PROCESS FOR THE DENITRATION OF EXHAUST GASES WITH HEAT TREATED ACTIVATED CARBON

Description

Technical Field

[0001] This invention relates to the removal of nitrogen oxides present in combustion exhaust gases discharged from boilers, engines, turbines and the like, and more particularly to an exhaust gas denitration technique in which cold to hot nitrogen oxides can be efficiently reduced and thereby decomposed to nitrogen and water.

[0002] This invention is especially suitable for the denitration of cold exhaust gases discharged from the outlets of existing exhaust gas denitration apparatus, boilers and the like.

[0003] Moreover, this invention also relates to the removal of nitrogen oxides present in ventilation gases produced in road tunnels, underground parking spaces, street crossings and the like, and more particularly to a low-temperature denitration technique in which nitrogen oxides having a lower concentration (typically about 15 ppm or less) and a low temperature (typically ordinary temperature to about 50°C) as compared with exhaust gases from boilers and the like can be efficiently reduced and thereby decomposed to nitrogen and water.

[0004] The present invention can be suitably used for the removal of nitrogen oxides present in tunnels and for the removal of nitrogen oxides present in exhaust gases from nitric acid production plants.

Background Art

[0005] For the denitration of exhaust gases from stationary nitrogen oxide-producing sources such as boilers, a method for reducing nitrogen oxides selectively by using vanadium oxide as a catalyst and ammonia as a reducing agent (i.e., the SCR method) has conventionally been known and is widely employed for practical purposes ("Techniques and Regulations for the Prevention of Environmental Pollution", Volume on the Atmosphere, p. 130, Maruzen Co., Ltd.). However, in this method using the vanadium oxide catalyst, the temperature of exhaust gas needs to be raised to 300°C or above in order to achieve a practically sufficient degree of denitration. Consequently, it is necessary to install a denitrator containing a catalyst bed in the high-temperature section of the boiler (e.g., just behind the outlet of the boiler or in the heat transfer section of the boiler), or reheat cold exhaust gas and thereby raise its temperature. However, these techniques involve the following problems.

[0006] When the denitrator is installed in the high-temperature section of the boiler, various problems arise in that the overall equipment becomes complicated, the use of a heat-resisting material causes an increase in equipment cost, and workability for replacement of the catalyst bed is reduced. When cold exhaust gas is reheated, an additional heater is required, resulting in an increase in equipment cost.

[0007] Accordingly, a first object of the present invention is to provide a technique by which the denitration of exhaust gases from stationary nitrogen oxide-producing sources such as boilers can be performed at low temperatures ranging from ordinary temperature (about 5 to 20°C) to about 150°C.

[0008] On the other hand, exhaust gases from road tunnels are characterized in that they have a much lower NO concentration of about 10 ppm or less as compared with the concentration of nitrogen oxides in exhaust gases from boilers, their temperature is in the vicinity of ordinary temperature, and they are produced in enormous volumes. Consequently, in order to remove denitrate gases from road tunnels according to the conventional SCR method, the temperature of the gases must be raised to 300°C or above. This requires a huge amount of thermal energy and is unprofitable from an economical point of view.

[0009] In Japanese Patent Publication No. 41142/'95 and Japanese Patent Provisional Publication No 47227/'95 there has been proposed a process in which low concentration NO at ordinary temperature is oxidised to NO₂ with ozone, the resulting NO₂ is adsorbed to an adsorbent, and the highly concentrated NO₂ is decomposed by treatment with a reducing gas such as ammonia. However, in this process involving an adsorption step, not only the equipment is increased in size and becomes complicated, but also the use of ozone poses a new safety problem. Thus, it is difficult to put this process to practical use.

[0010] Accordingly, a second object of the present invention is to provide a technique by which NO present in exhaust gases from road tunnels, and hence having a low concentration and a temperature in the vicinity of ordinary temperature can be directly reacted catalytically with ammonia and thereby decomposed to nitrogen and water.

[0011] JP 54-064091 discloses the use of an acrylonitrile fibre which has been subjected to an oxidation treatment and an activation treatment as an adsorbent for the removal of nitrogen oxides. The fibre is treated at 200 to 300°C in an oxidative atmosphere and then activated by further treatment at 700 to 1000°C with, inter alia, water vapour, carbon dioxide and ammonia. Clearly, the requirement for the activation treatment after the oxidation treatment introduced additional complexity and cost into the process.

[0012] JP 06-079176 teaches the preparation of an active carbon fibre catalyst for use in the reduction of nitrogen monoxide with ammonia and the removal of nitrogen monoxide. The active carbon fibre catalyst is prepared by baking active carbon fibre in a non-oxidising atmosphere at 600 to 1200°C and then subjecting the baked fibre to an activation treatment using sulphuric acid. Again, the process suffers from the requirement to perform an additional treatment, utilising hazardous sulphuric acid, following the baking treatment.

[0013] Now, an example of exhaust gas treatment by means of a conventional exhaust gas treating system is explained with reference to FIG. 7.

[0014] In FIG. 7, reference numeral 41 designates a boiler; 42, a denitrator; 43, an air preheater; 44, a dust collector; 45, a gas-gas heater; 46, a desulfurizer; and 47, a stack.

[0015] As shown in FIG. 7, a denitrator 42 using a catalyst is installed at the outlet of a boiler 41 in order to remove nitrogen oxides (NO_x) present in the exhaust gas, and an air preheater 43 is installed at the outlet of denitrator 42 in order to lower the temperature of the exhaust gas to about 130°C.

[0016] The exhaust gas having passed through the aforesaid air preheater 43 is dedusted in a dust collector 44, passed through a gas-gas heater 45 and then introduced into a desulfurizer 46 where sulfur oxides (SO_x) are removed therefrom. Thereafter, the exhaust gas is discharged into the atmosphere through a stack 47.

[0017] As described above, in the current practical process for the removal of nitrogen oxides present in exhaust gas from boilers, there is used a denitrator 42 based on the selective catalytic reduction (SCR) method in which nitrogen oxides are decomposed to nitrogen and water vapor by using a catalyst comprising V₂O₅ supported on TiO₂ and a reducing agent comprising NH₃. However, this process involves the following problems.

[0018] First, a reaction temperature of 300 to 400°C is required because of the performance of the catalyst. Secondly, NH₃ is required for use as reducing agent. Thirdly, since the current leak level of NO_x is from 5 to 40 ppm, an excess of NH₃ needs to be injected for the purpose of reducing the leak level of NO_x to zero.

[0019] Moreover, recent environmental standards demand that the concentration of nitrogen oxides (NO_x) in exhaust gases should be reduced to a level of 1 ppm or less which is commonly known as a high-degree denitration level. In the aforesaid conventional denitration treatment based on the selective catalytic reduction (SCR) method, a marked increase in removal cost due to an increased size of equipment is unavoidable, even though the conditions are optimized. On the other hand, it is desired from the viewpoint of environmental problems to improve the efficiency of removal of nitrogen oxides.

[0020] Accordingly, in view of the above-described problems, a third object of the present invention is to provide a denitration system which can achieve an improvement in the efficiency of removal of nitrogen oxides present in exhaust gases as compared with the prior art.

Disclosure of the Invention

[0021] The present inventors have carried out investigations with a view to accomplishing the above-described first and second objects, and have now found that, when an active carbon having a large specific surface area and high porosity (in particular, one obtained by heat-treating active carbon fibers or a granular active carbon having a large number of fine micropores with a size of 20 Å or less under specific conditions) is used as a catalyst for the denitration reaction of exhaust gas, a high degree of denitration can be achieved even at low temperatures of 150°C or below. Moreover, they have also found that a high degree of denitration can be achieved even when exhaust gas having a low NO concentration is treated in the vicinity of ordinary temperature.

[0022] That is, the present invention provides the following technique concerning the denitration of exhaust gas. Specifically, the present invention provides a selective catalytic reduction method for the denitration of exhaust gases which consists of the steps of:

(a) heat treating raw active carbon fibres having a pore diameter of 10 to 30 Å, a pore volume of 0.3 to 1.2 ml/g and a specific surface area of 500 to 2000 m²/g at 600 to 1200°C in a non-oxidising atmosphere such that the heat treated active carbon has micropores with a size of 20Å or less and an atomic surface oxygen to surface carbon ratio of 0.05 or less; and

(b) bringing exhaust gas containing 500 ppm or less of nitrogen oxides, 3% or more of oxygen and not more than 80% of water as water vapour and ammonia gas having the same concentration as the nitrogen oxides into contact, at a temperature of 100°C or below, with said heat treated active carbon from step a), as such.

[0023] The present invention also provides the denitration method wherein a higher degree of denitration of nitrogen oxides having a temperature of 20 to 150°C and a concentration of 5 to 400 ppm is performed at the outlet of an exhaust gas treating apparatus or the outlet of a boiler.

[0024] In order to accomplish the above-described third object, a first denitration system using active carbon in accordance with the present invention comprises a first packed reactor which is packed with a heat-treated active carbon produced by heat-treating a rsw active carbon at a temperature in the range of 600 to 1,000°C, and a second packed reactor which is located downstream thereof and packed with the heat-treated active carbon, whereby exhaust gas and ammonia (NH₃) are introduced into the first packed reactor so as to bring nitrogen oxides (NO_x) present in the exhaust gas into contact with the ammonia and remove the nitrogen oxides by the continuous selective reduction of them to nitrogen (N₂), and any excess ammonia is recovered by adsorption in the second packed reactor.

[0025] In the aforesaid denitration system, a gas to be treated can be alternately introduced into the first packed reactor and the second packed reactor so as to perform denitration and ammonia adsorption repeatedly.

[0026] In order to accomplish the above-described third object, a second denitration system using active carbon in accordance with the present invention comprises a denitrator packed with a heat-treated active carbon which is produced by heat-treating a raw active carbon at a temperature in the range of 600 to 1,000°C, and first and second ammonia adsorbers located before and behind the denitrator, respectively, whereby exhaust gas containing nitrogen oxides is alternately introduced through any one of the first and second ammonia adsorbers, ammonia (NH₃) is introduced at a position between the first or second ammonia adsorber and the denitrator, nitrogen oxides (NO_x) present in the exhaust gas are brought into contact with the heat-treated active carbon placed in the denitrator and removed by the continuous selective reduction of them to nitrogen (N₂), and any excess ammonia is recovered by adsorption in the adsorber located downstream of the denitrator.

[0027] In the aforesaid denitration systems, the raw active carbon fibers preferably comprise carbon fibers derived from polyacrylonitrile or pitch.

[0028] The heat-treated active carbon of the present invention is highly effective as a catalyst for the denitration of exhaust gas. More specifically, when the heat-treated active carbon of the present invention is used for purposes of denitration, exhaust gases containing nitrogen oxides at low to high concentrations (about 20 to 500 ppm) can be denitrated at a low temperature ranging from ordinary temperature to about 100°C and with a high degree of denitration of about 40 to 80%.

[0029] Especially when active carbon fibers derived from pitch are used, excellent denitration performance can be achieved even under a high partial pressure of water vapor.

[0030] Moreover, when the heat-treated active carbon of the present invention is used, gases containing nitrogen oxides at a low concentration of 15 ppm or less can be denitrated at a low temperature ranging from ordinary temperature to about 50°C and with a high degree of denitration of about 40 to 80%, without oxidizing NO to NO₂ by means of ozone, electron rays or the like, or without concentrating nitrogen oxides by means of an adsorbent. Especially when active carbon fibers derived from pitch are used, excellent denitration performance can be achieved even under a high partial pressure of water vapor.

[0031] In the denitration systems of the present invention wherein the treatment of gases containing nitrogen oxides is performed by using an active carbon heat-treated under specific conditions as an ammonia adsorbent, low-concentration nitrogen oxides (NO_x) can be treated and, therefore, a higher degree of denitration can be achieved.

Brief Description of the Drawings

[0032] 

FIG. 1 is a schematic diagram showing the denitration reaction mechanism at the surfaces of an active carbon modified by the process of the present invention;

FIG. 2 is a schematic illustration of a first embodiment of the denitration system in accordance with the present invention;

FIG. 3 is a schematic illustration of a second embodiment of the denitration system in accordance with the present invention;

FIG. 4 is a schematic illustration of a third embodiment of the denitration system in accordance with the present invention;

FIG. 5 is a schematic illustration of the third embodiment of the denitration system in accordance with the present invention;

FIG. 6 is a schematic illustration of the third embodiment of the denitration system in accordance with the present invention; and

FIG. 7 is a schematic illustration of a conventional denitration system.

Best Mode for Carrying Out the Invention

[0033] In this specification, all percentages are by volume unless otherwise stated. The term "non-oxidizing atmosphere" comprehends both inert gas atmospheres and reducing atmospheres. The term "ordinary temperature" means temperatures in the range of about 5 to 40°C.

[0034] The raw active carbon fibers which can be used in the present invention to produce a heat-treated active carbon for use in denitration include various types of active carbon fibers such as those derived from pitch, PAN, phenol and cellulose. Among them, active carbon fibers derived from pitch have low nitrogen and oxygen contents and enhance the effect of removing oxygen-containing functional groups present at the surfaces thereof by a heat treatment which will be described later. Accordingly, they exhibit high nitrogen oxide-removing activity even under a high partial pressure of water vapor. Thus, it is preferable to use active carbon fibers derived from pitch. Although no particular limitation is placed on the properties of the raw active carbon fibers, they usually have a pore diameter of about 10 to 30 Å, a pore volume of about 0.3 to 1.2 ml/g, and a specific surface area of about 500 to 2,000 m²/g.

[0035] In the present invention, a heat-treated active carbon which has high catalytic activity for denitration and minimizes the influence of moisture in exhaust gas can be obtained by heat-treating the raw active carbon at 600 to 1,200°C in a non-oxidizing atmosphere such as nitrogen gas, argon gas or helium gas to remove oxygen-containing functional groups (such as COOH and COH) present at the surfaces of the raw active carbon and thereby reduce the atomic oxygen/carbon ratio of the surfaces to 0.05 or less.

[0036] When the denitration of exhaust gas is performed according to the method of the present invention, exhaust gas containing nitrogen oxides at a low to high concentration (about 500 ppm or less), 3% or more of oxygen, and 0 to 80% of moisture as water vapor is brought into contact with NH₃ gas having the same concentration (or equivalent amount) as the nitrogen oxides, in the presence of the aforesaid heat-treated active carbon, at a temperature ranging from ordinary temperature (about 5 to 20°C) to about 100°C.

[0037] Thus, the nitrogen oxides are selectively reduced and thereby decomposed to nitrogen and water.

[0038] In the present invention, while the exhaust gas comes into contact with the heat-treated active carbon or passes through the heat-treated active carbon, nitrogen oxides (NO_x) present therein react with ammonia (NH₃) used as a reducing agent, as represented by the following equations, and thereby decomposed to harmless nitrogen (N₂) and water vapor (H₂O).

        4NO + 4NH₃ + O₂ -> 4N₂ + 6H₂O   (1)

        6NO₂ + 8NH₃ 7N₂ + 12H₂O   (2)

[0039] The reaction mechanism (at temperatures higher than 100°C) at the surfaces of the heat-treated active carbon, which is represented by equation (1), is shown in FIG. 1.

[0040] First of all, ammonia is adsorbed to oxidizing oxygen-containing functional groups present at the surfaces of the heat-treated active carbon, so that active species such as OH (ad.) and NH₂ (ad.) are formed. Then, NH₂ (ad.) reacts with NO and thereby reduced to N₂ and H₂O. After N₂ and H₂O are eliminated, the remaining -OH groups are oxidized by oxygen to regenerate oxidizing oxygen-containing functional groups.

[0041] The reason why these reactions proceed even at ordinary temperature is that the heat-treated active carbon has micropores with a size of 20 Å or less, and the reactants condense in the micropores and create high-pressure reactions in microscopic regions.

[0042] Usually, the above-described reactions are markedly inhibited by moisture present in the exhaust gas. This is due to the competitive adsorption of water and O₂ or NH₃. In the present invention, however, the raw active carbon is heat-treated in a non-oxidizing atmosphere to remove hydrophilic oxygen-containing groups and thereby minimize the influence of moisture in exhaust gas. Thus, a high degree of denitration can be achieved even at high humidity and low temperatures ranging from ordinary temperature to about 100°C, without any reduction in adsorption performance.

Examples

[0043] The features of the present invention are more clearly explained with reference to the following examples and comparative examples. However, these examples are not to be construed to limit the scope of the present invention.

Examples 1-9

[0044] Heat-treated active carbon fibers in accordance with the present invention were produced by heat-treating the following three types of pitch-derived raw active carbon fibers (all manufactured by Osaka Gas Co., Ltd.) at 600-1,200°C in an atmosphere of nitrogen for one hour.
OG-5A; specific surface area, 500 m²/g
OG-10A; specific surface area, 1,000 m²/g
OG-20A; specific surface area, 2,000 m²/g

[0045] 2 g each of the heat-treated active carbon fibers obtained as above were separately packed in tubular reactors (25 mm in inner diameter), and a nitrogen oxide-containing gas was passed therethrough at a temperature of 150°C and a flow rate of 400 cc/min. The nitrogen oxide-containing gas was composed of 150 ppm NO, 150 ppm NH₃, 15% O₂ and the balance N₂, and its moisture content was 80% as expressed in terms of the partial pressure of water vapor.

[0046] The effluent gas from each reactor was analyzed with a chemoluminescence type NO_x meter (ECL-88US; manufactured by Yanagimoto Seisakusho), and the degree of denitration was calculated according to the following equation.

[0047] The steady-state values obtained in a stabilized state 30 hours after the start of the reaction are shown in Table 1.

[0048] The atomic oxygen/carbon ratio at the surfaces of the active carbon fibers (hereinafter referred to as O/C) was measured with a photoelectron spectroscopic analyzer ("ESCA850"; manufactured by Shimadzu Corp.).

Comparative Examples 1-3

[0049] Instead of being heat-treated, the three types of pitch-derived raw active carbon fibers used in Examples 1-9 were directly packed in tubular reactors similar to those used in Examples 1-9, and subjected to denitration reaction in the same manner as in Examples 1-9. The results thus obtained are also shown in Table 1.

Table 1

	Type of sample	Heat-treating temperature (°C)	Degree of denitration (%)	O/C
Comparative Example 1	OG-5A	-	2	0.122
Example 1	OG-5A	600	20	0.047
Example 2	OG-5A	800	33	0.033
Example 3	OG-5A	1,000	26	0.025
Comparative Example 2	OG-10A	-	3	0.096
Example 4	OG-10A	600	22	0.050
Example 5	OG-10A	800	28	0.044
Example 6	OG-10A	1,000	25	0.023
Comparative Example 3	OG-20A	-	2	0.080
Example 7	OG-20A	600	18	0.045
Example 8	OG-20A	800	24	0.035
Example 9	OG-20A	1,000	20	0.025

[0050] It is evident from the results shown in Table 1 that the heat-treated active carbon fibers exhibit an excellent denitrating effect.

Examples 10-34

[0051] Heat-treated active carbon fibers in accordance with the present invention were produced by heat-treating the following four types of pitch-derived raw active carbon fibers (all manufactured by Osaka Gas Co., Ltd.) at 600-1,200°C in an atmosphere of nitrogen for one hour.
OG-7A; specific surface area, 700 m²/g
OG-8A; specific surface area, 800 m²/g
OG-10A; specific surface area, 1,000 m²/g
OG-20A; specific surface area, 2,000 m²/g

[0052] 2 g each of the heat-treated active carbon fibers obtained as above were separately packed in tubular reactors (25 mm in inner diameter), and a gas containing nitrogen oxide at a low concentration was passed therethrough at a temperature of 25°C and a flow rate of 400 cc/min. The nitrogen oxide-containing gas was composed of 10 ppm NO, 10 ppm NH₃, 15% O₂ and the balance N₂, and its moisture content was 0% or 80% as expressed in terms of relative humidity at 25°C.

[0053] The effluent gas from each reactor was analyzed with a chemoluminescence type NO_x meter (ECL-88US; manufactured by Yanagimoto Seisakusho), and the degree of denitration was calculated according to the following equation.

[0054] The steady-state values obtained in a stabilized state 30 hours after the start of the reaction are shown in Tables 3 to 6.

[0055] The atomic oxygen/carbon ratio at the surfaces of the active carbon fibers was measured with a photoelectron spectroscopic analyzer ("ESCA850"; manufactured by Shimadzu Corp.).

Comparative Examples 4-11

[0056] Instead of being heat-treated, the four types of pitch-derived raw active carbon fibers used in Examples 10-34 were directly packed in tubular reactors similar to those used in Examples 10-34, and subjected to denitration reaction in the same manner as in Examples 10-34. The results thus obtained are also shown in Tables 3 to 6.

Table 3

Relative humidity during reaction: 0%
	Type of sample	Heat-treating temperature (°C)	Degree of denitration (%)	Surface oxygen/ carbon
Comparative Example 4	OG-7A	-	60	0.122
Example 10	OG-7A	600	65	0.047
Example 11	OG-7A	700	66	0.042
Example 12	OG-7A	800	70	0.033
Example 13	OG-7A	850	74	0.030

Relative humidity during reaction: 80%
Comparative Example 5	OG-7A	-	8	0.122
Example 14	OG-7A	600	14	0.047
Example 15	OG-7A	700	20	0.042
Example 16	OG-7A	800	30	0.033
Example 17	OG-7A	850	39	0.030

Table 4

Relative humidity during reaction: 0%
	Type of sample	Heat-treating temperature (°C)	Degree of denitration (%)	Surface oxygen/ carbon
Comparative Example 6	OG-8A	-	58	0.115
Example 18	OG-8A	600	65	0.044
Example 19	OG-8A	700	66	0.039
Example 20	OG-8A	800	72	0.030
Example 21	OG-8A	855	75	0.027

Relative humidity during reaction: 80%
Comparative Example 7	OG-8A	-	22	0.115
Example 22	OG-8A	600	30	0.044
Example 23	OG-8A	700	33	0.029
Example 24	OG-8A	800	42	0.030
Example 25	OG-8A	850	46	0.027

Table 5

Relative humidity during reaction: 0%
	Type of sample	Heat-treating temperature (°C)	Degree of denitration (%)	Surface oxygen/ carbon
Comparative Example 8	OG-10A	-	48	0.096
Example 26	OG-10A	600	64	0.050
Example 27	OG-10A	850	42	0.043

Relative humidity during reaction: 80%
Comparative Example 9	OG-10A	-	9	0.096
Example 28	OG-10A	600	18	0.050
Example 29	OG-10A	850	24	0.043
Example 30	OG-10A	900	20	0.035

Table 6

Relative humidity during reaction: 0%
	Type of sample	Heat-treating temperature (°C)	Degree of denitration (%)	Surface oxygen/ carbon
Comparative Example 10	OG-20A	-	42	0.080
Example 31	OG-20A	600	50	0.045
Example 32	OG-20A	850	38	0.035

Relative humidity during reaction: 80%
Comparative Example 11	OG-20A	-	6	0.080
Example 33	OG-20A	600	15	0.045
Example 34	OG-20A	850	16	0.035

[0057] It is evident from the results shown in Tables 3 to 6 that the active carbon fibers modified by heat treatment exhibit an excellent denitrating effect.

Examples 35-38

[0058] One type of phenol-derived active carbon fibers ["FE-300" (trade name); manufactured by Toho Rayon Co., Ltd.; specific surface area, 850 m²/g] was heat-treated in the same manner as in Examples 10-34, and then used to treat a NO-containing gas. The results thus obtained are shown in Table 7.

Comparative Examples 12-13

[0059] Instead of being heat-treated, the two types of phenol-derived raw active carbon fibers used in Examples 35-38 were directly packed in tubular reactors similar to those used in Examples 35-38, and subjected to denitration reaction in the same manner as in Examples 35-38. The results thus obtained are also shown in Table 7.

Table 7

Relative humidity during reaction: 0%
	Type of sample	Heat-treating temperature (°C)	Degree of denitration (%)	Surface oxygen/ carbon
Comparative Example 12	FE-300	-	64	0.250
Example 35	FE-300	600	50	0.120
Example 36	FE-300	850	40	0.050

Relative humidity during reaction: 80%
Comparative Example 13	FE-300	-	5	0.250
Example 37	FE-300	600	14	0.120
Example 38	FE-300	850	8	0.050

[0060] It is evident from the results shown in Table 7 that the heat-treated active carbon fibers derived from phenol exhibit an improved denitrating effect, especially under high-humidity conditions including a relative humidity of 80%.

[0061] Now, several embodiments of the denitration system in accordance with the present invention are explained in greater detail. However, it is to be understood that the present invention is not limited thereto.

First Embodiment of the Denitration System

[0062] FIG. 2 illustrates a first embodiment of the denitration system for practicing the present invention.

[0063] In FIG. 2, reference numerals 1 and 2 designate a first packed reactor and a second packed reactor, respectively.

[0064] As shown in this figure, the first and second packed reactors are packed with a heat-treated active carbon which has been produced by heat-treating a raw active carbon at a temperature in the range of 600 to 1,000°C.

[0065] A nitrogen oxide-containing gas to be treated, together with ammonia (NH₃), is introduced into first packed reactor 1 where nitrogen oxides (NO_x) present in the gas to be treated are brought into contact with the ammonia and removed by the continuous selective reduction of them to nitrogen (N₂). Moreover, in second packed reactor 2, any excess ammonia remaining after the reaction is recovered by adsorption.

[0066] As the heat-treated active carbon packed into the aforesaid first packed reactor 1 and second packed reactor 2, there is used one obtained by chemically treating pitch-derived carbon fibers (formed by the melt spinning of pitch obtained as residue in coal chemical and petrochemical processes) under the following conditions.

[0067] In this embodiment, the aforesaid pitch-derived active carbon fibers comprised pitch-derived active carbon fibers "OG-5A" (trade name) manufactured by Osaka Gas Co., Ltd. These active carbon fibers were fired at about 850°C in a reducing atmosphere for one hour, shaped into a corrugated form, and then used in the embodiment.

[0068] Moreover, when polyacrylonitrile (PAN)-derived active carbon fibers obtained by firing and carbonizing high-molecular-weight polyacrylonitrile fibers ["FE-300" (trade name); manufactured by Toho Rayon Co., Ltd.] were used as the heat-treated active carbon, the concentration of nitrogen oxides (NO_x) in exhaust gas could also be reduced in the same manner as described above.

[0069] Furthermore, when a granular active carbon ["HC-30" (trade name); manufactured by Tsurumi Coal Co., Ltd.] heat-treated at 400-1,400°C in an atmosphere of nitrogen for one hour was used as the heat-treated active carbon, the concentration of nitrogen oxides (NO_x) in exhaust gas could also be reduced in the same manner as described above.

[0070] Besides the aforesaid heat treatment, the denitration performance and ammonia adsorption performance of active carbon can be improved by subjecting it to the following chemical treatment.

Metal carrying treatment

[0071] This treatment comprises adding a raw active carbon to a mixture composed of 100 parts by weight of active carbon, 10 parts by weight of iron nitrate, and 300 parts by weight of water, heating the resulting mixture at 60-70°C to evaporate the water, and holding it at 400°C (or 300-1,200°C) in an inert gas (N₂) for 4 hours.

[0072] Copper nitrate, manganese nitrate, nickel nitrate, cobalt nitrate, zinc nitrate and the like may also be used in place of the aforesaid iron nitrate.

[0073] The active carbon which has been subjected to a chemical treatment such as the metal carrying treatment shows an improvement in denitration performance and ammonia adsorption performance, and can be applied to the denitration in this and the other embodiments which will be described later.

Second Embodiment of the Denitration System

[0074] FIG. 3 illustrates a second embodiment of the denitration system in accordance with the present invention.

[0075] In FIG. 3, reference numeral 11 designates a first packed reactor; 12, a second packed reactor; 13 to 18, valves; and 19, an ammonia supply line.

[0076] As shown in FIG. 3, this denitration system is constructed so that a gas to be treated is alternately introduced into a first packed reactor 11 and a second packed reactor 12 which are packed with a heat-treated active carbon produced by heat-treating a raw active carbon at a temperature in the range of 600 to 1,000°C, whereby the gas is subjected to denitration reaction and any excess ammonia is recovered by adsorption.

[0077] In the first-step operation of this embodiment, as shown in FIG. 3(A), valves 13-15 are opened, valves 16-18 are closed, and an excess of ammonia (NH₃) is introduced through an ammonia supply line 19. Thus, in first packed reactor 11, nitrogen oxides (NO_x) present in the gas to be treated are brought into contact with the ammonia introduced together with the gas, and removed by the continuous selective reduction of them to nitrogen (N₂).

[0078] The gas from which nitrogen oxides have been removed is passed through valve 14 and introduced into second packed reactor 12 which is packed with the aforesaid heat-treated active carbon, where any excess ammonia is recovered by adsorption.

[0079] In the succeeding second-step operation, as shown in FIG. 3(B), valves 13-15 are closed, valves 16-18 are opened, and an excess of ammonia (NH₃) is introduced through ammonia supply line 19. Thus, in second packed reactor 12, nitrogen oxides (NO_x) present in the gas to be treated are brought into contact with the ammonia introduced together with the gas, and removed by the continuous selective reduction of them to nitrogen (N₂).

[0080] During this process, the excess ammonia adsorbed in second packed reactor 12 during the aforesaid first-step operation is also used for purposes of reduction, so that second packed reactor 12 is regenerated.

[0081] The gas from which nitrogen oxides have been removed is passed through valve 17 and introduced into first packed reactor 11, where any excess ammonia is recovered by adsorption.

[0082] Thus, nitrogen oxides can be continuously and efficiently treated by introducing a gas to be treated alternately into first packed reactor 11 and second packed reactor 12 so as to perform denitration and ammonia adsorption repeatedly.

Third Embodiment of the Denitration System

[0083] FIGs. 4 to 6 illustrate a third embodiment of the denitration system in accordance with the present invention.

[0084] In FIGs. 4 to 6, reference numeral 21 designates a first ammonia adsorber; 22, a second ammonia adsorber; 23, a denitrator; 24, an ammonia supply source; and 25 to 30, valves.

[0085] As shown in FIGs. 4 to 6, this denitration system includes a first ammonia adsorber 21 and a second ammonia adsorber 22 which are packed with a heat-treated active carbon produced by heat-treating a raw active carbon at a temperature in the range of 600 to 1,000°C, and a denitrator 23 located therebetween and packed with a heat-treated active carbon produced by heat-treating a raw active carbon at a temperature in the range of 600 to 1,000°C. Exhaust gas is alternately introduced from the sides of first ammonia adsorber 21 and second ammonia adsorber 22, whereby the gas is subjected to denitration reaction and any excess ammonia is recovered by adsorption.

[0086] In the first-step operation of this embodiment, as shown in FIG. 4, valves 25, 28 and 30 are opened, valves 26, 27 and 29 are closed, and an excess of ammonia (NH₃) is introduced from an ammonia supply source 24 into denitrator 23 by way of valve 28. Thus, in denitrator 23, nitrogen oxides (NO_x) present in the exhaust gas are brought into contact with the ammonia introduced together with the exhaust gas, and removed by the continuous selective reduction of them to nitrogen (N₂).

[0087] The exhaust gas from which nitrogen oxides have been removed is introduced into second ammonia adsorber 22 located on the downstream side, where any excess ammonia is recovered by adsorption. Thereafter, the cleaned gas is discharged through valve 30.

[0088] In the succeeding second-step operation, as shown in FIG. 5, valves 25, 28 and 30 are closed, valves 26, 27 and 29 are opened, and an excess of ammonia (NH₃) is introduced from ammonia supply source 24 into denitrator 23 by way of valve 29. Thus, in denitrator 23, nitrogen oxides (NO_x) present in the gas to be treated are brought into contact with the ammonia introduced together with the gas, and removed by the continuous selective reduction of them to nitrogen (N₂).

[0089] During this process, the excess ammonia adsorbed in second ammonia adsorber 22 during the aforesaid first-step operation is also used for purposes of reduction, so that second ammonia adsorber 22 is regenerated.

[0090] The exhaust gas from which nitrogen oxides have been removed is introduced into first ammonia adsorber 21 located on the downstream side, where any excess ammonia is recovered by adsorption. Thereafter, the cleaned gas is discharged through valve 27.

[0091] In the succeeding third-step operation, as shown in FIG. 6, valves 25, 28 and 30 are opened, valves 26, 27 and 29 are closed, and an excess of ammonia (NH₃) is introduced from ammonia supply source 24 into denitrator 23 by way of valve 28, similarly to the first-step operation. Thus, in denitrator 23, nitrogen oxides (NO_x) present in the gas to be treated are brought into contact with the ammonia introduced together with the gas, and removed by the continuous selective reduction of them to nitrogen (N₂).

[0092] During this process, the excess ammonia adsorbed in first ammonia adsorber 21 during the aforesaid second-step operation is also used for purposes of reduction, so that first ammonia adsorber 21 is regenerated.

[0093] The exhaust gas from which nitrogen oxides have been removed is introduced into second ammonia adsorber 22 located on the downstream side, where any excess ammonia is recovered by adsorption. Thereafter, the cleaned gas is discharged through valve 30.

[0094] Thus, nitrogen oxides can be continuously and efficiently treated by introducing exhaust gas alternately into first ammonia adsorber 21 and second ammonia adsorber 22 so as to perform denitration and ammonia adsorption repeatedly and, moreover, regenerate the ammonia adsorbers.

[0095] The treatment of exhaust gases discharged from boilers, gas turbines, engines and combustion furnaces for burning various types of fuel is facilitated by applying the aforesaid denitration systems to the removal of nitrogen oxides (NO_x) present therein.

[0096] Moreover, the present invention can also be suitably used for the removal of nitrogen oxides present in tunnels and for the removal of nitrogen oxides present in exhaust gases from nitric acid production plants.

Claims

1. A selective catalytic reduction method for the denitration of exhaust gases which consists of the steps of:

(a) heat treating raw active carbon fibres having a pore diameter of 10 to 30 Å, a pore volume of 0.3 to 1.2 ml/g and a specific surface area of 500 to 2000 m²/g at 600 to 1200°C in a non-oxidising atmosphere such that the heat treated active carbon has micropores with a size of 20Å or less and an atomic surface oxygen to surface carbon ratio of 0.05 or less; and

(b) bringing exhaust gas containing 500 ppm or less of nitrogen oxides, 3% or more of oxygen and not more than 80% of water as water vapour and ammonia gas having the same concentration as the nitrogen oxides into contact, at a temperature of 100°C or below, with said heat treated active carbon from step a), as such.

2. A selective catalytic reduction method as claimed in claim 1, said method additionally comprising providing an apparatus which comprises a first packed reactor which is packed with said heat-treated active carbon fibre and a second packed reactor which is located downstream thereof and packed with said heat-treated active carbon fibre, introducing exhaust gas and ammonia into the first packed reactor so as to bring nitrogen oxides present in the exhaust gas into contact with the ammonia and remove the nitrogen oxides by the continuous selective reduction to nitrogen, and recovering any excess ammonia by adsorption in the second packed reactor.

3. A selective catalytic reduction method as claimed in claim 1, said method additionally comprising providing an apparatus which comprises a denitrator packed with said heat-treated active carbon fibre and first and second ammonia adsorbers located before and behind said denitrator, respectively, alternately introducing exhaust gas containing nitrogen oxides through the first and second ammonia adsorbers, introducing ammonia at a position between the first or second ammonia adsorber and the denitrator, contacting nitrogen oxides present in the exhaust gas with the heat-treated active carbon fibre placed in the denitrator and thereby removing them by reduction to nitrogen, and recovering any excess ammonia by adsorption in the adsorber located downstream of the denitrator.

4. A selective catalytic reduction method as claimed in claim 2 or 3 to remove nitrogen oxide(s) from an exhaust gas such as a ventilation gas, boiler exhaust gas or furnace exhaust gas.

5. A selective catalytic reduction method as claimed in claim 4 wherein the exhaust gas is introduced alternately into the first packed reactor and the second packed reactor so as to perform denitration and ammonia adsorption repeatedly.

6. A selective catalytic reduction method as claimed in any one of claims 1 to 5 wherein said raw active carbon fibres are derived from polyacrylonitrile or pitch.

Ansprüche

1. Selektives katalytisches Reduktionsverfahren für die Entstickung von Abgasen, welches aus den folgenden Schritten besteht:

a) Hitze-Behandeln roher aktiver Kohlenstoff-Fasern, die einen Porendurchmesser von 10 bis 30 Å, ein Porenvolumen von 0,3 bis 1,2 ml/g und eine spezifische Oberfläche von 500 bis 2.000 m²/g aufweisen, bei 600 bis 1.200 °C in einer nicht-oxidierenden Atmosphäre derart, dass der Hitze-behandelte aktive Kohlenstoff Mikroporen mit einer Größe von 20 Å oder weniger und ein atomares Oberflächen-Sauerstoff zu Oberflächen-Kohlenstoff-Verhältnis von 0,05 oder weniger aufweist; und

b) In-Kontakt-Bringen von Abgas, das 500 ppm oder weniger Stickstoff oxide, 3 % oder mehr Sauerstoff und nicht mehr als 80 % Wasser als Wasserdampf enthält, und Ammoniak-Gas, das dieselbe Konzentration wie die Stickstoff-Oxide aufweist, mit dem Hitze-behandelten aktiven Kohlenstoff aus Schritt a) als solchem bei einer Temperatur von 100 °C oder darunter.

2. Selektives katalytisches Reduktionsverfahren wie in Anspruch 1 beansprucht, wobei das Verfahren zusätzlich den Schritt umfasst, dass man eine Vorrichtung bereitstellt, die einen ersten gepackten Reaktor, der mit der Hitze-behandelten aktiven Kohlenstoff-Faser gepackt ist, und einen zweiten gepackten Reaktor umfasst, der stromabwärts davon angeordnet ist und mit der Hitze-behandelten Kohlenstoff-Faser gepackt ist, Abgas und Ammoniak in den ersten gepackten Reaktor einleitet und so Stickstoff-Oxide, die in dem Abgas zugegen sind, in Kontakt mit dem Ammoniak bringt und die Stickstoff-Oxide durch die kontinuierliche selektive Reduktion zu Stickstoff entfernt, und irgendeinen Überschuss an Ammoniak durch Adsorption in dem zweiten gepackten Reaktor zurückgewinnt.

3. Selektives katalytisches Reduktionsverfahren wie in Anspruch 1 beansprucht, wobei das Verfahren zusätzlich den Schritt umfasst, dass man eine Vorrichtung bereitstellt, die einen Denitrator, der mit der Hitze-behandelten aktiven Kohlenstoff-Faser gepackt ist, und einen ersten und einen zweiten Ammoniak-Adsorber umfasst, die vor bzw. hinter dem Denitrator angeordnet sind, abwechselnd Abgas, das Stickstoff-Oxide enthält, durch den ersten und den zweiten Ammoniak-Adsorber leitet, Ammoniak an einer Stelle zwischen dem ersten oder zweiten Ammoniak-Adsorber und dem Denitrator einleitet, Stickstoff-Oxide, die in dem Abgas zugegen sind, mit der Hitze-behandelten aktiven Kohlenstoff-Faser in Kontakt bringt, die in dem Denitrator angeordnet ist, und diese dadurch durch Reduktion zu Stickstoff entfernt, und irgendeinen Überschuss an Ammoniak durch Adsorption in dem Adsorber wieder gewinnt, der stromabwärts von dem Denitrator angeordnet ist.

4. Selektives katalytisches Reduktionsverfahren wie in Anspruch 2 oder 3 beansprucht, zum Entfernen von Stickstoff-Oxid(en) von einem Abgas wie beispielsweise einem Belüftungsgas, Kessel-Abgas oder Ofen-Abgas.

5. Selektives katalytisches Reduktionsverfahren wie in Anspruch 4 beansprucht, worin das Abgas abwechselnd in den ersten gepackten Reaktor und den zweiten gepackten Reaktor eingeleitet wird und so eine Entstickung und Ammoniak-Adsorption wiederholt durchgeführt wird.

6. Selektives katalytisches Reduktionsverfahren wie in irgendeinem der Ansprüche 1 bis 5 beansprucht, worin die rohen aktiven Kohlenstoff-Fasern von Polyacrylnitril oder Pech abgeleitet sind.

Revendications

1. Un procédé de réduction catalytique sélective pour l'élimination de l'azote dans les gaz d'échappement comprenant les étapes suivantes:

(a) traiter thermiquement des fibres brutes de charbon actif ayant un diamètre de pore de 10 à 30Å, un volume de pore de 0,3 à 1,2 ml/g et une aire de surface spécifique de 500 à 2000 m²/g entre 600 et 1200°C dans une atmosphère non-oxydante de façon que le charbon actif soumis au traitement thermique ait des micropores d'une dimension de 20Å ou moins et un rapport entre l'oxygène atomique de surface et le carbone de surface de 0,05 ou moins; et

(b) amener le gaz d'échappement contenant 500 ppm ou moins d'oxydes d'azote, 3% ou plus d'oxygène et pas plus de 80% d'eau sous forme de vapeur d'eau et du gaz ammoniac ayant la même concentration que les oxydes d'azote en contact, à une température de 100°C ou en dessous, avec ledit charbon actif traité thermiquement dans l'étape a), tel quel.

2. Un procédé de réduction catalytique sélective selon la revendication 1, ledit procédé comprenant additionnellement la réalisation d'un appareil qui comprend une premier réacteur garni qui est rempli de ladite fibre de charbon actif traitée thermiquement et un second réacteur garni qui est situé en aval du premier et rempli de ladite fibre de charbon actif traitée thermiquement, l'introduction du gaz d'échappement et de l'ammoniac dans le premier réacteur garni de façon à amener les oxydes d'azote présents dans le gaz d'échappement en contact avec l'ammoniac et éliminer les oxydes d'azote par réduction sélective continue en azote, et la récupération de tout l'ammoniac en excès par adsorption dans le second réacteur garni.

3. Un procédé de réduction catalytique sélective selon la revendication 1, ledit procédé comprenant additionnellement la réalisation d'un appareil qui comprend un dénitrateur garni de ladite fibre de charbon actif traitée thermiquement et des premier et second adsorbeurs d'ammoniac situés respectivement devant et derrière ledit dénitrateur, alternativement l'introduction du gaz d'échappement contenant des oxydes d'azote via les premier et second adsorbeurs d'ammoniac, l'introduction d'ammoniac dans une position entre le premier ou le second adsorbeur d'ammoniac et le dénitrateur, la mise en contact des oxydes d'azote présents dans le gaz d'échappement avec la fibre de charbon actif traitée thermiquement placée dans le dénitrateur et de ce fait leur élimination par réduction en azote, et la récupération de tout l'ammoniac en excès par adsorption dans l'adsorbeur situé en aval du dénitrateur.

4. Un procédé de réduction catalytique sélective selon l'une des revendications 2 et 3 pour éliminer l'oxyde d'azote ou les oxydes d'azote d'un gaz d'échappement comme un gaz de ventilation, un gaz d'échappement de chaudière ou un gaz d'échappement de four.

5. Un procédé de réduction catalytique sélective selon la revendication 4 où le gaz d'échappement est de façon alternative introduit dans le premier réacteur garni et le second réacteur garni de façon à obtenir l'élimination de l'azote et l'adsorption de l'ammoniac de façon répétitive.

6. Un procédé de réduction catalytique sélective selon l'une quelconque des revendications 1 à 5 où lesdites fibres de charbon actif brutes sont dérivées du polyacrylonitrile ou du brai.

Drawing