Method for desulphurizating and denitrating flue gas in integrated manner based on low-temperature adsorption

Abstract

Provided is a method for desulphurizating and denitrating a flue gas in an integrated manner based on low-temperature adsorption. The method includes: decreasing a temperature of the flue gas below a room temperature by using a flue gas cooling system; removing moisture in the flue gas by using a dehumidification system; sending the flue gas to a SO.sub.2 and NO.sub.x adsorbing column system; and simultaneously adsorbing SO.sub.2 and NO.sub.x of the flue gas with a material of activated coke, activated carbon, a molecular sieve or diatom mud in the SO.sub.2 and NO.sub.x adsorbing column system to implement an integration of desulphurization and denitration of the flue gas based on the low-temperature adsorption. With the present method, SO.sub.2 and NO.sub.x of the flue gas can be adsorbed simultaneously in an environment having a temperature below the room temperature.

Claims

1. A method for desulphurizating and denitrating a flue gas in an integrated manner based on low-temperature adsorption, comprising: decreasing a temperature of the flue gas below a room temperature by using a flue gas cooling system (1); removing moisture in the flue gas by using a dehumidification system; sending the flue gas to a SO.sub.2 and NO.sub.x adsorbing column system (2); and simultaneously adsorbing SO.sub.2 and NO.sub.x of the flue gas with a material of activated coke, activated carbon, a molecular sieve or diatom mud in the SO.sub.2 and NO.sub.x adsorbing column system (2) to implement an integration of desulphurization and denitration of the flue gas based on the low-temperature adsorption.

2. The method according to claim 1, wherein NO is oxidized to NO.sub.2 by the activated coke, the activated carbon, the molecular sieve or the diatom mud at a low temperature, and NO.sub.2 is adsorbed.

3. The method according to claim 1, wherein the temperature of the flue gas is decreased to a range of −100° C. to 25° C. by the flue gas cooling system (1).

4. The method according to claim 1, further comprising: heating or vacuumizing the activated coke, the activated carbon, the molecular sieve or the diatom mud adsorbed with SO.sub.2 and NO.sub.x, to regenerate and recycle the activated coke, the activated carbon, the molecular sieve or the diatom mud, and to desorb and recycle SO.sub.2 and NO.sub.x.

5. The method according to claim 4, wherein the heating is performed at a temperature of 100° C. to 350° C.

6. The method according to claim 1, wherein the material of activated coke, activated carbon, a molecular sieve or diatom mud is in a form of particles with a size of 30 to 40 mesh.

Description

BRIEF DESCRIPTION OF THE DRAWINGS

(1) FIG. 1 is a schematic diagram showing a process according to the present disclosure.

(2) FIG. 2 is a graph showing a relationship between a sulfur capacity of activated carbon and an adsorption temperature at a SO.sub.2 concentration of 3000 mg/Nm.sup.3.

(3) FIG. 3 is a graph showing a penetration time of NO.sub.x adsorption of activated carbon at a NO.sub.x concentration of 500 mg/Nm.sup.3.

(4) FIG. 4 is a schematic diagram showing an experimental device of Example 1, Example 2 and Comparative Example.

REFERENCE NUMERALS

(5) 1: flue gas cooling system; 2: SO.sub.2 and NO.sub.x adsorbing column system.

DETAILED DESCRIPTION

(6) The following is the detailed description of the present disclosure in combination with the drawings.

(7) An existing integrated desulphurization and denitration technology is industrially applied based on activated coke adsorption. This technology refers to that SO.sub.2 is adsorbed and thus removed due to porous adsorption characteristics of activated coke. However, the activated coke adsorption process cannot adsorb and remove NO.sub.x, since it is difficult for NO to be adsorbed. In this technology, it still needs to reduce NO.sub.x into N.sub.2 by spraying ammonia to the gas, and activated coke is used as a selective reduction catalyst. By using activated coke, a denitration rate is relatively low and to be from about 70% to 80%, which cannot meet a requirement of ultra-clean emissions. In addition, since the activated coke dry desulphurization is based on H.sub.2SO.sub.4 chemical adsorption, a regeneration temperature is high. Activated coke participates in the regeneration reaction, which causes a large loss.

(8) A process of activated coke (carbon) dry desulfurization is as follows.
SO.sub.2+H.sub.2O+1/2O.sub.2═H.sub.2SO.sub.4  Adsorption reaction:

(9) Heating regeneration reaction:
a reaction at 350° C. to 450° C.: H.sub.2SO.sub.4+C.fwdarw.CO.sub.2+2SO.sub.2+2H.sub.2O
a reaction above 450° C.: H.sub.2SO.sub.4+C.fwdarw.CO+SO.sub.2+H.sub.2O A process of activated coke (carbon) catalytic reduction denitration is as follows. 4NO+4NH.sub.3+O.sub.2.fwdarw.3N.sub.2+6H.sub.2O 6NO+4NH.sub.3.fwdarw.5N.sub.2+6H.sub.2O 2NO.sub.2+4NH.sub.3+O.sub.2.fwdarw.3N.sub.2+6H.sub.2O 6NO.sub.2+8NH.sub.3.fwdarw.7N.sub.2+12H.sub.2O

(10) In order to solve the problems existing in the related art, the present disclosure provides a method for desulphurizating and denitrating a flue gas in an integrated manner based on low-temperature adsorption, which is capable of simultaneously adsorbing SO.sub.2 and NO.sub.x (i.e., NO and/or NO.sub.2) and removing them from the flue gas in an environment having a temperature lower than the room temperature.

(11) In an embodiment, the method for desulphurizating and denitrating the flue gas in the integrated manner based on the low-temperature adsorption includes: decreasing a temperature of the flue gas below a room temperature by using a flue gas cooling system; removing moisture in the flue gas by using a dehumidification system; sending the flue gas to a SO.sub.2 and NO.sub.x adsorbing column system; and simultaneously adsorbing SO.sub.2 and NO.sub.x of the flue gas with a material of activated coke, activated carbon, a molecular sieve or diatom mud in the SO.sub.2 and NO.sub.x adsorbing column system to implement an integration of desulphurization and denitration of the flue gas based on the low-temperature adsorption.

(12) In an embodiment, NO is oxidized to NO.sub.2 by the activated coke, the activated carbon, the molecular sieve or the diatom mud at a low temperature, and NO.sub.2 is adsorbed.

(13) In an embodiment, the temperature of the flue gas is decreased to a range of −100° C. to 25° C. by the flue gas cooling system.

(14) In an embodiment, the method further includes: heating or vacuumizing the activated coke, the activated carbon, the molecular sieves or the diatom mud adsorbed with SO.sub.2 and NO.sub.x, to regenerate and recycle the activated coke, the activated carbon, the molecular sieve or the diatom mud, and to desorb and recycle SO.sub.2 and NO.sub.x.

(15) In an embodiment, the heating is performed at a temperature of 100° C. to 350° C.

(16) In an embodiment, the material of activated coke, activated carbon, a molecular sieve or diatom mud is in a form of particles with a size of 30 to 40 mesh.

(17) The present disclosure has the following beneficial effects.

(18) In the method of present disclosure, the desulphurization and the denitration of the flue gas based on the low-temperature adsorption are integrated. The temperature of the flue gas is decreased below the room temperature by the flue gas cooling system, the moisture contained in the flue gas is removed by using the dehumidification system, and SO.sub.2 and NO.sub.x contained in the flue gas are adsorbed by the material of the activated coke, the activated carbon, the molecular sieve or the diatom mud in the SO.sub.2 and NO.sub.x adsorbing column system to simultaneously adsorb SO.sub.2 and NO.sub.x and remove them from the flue gas in an environment having a temperature lower than the room temperature. It should be noted that, an adsorption capacity for SO.sub.2 at a low temperature is much higher than an adsorption capacity at a high temperature. The flue gas is desulphurized after the temperature of the flue gas is decreased below the room temperature, which greatly reduces an adsorbent loading and a size of the adsorbing column. Further, NO.sub.x may be efficiently adsorbed and removed at a low temperature, and cannot be effectively adsorbed and removed at the room temperature or higher. In this case, by decreasing the temperature of the flue gas below the room temperature, the NO.sub.x adsorption and the flue gas denitration are improved. In addition, it should be noted that the present disclosure provides adsorbing and removing SO.sub.2 and NO.sub.x simultaneously at the same temperature and in the same device, and thus can be widely applied to a flue gas containing SO.sub.2 and NO.sub.x, for example obtained from coal-burning, such as a power plant flue gas, a steel plant flue gas, or a coke oven flue gas.

(19) Furthermore, the adsorbent may be regenerated by heating at a temperature of 100° C. to 350° C. or vacuum sucking. This regeneration temperature is lower than that of a conventional activated coke dry desulphurization and denitration regeneration process. In the present disclosure, the activated coke does not participate in the regeneration reaction, and thus the loss is low.

(20) The present disclosure is further described with reference to the drawings.

(21) As shown in FIG. 1, a method for desulphurizating and denitrating a flue gas in an integrated manner based on low-temperature adsorption provided in an embodiment of the present disclosure includes the following steps.

(22) A temperature of a flue gas containing SO.sub.2 and NO.sub.x is decreased below room temperature by using a flue gas cooling system 1, a part of a water vapour in the flue gas may be removed by condensation. A moisture content of the flue gas will not be higher than a saturated moisture content at the cooling temperature. The cooled flue gas flows through a SO.sub.2 and NO.sub.x adsorbing column system 2, where SO.sub.2 and NO.sub.x are adsorbed by activated coke, activated carbon, molecular sieves or diatom mud and thus are removed from the flue gas. The low-temperature flue gas after desulphurization and denitration is discharged after cold energy recovery. SO.sub.2 and NO.sub.x adsorbed by the adsorbent are desorbed by heating regeneration or vacuum sucking regeneration, and are recycled. The adsorbent may be recycled after regeneration.

Example 1

(23) As shown in FIG. 4, an analog flue gas includes SO.sub.2 of 3000 mg/Nm.sup.3, NO.sub.x of 500 mg/Nm.sup.3, CO.sub.2 of 12%, and 02 of 6%. A flow rate of the analog flue gas is 1 L/min.

(24) The analog flue gas containing SO.sub.2 and NO.sub.x is humidified by a gas-washing bottle filled with 30% calcium chloride solution as a humidifier, and the gas-washing bottle is placed in a constant temperature bath at −20° C., and thus a moisture content of the flue gas is a saturated humidity at this temperature. After the flue gas has been introduced for a period of time, pollutant composition at an inlet of the gas-washing bottle is the same as that at an outlet of the gas-washing bottle, the low-temperature flue gas with the saturated humidity is introduced into an adsorption tube. The adsorption tube is filled with 5 g activated carbon particles with a size of 30 to 40 mesh. Contents of SO.sub.2 and NO.sub.x contained in the flue gas after passing through the activated carbon bed are detected by a flue gas analyzer, and saturated adsorption capacities calculated from breakthrough curves (i.e., penetration time curves) of SO.sub.2 and NO.sub.x are shown in Table 1.

Example 2

(25) In Example 2, a constant temperature bath is controlled at 0° C., and other operations are the same as those in Example 1.

Comparative Example

(26) In the Comparative Example, a constant temperature bath is controlled at 100° C. while the desulfurization and the denitration are carried out, and other operations are the same as those in Example 1.

(27) Table 1 shows penetration times and effective adsorption amounts of SO.sub.2 and NO.sub.x in the above inventive examples and the comparative example.

(28) TABLE-US-00001 TABLE 1 Comparative Example 1 Example 2 Example adsorption temperature −20° C.   0° C. 100° C. SO.sub.2 penetration time 300 min  145 min  37 min effective adsorption 180 mg/g   87 mg/g  22 mg/g amount for SO.sub.2 NO.sub.x penetration time 800 min  230 min  0 effective adsorption  96 mg/g 27.6 mg/g  0 amount for NO.sub.x

(29) An effective adsorption amount refers to an adsorption amount before SO.sub.2 or NO.sub.x does not penetrate the adsorbent. The above results of the inventive examples and the comparative example in table 1 show that: a) the adsorption amount of SO.sub.2 at −20° C. is about 8 times that at 100° C., and thus a better SO.sub.2 adsorption effect may be achieved at a low temperature; b) NO.sub.x may be effectively adsorbed and removed at low temperature, but NO.sub.x penetrates the bed instantly at a high temperature and cannot be adsorbed and removed, which needs to be reduced by injecting ammonia. Therefore, the method of desulphurizating and denitrating the flue gas in the integrated manner based on the low-temperature adsorption of the present disclosure is more advantageous than conventional adsorption desulphurization methods.