an experimental example of the present invention.
FIG. 9 is a graph showing hydrogen sulfide removal rate according to a change in specific energy when the carrier is gamma-Al ₂ O ₃ in one experimental example of the present invention.
10 is a graph showing the hydrogen sulfide removal rate according to the change in non-energy energy when the carrier is beta-zeolite in one experimental example of the present invention.
11 is a graph showing the hydrogen sulfide removal rate according to the change in space velocity and specific input energy in an experimental example of the present invention.

Advantages and features of the present invention and methods for accomplishing the same will be apparent with reference to the embodiments and experimental examples described below in detail together with the accompanying drawings. However, the present invention is not limited to the embodiments and experimental examples disclosed below, but may be embodied in various different forms, only the present examples and experimental examples are provided so that the disclosure of the present invention is complete, and the present invention belongs to It is provided to fully inform the person skilled in the art the scope of the invention, which is only defined by the claims. Unless otherwise stated throughout the specification, the same reference numerals refer to the same components, and the words used in the singular are intended to include the plural unless otherwise indicated. In the present invention, 'treatment' is meant to include the removal, reduction or conversion of the material to other forms.

Hereinafter, an embodiment of the present invention will be described in detail with reference to FIG. 1.

1 is a flow chart showing a processing method according to an embodiment of the present invention.

As shown in the flowchart of FIG. 1, the gaseous hydrogen sulfide treating method according to an embodiment of the present invention includes (A) preparing a gaseous hydrogen sulfide treating apparatus; (B) power supply step; And (C) passing gaseous hydrogen sulfide. In addition, (D) may further comprise a post-treatment step. Steps (B) and (C) may be performed simultaneously or in a reverse order regardless of the order.

Hereinafter, an example of the gaseous hydrogen sulfide treatment apparatus of step (A) will be described in detail with reference to FIGS. 2 to 3.

FIG. 2 is a view showing an external appearance of a gaseous hydrogen sulfide treatment apparatus that can be used in an embodiment of the present invention, and FIG.

An example of the gaseous hydrogen sulfide processing apparatus 100 includes a reactor body 10, a discharge electrode 40, an external electrode 60, a grounding part 70, a power supply part 80, a carrier 50 carrying a catalyst, And heat resistant supports 20 and 30.

The reaction body 10 includes a gas inlet part 11 and a gas outlet part including an accommodating part 15 capable of accommodating a carrier carrying a discharge electrode and a catalyst therein, and an opening part formed at one end and the other end thereof, respectively. Including, gaseous hydrogen sulfide may flow in the direction of the arrow to flow through the receiving portion. The reaction base 10 is made of a dielectric substance, and the dielectric substance is not limited to this as long as it is a substance that generates electric polarization but no direct current when applying an electrostatic field. , Paraffin, ceramic, glass, and preferably an insulator such as borosilicate glass (trade name pyrex glass), and / or quartz, preferably borosilicate glass.

The discharge electrode 40 is accommodated in the accommodating part 15, and a part of the discharge electrode 40 is disposed to be in contact with the inner surface of the reactor body 10, and the outer electrode 60 is disposed to be in contact with the outer surface of the reactor body. . The discharge electrode 40 and the external electrode 60 are separated by the reactor body 10 made of a dielectric material, so that direct discharge does not occur between both electrodes and charge buildup of the dielectric material occurs when an alternating voltage is applied. -Up) can maximize the voltage efficiency applied by AC power. As a result, a dielectric barrier discharge occurs to generate electrons, and various reactive species are generated through atmospheric gases (nitrogen, oxygen, carbon dioxide, etc.) and dissociation, electron collision, ionization, excitation process, and radical reaction.

The discharge electrode 40 or the external electrode 60 is not limited to this as long as it is a conductive electrode. Preferably, the discharge electrode is a tungsten wire, and the external electrode may be an aluminum plate. The discharge electrode 40 may be all or part of the spiral shape, and the external electrode 60 is in contact with the outer surface of the reactor body 10 to surround the outer periphery, so that the discharge can occur more effectively. . In addition, the external electrode 60 may be grounded by connecting one end of the ground portion 70 made of a conductive wire mainly composed of copper, graphite, carbon, or the like. It is possible to increase the contact area with the catalyst by making the discharge electrode 40 spiral. As a result, the combined effect of the catalyst and the plasma can be increased.

The power supply unit 80 supplies power to the discharge electrode 40, and one end of the discharge electrode 40 and a ground part 70 of which the part is exposed to the outside of the receiving unit 15 by wires 83 and 85. It can be connected to the side to form a circuit. The power supply unit may be a high voltage AC power supply device. The high voltage AC power supply may have an applied voltage of 0 to 18 kV. Although not limited by this by the power supply unit 80, the power can be supplied so that the non-input energy is 1.0 ~ 1.8 Wh / m ³ .

The carrier 50 is one or more selected from aluminum oxide (Al ₂ O ₃ ) or zeolite carrying at least one catalyst selected from silver, copper or manganese, and is accommodated in the accommodating part 15 to pass through the accommodating part. It is believed that the gaseous hydrogen sulfide is treated with the plasma. The carrier 50 is composed of a plurality of spherical carriers. As a result, the discharge electrode 40 is surrounded by the carrier 50 and effectively discharges on the surface of the catalyst on the carrier. Therefore, it is determined that hydrogen sulfide can be more effectively treated. The carrier may preferably be a zeolite carrying one or more catalysts selected from silver, copper or manganese, and the zeolite may be preferably beta-zeolite. In addition, the catalyst may preferably be silver. The carrier may be beta-zeolite impregnated and supported to have a content of 3 to 8% by weight, preferably 5% by weight of silver.

The heat resistant support parts 20 and 30 are formed at gas inlet side and gas outlet side ends of the accommodating part 15 to close the accommodating part 15, but gas passes through the carrier 50. And through holes 25 and 35. The heat resistant support part may be a pair of support plates respectively formed at the gas inlet side end and the gas outlet side end. The heat resistant support parts 20 and 30 may support the carrier 50 to be maintained in the accommodating part 15 to selectively remove gaseous hydrogen sulfide from the accommodating part 15. As a result, gaseous hydrogen sulfide can be effectively treated. The heat resistant support parts 20 and 30 may be coupled to the reactor body by fitting or the like, and may be removable. The heat resistant support parts 20 and 30 may be made of a heat resistant material, and the heat resistant material may be heat-resistant plastic such as aromatic polyamide, polyimide, polyimida sol pyrrolone, polybenzoimidazole, and / or polyphenylene oxide. And / or cotton, paper, polyethylene, polyvinyl chloride, natural rubber, polyester, epoxy resin, melamine resin, phenol resin, polyurethane, mica, asbestos, glass fiber, and the like. The heat resistant support parts 20 and 30 may be made of an insulator.

Since the support parts 20 and 30 are made of a heat resistant material, the support parts 20 and 30 may play an original role without being deformed by heat that may occur during discharge. The heat resistant material refers to a material that is physically stable under high temperature, preferably a material whose mechanical strength is maintained at 300 to 600 degrees Celsius (in air).

In order to allow the gaseous hydrogen sulfide to pass smoothly through the receiving part 15, a blower may be installed at the front and / or rear ends of the reactor body 10.

Step (B) is a step of supplying power to the discharge electrode of the step (A), it can be supplied to the high voltage AC power supply. Although not limited to this, Preferably, the power can be supplied such that the specific input energy is 1.0 to 1.8 Wh / m ³ . In the non-energy, and it is concerned with compared to one 1.8Wh / m ³ in excess of the throughput is too inefficient energy input, there is a concern that insufficient throughput in 1.0Wh / m ³ or less. The non-injection energy may be based on a gaseous hydrogen sulfide treatment having an average concentration occurring in a conventional sewer.

Step (C) is a step of passing the gaseous hydrogen sulfide through the receiving portion of the step (A), the space velocity during the passage is not limited thereto, but preferably It can be 35,000 ~ 65,000hr ^-1 . If the space speed is less than 35,000Hr ^-1 , there is a fear that the increase in throughput due to the decrease in space speed is not large, and if the space speed is greater than 65,000Hr ^-1 , the throughput may be insufficient. The space velocity may be based on gaseous hydrogen sulfide treatment of an average concentration occurring in a conventional sewer.

The space velocity is the inverse of the residence time and the residence time is a function of the amount of catalyst and the flow rate. The space velocity can be calculated by the following equation.

Space Velocity (SV) (hr ^-1 ) = Process Gas Flow (m ³ / hr) ÷ Catalyst Volume (m ³ )

The post-treatment step (D) may be a step of post-treatment of the gas passing through the receiving part of the step (C) with a scrubber. In the post-treatment step, sulfur dioxide converted to hydrogen sulfide can be easily removed.

Hereinafter, with reference to (D) the post-treatment step, a modification of the gaseous hydrogen sulfide treatment apparatus applicable to one embodiment of the present invention will be described in detail with reference to FIGS. 4 to 5. Unless otherwise stated, the contents mentioned in the gaseous hydrogen sulfide treatment apparatus applicable to one embodiment of the present invention are equally applicable to the modification of the gaseous hydrogen sulfide treatment apparatus applicable to one embodiment of the present invention, unless there is a contradiction. .

4 is a view showing a modification of the gaseous hydrogen sulfide treatment apparatus applicable to an embodiment of the present invention, Figure 5 is a conceptual diagram showing an example of a scrubber applicable to the apparatus of FIG.

Referring to FIG. 4, a modification of the gaseous hydrogen sulfide treatment apparatus applicable to an embodiment of the present invention is provided at the rear end of the gaseous hydrogen sulfide treatment reactor 110 of the same type as the gaseous hydrogen sulfide treatment reactor applicable to an embodiment of the present invention. By installing the sulfur dioxide treatment scrubber 200, gaseous hydrogen sulfide flows into the reactor 110, it is possible to easily process the converted sulfur dioxide. Since sulfur dioxide is more soluble in water than hydrogen sulfide, it can be easily processed using a scrubber. As a result, gaseous hydrogen sulfide can be effectively treated. The scrubber 200 may be a known scrubber.

An operation of the scrubber will be described with reference to FIG. 5 as follows. As shown in FIG. 5, the scrubber is provided with a nozzle unit 240 at an upper end of a housing 210 in which water is stored at a lower end of the scrubber, and the water is stored in the nozzle unit using a pump or the like by a pipe 250. 240 is injected into the sulfur dioxide-containing gas introduced into the housing 210 through the inlet pipe 220. Since sulfur dioxide is water-soluble, it is dissolved by the sprayed water and falls down, and the hydrogen sulfide as well as the gas removed up to sulfur dioxide are discharged to the outside through the outlet pipe 230. The blower 300 may be disposed at the rear end of the scrubber 200 to allow the hydrogen sulfide removal gas to flow out.

<Experimental Example>

1. Composition of Experiment Device

The experimental apparatus was configured as shown in FIG. Hydrogen sulfide treatment reactor was used in the same manner as the apparatus shown in Figs.

As the reactor body, borosilicate glass (trade name pyrex glass) tubes having an internal diameter of 46 mm and a length of 120 mm were used. Both ends of the tube were inserted into a heat-resistant plastic disc (46 mm in diameter) of porous (pore diameter 0.0001-2 mm) to form an accommodating part. The discharge rod used a tungsten wire having a diameter of 1mm, and used an aluminum foil as the external electrode. As a power supply device for generating plasma, a 360W high voltage AC power supply (applied voltage: 0-18 kV and frequency: 60 Hz) was used. The carrier on which the catalyst was supported was accommodated in the receiving portion.

Gas generator is a device for generating a hydrogen sulfide gas of a constant concentration for the experiment, and includes a hydrogen sulfide cylinder, a mass flow regulator, a chamber. The hydrogen sulfide gas of Bombe was injected and diluted in a chamber in a state in which the injection amount was controlled by a mass flow controller (MFC) to maintain a concentration of about 5 ppm of hydrogen sulfide. The hydrogen sulfide concentration is an average concentration of gaseous hydrogen sulfide generated from a conventional sewer.

After the hydrogen sulfide treatment reactor, a blower was connected to blow the treated gas.

The analysis unit includes equipment for measuring the hydrogen sulfide concentration at the front and rear of the reactor, and was used in the US Odalog L2 H2S-50 of APP-Tek, and the instrument was calibrated from time to time using a standard gas (H2S 31.6ppm).

Sulfur dioxide was measured with a gastec detector (GASTEC, GV-100s, Japan) and a detector tube (GASTEC, 0.05-10 ppm measurement range, SO ₂ 5Lb).

AC voltage was measured by connecting a high voltage probe (Tektronix, P6015A, USA) connected to the power supply to a digital oscilloscope (Tektronix, TDS2014B, USA).

The energy used was measured using an integrated power meter and converted to SIE. Specific input energy is defined as the ratio of input power to the flow rate of the processing gas as follows.

Specific input energy (Wh / m ³ ) = Input power (W) ÷ Process gas flow rate (m ³ / hr)

2. Preparation of Supported Carrier

As a carrier, spherical gamma-Al ₂ O ₃ (414069, Sigma-Aldrich, USA) and beta-zeolite (H type, Cosmo chemical, Korea) with a diameter of 3 to 4 mm were used, and washed for about 1 hour in 0.5M hydrochloric acid solution. And washed again with secondary distilled water. It was calcined for 4 hours in an air atmosphere of about 450 degrees Celsius to remove impurities and activate. The transition metal precursors (AgNO ₃ , CuNO ₃ , MnCl ₂ ) were dispersed in distilled water so that the impregnated content of the transition metals (Ag, Cu, Mn) was 5 wt% based on the unit mass of the carrier, and the solution was added to the active carrier at room temperature. After 30 minutes of stirring at 50 ° C vacuum evaporator was evaporated for 2 hours. The dried catalyst was placed in a glass bottle and the inlet was covered with aluminum foil to dry at about 105 degrees Celsius for 24 hours, and the prepared catalyst was calcined for about 19 hours in an air atmosphere of 500 degrees Celsius.

Physical properties of the prepared catalyst were measured by using a BET specific surface area measuring instrument (BELSORP-mini, BEL, Japan), SEM (Scanning electronic microscope; JEOL, JSM-5600, Japan), EDX (Energy dispersive X- ray; Noran, Noran SII-1609, USA) The specific surface area was measured using BET (BELSORP-mini, BEL, Japan), SEM (JEOL, JSM-5600, Japan), EDX (Noran, Noran SII-1609, USA, surface shape and component analysis.

SEM surface shape analysis results of the carrier on which the catalyst is supported are shown in FIG. 7.

As shown in FIG. 7, the shape of the crystal phase of the carrier is almost similar, but it can be seen that the pores vary according to the type of transition metal. This is not because the basic structure of the carrier is changed, but because the transition metal is impregnated to affect the pore structure.

In addition, the specific surface area for each carrier on which the catalyst is supported is shown in Table 1 below.

Catalyst / carrier

Specific surface area (m ² / g)
Ag / gamma-Al ₂ O ₃

291
Cu / Gamma-Al ₂ O ₃

208
Mn / gamma-Al ₂ O ₃

200
Ag / beta-zeolite

480
Cu / beta-zeolite

462
Mn / beta-zeolite

403

Considering that the specific surface area of the carrier suggested by the manufacturer was gamma-Al ₂ O ₃ of 315 m ² / g and beta-zeolite of 550 m ² / g, the specific surface area of the catalyst loading decreased. It can be seen that the specific surface area also changes depending on the type of catalyst and carrier. As can be seen in the microstructure shown in FIG. 6, it is determined that the transition metal is impregnated into the carrier to change the pore structure.

In addition, EDX component analysis confirmed that the support of the catalyst prepared by the impregnation method by 5wt%.

3. Experimental conditions

Hydrogen sulfide treatment experiment was carried out under the conditions as shown in Table 2, using a carrier prepared with a catalyst prepared above.

Item

Figures or substances
Hydrogen sulfide inflow concentration (ppm)

5
Space velocity (hr ^-1 )

30,000-90,000
Specific input energy (Wh / m ³ )

0.15-1.8
carrier

Gamma-Al ₂ O ₃ , beta-zeolite
catalyst

Ag, Cu, Mn
Catalyst supported carrier amount (g)

40-100

4. Experimental results

4.1 Confirmation of hydrogen sulfide treatment effect over time

When hydrogen sulfide is removed using the catalyst and the plasma simultaneously, the adsorption and the removal by the plasma are simultaneously performed. Since hydrogen sulfide is adsorbed at the beginning of the reaction, the concentration is low at the outlet of the reactor, making it difficult to grasp the influence of plasma. Therefore, experiments were performed after adsorbing hydrogen sulfide for about 20 minutes to show the combined effect of catalyst-plasma. 8 is a graph showing the concentration change of hydrogen sulfide and its product sulfur dioxide in the effluent gas over time. The results of FIG. 8 are the results under the conditions of a space velocity of 60,000 hr ⁻¹ and specific input energy of 1.2 Wh / m ³ using a silver-supported beta-zeolite catalyst.

As shown in FIG. 8, 5 ppm of hydrogen sulfide was introduced into the reactor and initially adsorbed by a catalyst, and then passed through about 20 minutes, and it was found that the outlet concentration was equal to the inlet concentration. It can be seen that by driving, the concentration of hydrogen sulfide is drastically reduced and the concentration of sulfur dioxide is drastically increased by the catalyst-plasma reaction.

The process of the present invention results in the conversion of hydrogen sulfide to sulfur dioxide, which is more soluble in water. The converted sulfur dioxide can be easily removed using a wet scrubber or the like. As a result, it can be said that there is an advantage of the present invention in that hydrogen sulfide, which is not easily treated, can be converted into sulfur dioxide, which is easier to treat.

4.2 Confirmation of hydrogen sulfide treatment effect by catalyst and carrier

By changing the specific input energy, the treatment efficiency according to the catalyst and the carrier was measured at a space velocity of 60,000 hr ⁻¹ , and the results are shown in FIGS. 9 and 10. In addition, for comparison, the results for the carrier alone (γ-Al ₂ O ₃ ), the same experiment for the case of using only the plasma (Plasma w / o catalyst) without using both the catalyst and the carrier, the results are shown in Figure 9 and It is shown together in FIG.

9 is a graph showing the hydrogen sulfide removal rate according to the non-injection energy change when the carrier is gamma-Al ₂ O ₃ , and FIG. 10 is a graph showing the hydrogen sulfide removal rate according to the non-injection energy change when the carrier is beta-zeolite.

As shown in FIG. 9 and FIG. 10, when the catalyst-plasma is used, the treatment efficiency is significantly higher than that of the single plasma reaction. It is determined that the active molecules and radicals generated by the plasma have a great influence on the activation of the catalyst. In addition, beta-zeolite appears to have a higher than the hydrogen sulfide removal efficiency when using the gamma -Al ₂ O _3, which zeolite is gamma -Al ₂ O ₃ It is believed that this is because active radicals are easily adsorbed and oxidized in treating hydrogen sulfide with a larger surface area.

In addition, it can be seen that the removal efficiency varies depending on the type of metal catalyst. Both carriers show high efficiency of Ag, and Mn and Cu are shown in the order.

In particular, as shown in FIG. 10, it can be seen that the beta-zeolite support on which silver is supported exhibits a significantly high throughput even at a relatively low specific input energy (see arrowed portion in FIG. 9). From these results, it can be seen that in the hydrogen sulfide treatment, the beta-zeolite carrier on which silver is supported shows an excellent effect.

4.3 Checking the effect of hydrogen sulfide treatment on the variation of space velocity and specific input energy

The conversion of the reactants is affected by the residence time in the catalyst bed, where the residence time is a function of the amount and flow rate of the catalyst, and the space velocity, which is the inverse of the residence time, is mainly used to explain the residence time of the reactants in the catalyst bed.

For the 5wt% Ag / beta-zeolite catalyst that showed the highest H ₂ S removal efficiency, change the amount of catalyst under constant flow rate to determine the relationship between its activity and space velocity. After setting to 45000, 65000, 90000 hr ^-1 , the treatment efficiency according to the specific input energy (0.3, 0.7, 1.0, 1.3, 1.8 Wh / m ³ ) was measured. In addition, the results are shown in FIG.

11 is a graph showing the hydrogen sulfide removal rate according to the change in space velocity and specific input energy. As shown in Fig. 11, the removal rate tends to increase as the space velocity is smaller and as the specific energy is increased. In the range of space velocity 35,000 ~ 65,000hr ^-1 and specific energy 1.0 ~ 1.8Wh / m ³ , the removal rate is over 60%, which shows the superior effect. It can be seen that gas phase hydrogen sulfide can be more effectively treated under the above operating conditions because the change in throughput is largely expressed in and out of the above range. In particular, the space velocity of 35,000 ~ 65,000hr ^-1 , the specific input energy 1.8Wh / m ³ can be seen that the treatment rate is 100%, showing a particularly excellent effect.

It is understood from the results of 4.1 to 4.3 that the gaseous hydrogen sulfide can be effectively treated by the method of the present invention.

10: reactor body 11: gas inlet
13: gas outlet 15: receiver
20, 30: support portion 25: through hole
40: discharge electrode 60: external electrode
70: ground portion 80: power supply portion
83, 85: wire 100: gaseous hydrogen sulfide treatment device
110: gas phase hydrogen sulfide treatment reactor
200: scrubber 210: housing
220: inlet pipe 230: outlet pipe
240: nozzle 250: pipeline
300: blower

Claims (12)

(A) a reactor body including a gas inlet and a gas outlet comprising an accommodating part capable of accommodating a carrier carrying a discharge electrode and a catalyst therein, and openings formed at one end and the other end thereof, respectively; A discharge electrode accommodated in the accommodating part and disposed to be in contact with an inner surface of the reactor body; An external electrode disposed in contact with the outside of the reactor body; A ground part having one end connected to the external electrode; A power supply unit supplying power to the discharge electrode; At least one carrier selected from aluminum oxide (Al ₂ O ₃ ) or zeolite contained in the receiving part and supported with at least one catalyst selected from silver, copper or manganese; And a heat-resistant support part formed at each of the gas inlet side and the gas outlet side of the accommodation part to close the accommodation part, wherein the gas passage passes through the carrier and has a pore diameter that does not pass through the carrier. Preparing;
(B) supplying power to the discharge electrode of step (A); And
(C) gas-phase hydrogen sulfide treatment method comprising the step of passing the gaseous hydrogen sulfide through the receiving portion of step (A). The gas phase hydrogen sulfide treatment method according to claim 1, wherein the power supply of step (B) is supplied at a specific input energy of 1.0 to 1.8 Wh / m ³ . The gas phase hydrogen sulfide treatment method according to claim 2, wherein the specific input energy is a gaseous hydrogen sulfide treatment standard having an average concentration occurring in the sewer. The gas phase hydrogen sulfide treatment method according to claim 1, wherein the passage of step (C) is a passage at a space velocity of 35,000 to 65,000 hr ⁻¹ . The gas phase hydrogen sulfide treatment method according to claim 4, wherein the space velocity is a gaseous hydrogen sulfide treatment standard having an average concentration occurring in the sewer. The gas phase hydrogen sulfide treatment method according to claim 1, further comprising a post-treatment step of post-treating the gas passing through the receiving portion of step (C) with a sulfur dioxide treatment scrubber. The gas phase hydrogen sulfide treatment method according to claim 1, wherein the discharge electrode is partially or entirely spiraled. The gas phase hydrogen sulfide treatment method according to claim 1, wherein the carrier is a plurality of spherical carriers, and the discharge electrode is surrounded by the carrier. The gas phase hydrogen sulfide treatment method of claim 1, wherein the carrier is a zeolite carrying at least one catalyst selected from silver, copper or manganese. 10. The method of claim 9, wherein the catalyst is silver. The gas phase hydrogen sulfide treatment method according to claim 10, wherein the carrier is beta-zeolite impregnated so as to have a content of 3 to 8% by weight of silver. The gas phase hydrogen sulfide treatment method according to claim 11, wherein the carrier is beta-zeolite impregnated so as to have a content of 5% by weight of silver.

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