KR102053559B1 - Activated Carbon Flue Gas Purifier and Flue Gas Purification Method - Google Patents

Abstract

An activated carbon flue gas purification device including an activated carbon adsorption tower is provided. The activated carbon adsorption tower comprises a lower activated carbon bed layer portion (A), an upper activated carbon bed layer portion (B) and a transition zone (C) disposed between these two portions. The activated carbon adsorption tower comprises a feeder (3) disposed on or at the top of the adsorption tower, a flue gas inlet (1) disposed at the bottom of the adsorption tower and a flue gas outlet (2) disposed at the top of the adsorption tower, the lower activated carbon bed layer The flue gas outlet end G2 of the part A is connected with the flue gas inlet end G3 of the upper activated carbon bed layer part B via the flue gas channel 5. The lower activated carbon bed layer portion A has 2-7 activated carbon chambers divided by the porous separator 4 and thus formed by the porous separator 4, and the lower activated carbon chambers have flue gas flow The thickness increases sequentially along the direction. The upper activated carbon bed layer part B has 2-7 activated carbon chambers divided by the porous separator 4 and thus formed by the porous separator 4, and the activated carbon chambers disposed thereon are flue gas flows. The thickness increases sequentially along the direction.

Description

Activated Carbon Flue Gas Purifier and Flue Gas Purification Method

This application claims the benefit of priority of Chinese Patent Application No. 201510780033.7, filed with the Chinese Patent Office on November 13, 2015, under the name "Activated Carbon Flue Gas Purification Device and Flue Gas Purification Method", the entire disclosure of which is cited. Incorporated herein by.

The present application relates to an activated carbon flue gas purification device and a flue gas purification method, the device being an activated carbon flue gas purification device applicable for air pollution control, and related to the field of environmental protection.

For industrial flue gases, in particular for sinter flue gases in the steel industry, it is relatively ideal to use desulfurization and denitrification apparatus and technology, including activated carbon adsorption towers and desorption towers. In a desulfurization and denitrification apparatus comprising an activated carbon adsorption tower and a desorption tower (or a regeneration tower), the activated carbon adsorption tower is composed of sulfur oxides, nitrogen oxides and dioxins from sintered flue gases or exhaust gases (especially sintered flue gases of sinterers in the steel industry). It is used to adsorb contaminants, including, and the desorption tower is used for thermal regeneration of activated carbon.

Activated carbon desulfurization has a high degree of desulfurization and can simultaneously realize denitrification, dioxin removal and dust removal without generating waste water and wastes, and thus is a promising flue gas purification method. Activated carbon can be regenerated at high temperatures above 350 ° C. and contaminants such as sulfur oxides, nitrogen oxides, dioxins, etc. adsorbed on the activated carbon will desorb and decompose rapidly (sulfur oxides desorb and nitrogen oxides and dioxins decompose). And with the increase of temperature, the activated carbon regeneration speed is further accelerated, and thus the regeneration time is shortened. Preferably, the activated carbon regeneration temperature of the desorption tower is generally controlled at approximately 430 ° C., so the ideal desorption temperature (or regeneration temperature) is for example in the range of 390 ° C. to 450 ° C., more preferably of 400 ° C. to 440 ° C. Range.

A conventional activated carbon desulfurization technique is shown in FIG. Flue gas is introduced into the adsorption tower by a booster fan, a mixed gas of ammonia and air is injected from the tower inlet into the tower, improving the efficiency of NO _x removal, and the purified flue gas is sent to the sintering main chimney. Enter and exit. Activated carbon is added to the adsorption tower from the top of the tower and moves downwards under the action of both gravity and the evacuation device at the bottom of the tower. Activated carbon from the desorption tower is transported to the adsorption tower by a second activated carbon conveyor, saturated activated carbon adsorbed by contaminants in the adsorption tower is discharged from the bottom of the tower, and the discharged activated carbon is desorbed by the first activated carbon conveyor for regeneration of the activated carbon. Transported by

The function of the desorption tower is to release SO ₂ adsorbed on activated carbon, and more than 80% of dioxin can be decomposed at a temperature of 400 ° C. or higher and a constant residence time. The activated carbon can be cooled, sieved and reused. The released SO ₂ can be used to produce sulfuric acid and the like, and the desorbed activated carbon is transported by the conveyor to the adsorption tower for reuse in adsorbing SO ₂ and NO _x .

NO _x and ammonia to remove NO _x by performing such as SCR and SNCR reaction in the adsorption tower and desorption tower. As the dust passes through the adsorption tower, it is adsorbed on the activated carbon, separated by vibrating sieve at the bottom of the desorption tower, and the activated carbon powder obtained by the sieve is sent to the ash box, and then as fuel in the blast furnace or sintering furnace. It may be transported.

When using activated carbon to purify flue gas, flue gas may be passed through a multilayered activated carbon bed layer to enhance the purifying effect. The multilayer activated carbon bed layer structure may be mainly divided into a vertical structure and a front and rear structure as shown in FIG. 2. The bed of activated carbon in the column is the whole, and the activated carbon falls evenly by gravity. Along the flue gas flow direction, activated carbon, first contacted with the flue gas, adsorbs more contaminants in the flue gas and is released with the activated carbon in the rear, as a result of which the activated carbon in the rear is released from the tower without saturation by adsorption, Or the activated carbon in the front still remains in the tower after saturation by adsorption, and thus does not have a flue gas purification effect.

The prior art adopts an adsorption tower having a front and rear series structure as shown in FIG. However, there is a need for a set of activated carbon transportation devices that not only increases investment and operating costs, but also increases the amount of additional equipment maintenance work.

Therefore, in order to not only reduce investment and operating costs, but also to improve the purification effect, it is necessary to use a more reasonable activated carbon purification device.

An object of the present invention is to provide an activated carbon flue gas purification apparatus comprising an activated carbon adsorption tower.

The activated carbon adsorption tower has a transition located between the lower activated carbon bed layer portion (A) at the bottom, the upper activated carbon bed layer portion (B) at the top, and the lower activated carbon bed layer portion (A) and the upper activated carbon bed layer portion (B). Zone (C), the activated carbon adsorption tower comprising a supply vessel (3) located above or at the top of the adsorption tower, a flue gas inlet (1) located at the bottom of the adsorption tower, and a flue gas outlet located at the top of the adsorption tower ( 2), wherein the flue gas outlet end G2 of the lower activated carbon bed layer portion A is connected to the flue gas inlet end G3 of the upper activated carbon bed layer portion B through the flue gas channel 5; In communication, the lower activated carbon bed layer portion (A) has two to seven (preferably three to five) activated carbon chambers divided by a porous diaphragm (4), and the upper activated carbon bed layer portion (B) 2 to 7 (preferably 3 to 5) divided by the porous diaphragm 4 Dog) activated carbon chamber.

Preferably, the present application provides an activated carbon flue gas purification device including an activated carbon adsorption tower (that is, a desulfurization and denitrification device including an activated carbon adsorption tower and a desorption tower, or an activated carbon flue gas purification device including an activated carbon adsorption tower and a desorption tower). do. The activated carbon adsorption tower has a lower activated carbon bed layer portion (A) at the bottom, an upper activated carbon bed layer portion (B) at the top, and a transition zone (C) (or intermediate zone (C)) located between these two portions. It includes. The activated carbon adsorption tower further comprises a supply vessel 3 located above or at the top of the adsorption tower, a flue gas inlet 1 located at the bottom of the adsorption tower, and a flue gas outlet 2 located at the top of the adsorption tower, The flue gas outlet end G2 of the lower activated carbon bed layer part A communicates with the flue gas inlet end G3 of the upper activated carbon bed layer part B through the flue gas channel 5. The lower activated carbon bed layer part A is 2 to 7 (preferably 3 to 5, for example 3, 4) divided by (or formed by) a porous diaphragm 4. Dogs, five, six or seven activated carbon chambers (for example there are seven activated carbon chambers sequentially numbered a1, a2, a3, a4, a5, a6, a7, etc.). In addition, along the flue gas flow direction (in this order), the lower activated carbon chambers are sequentially increased in thickness, or along the flue gas flow direction, in the lower part behind the first activated carbon chamber a1 located below. In any two adjacent activated carbon chambers of (e.g., a2 and a3, or a3 and a4), the rear of two adjacent activated carbon chambers (e.g., a3 or a4) is the front of two adjacent activated carbon chambers of The thickness is greater than or equal to that of (eg, a2 or a3). The upper activated carbon bed layer part B is 2 to 7 (preferably 3 to 5, for example 3, 4) divided by (or formed by) a porous diaphragm 4. Dogs, five, six or seven activated carbon chambers (eg, there are seven activated carbon chambers sequentially numbered b1, b2, b3, b4, b5, b6, b7, etc.). In addition, along the flue gas flow direction (in this order), the activated carbon chambers located at the top sequentially increase in thickness, or along the flue gas flow direction, any one behind the first activated carbon chamber b1 located at the top. In two adjacent activated carbon chambers (e.g., b2 and b3, or b3 and b4), the rear one of the two adjacent activated carbon chambers (e.g., b3 or b4) is the one in front of the two adjacent activated carbon chambers ( For example, the thickness is greater than or equal to b2 or b3).

Preferably, in the flue gas flow direction in two to seven (eg three) activated carbon chambers located at the bottom or in two to seven (eg three) activated carbon chambers located at the top In order, the thickness of the second chamber a2 or b2 may be between 1 and 9 times the thickness of the first chamber a1 or b1 (eg, 2 times, 3 times, 4 times, 5 times, 6 times and 6 times). Same 1.5 to 7 times). Moreover, in the case where there is a third chamber a3 or b3, the thickness of the third chamber a3 or b3 is 1 to 2.5 times the thickness of the second chamber a2 or b2 (preferably 1.2 to 2 times). Pear, for example 1.3-fold, 1.5-fold or 1.8-fold). In the present application, by using the above structural design, the moving speed of the solid adsorption medium (or also referred to as the solid medium, such as activated carbon or activated carbon coke) in the front chamber is reduced to that of the solid adsorption medium (or referred to as the solid medium) in the rear chamber. Faster or the same as Breaking News.

Generally, the lower part has three activated carbon chambers, and in order of flue gas flow direction, the first chamber a1 (i.e. the front chamber), the second chamber a2 (i.e. the intermediate chamber) and the third chamber a3. ), I.e. the rear chamber, may each have a thickness of 90 to 250 mm (preferably 100 to 230 mm, eg 120, 150, 200 or 220 mm), 360 to 1000 mm (preferably 400 to 950 mm, for example). For example 450, 600, 700, 800 or 900 mm) and 432 to 1200 mm (preferably 450 to 1150 mm, for example 500, 600, 700, 800, 900, 1000 or 1100 mm).

Generally, the upper part has three activated carbon chambers, and in order of flue gas flow direction, the first chamber b1 (i.e., the front chamber), the second chamber b2 (i.e., the intermediate chamber), and the third chamber b3. ), I.e. the rear chamber, may each have a thickness of 90 to 250 mm (preferably 100 to 230 mm, eg 120, 150, 200 or 220 mm), 360 to 1000 mm (preferably 400 to 950 mm, for example). For example 450, 600, 700, 800 or 900 mm) and 432 to 1200 mm (preferably 450 to 1150 mm, for example 500, 600, 700, 800, 900, 1000 or 1100 mm).

Preferably, the flue gas inlet 1 located at the bottom of the adsorption tower and the flue gas outlet 2 located at the top of the adsorption tower lie on the same side of the adsorption tower.

Preferably, a roll feeder 6 is arranged at the bottom of each chamber of the lower activated carbon bed layer portion A. As shown in FIG.

Preferably, one or more discharge rotary valves 7 are arranged in the bottom barrel of the adsorption tower.

In general, a number of activated carbon channels 10 (eg 2 to 7, such as 3, 4, 5, 6) are arranged in the transition zone (C). Preferably, the activated carbon channel 10 is formed by a separator wall 9 and a tower wall of an adsorption tower, a cylinder 9 having a circular cross section or a cone cylinder 9, a tube having an elliptical cross section or It is formed by the cylinder 9 or by the tube or cylinder 9 which has a cross section of a polygon (for example, triangular or rectangular or pentagonal or hexagonal). More preferably, the separator plate 9 is a nonporous plate, or the cylinder 9 or the cone cylinder 9 is made of a nonporous plate. More preferably, the tube or cylinder 9 is made of a nonporous plate.

Preferably, two to seven activated carbon chambers (preferably three to five, for example three, four, five, six or seven) at the top pass through each activated carbon channel 10 In communication with the corresponding 2 to 7 (preferably 3 to 5, eg 3, 4, 5, 6 or 7) activated carbon chambers in.

Preferably, at the intermediate position in the vertical direction of the transition zone C, the sum of the cross-sectional areas of all activated carbon channels 10 is equal to or less than the sum of the cross-sectional areas of all activated carbon chambers at the top or the sum of the cross-sectional areas of all activated carbon chambers at the bottom, Preferably the former is 20% to 60% of the latter, preferably 20% to 50%, more preferably 22% to 35%.

The height of the transition zone C of the adsorption tower or the length of the vertical direction of the transition zone C of the adsorption tower is 1 to 5 m, preferably 1.2 to 4 m, more preferably 1.5 to 3 m.

The rolled feeder 6 is preferably arranged at the bottom of each activated carbon chamber at the top. Preferably, the rolled feeder 6 is located in the transition zone C of the adsorption tower and a gap or vertical distance is maintained between the rolled feeder 6 and the activated carbon layer of each activated carbon chamber at the bottom (ie, rolled feeder 6 Roll) does not contact the activated carbon layer of each activated carbon chamber at the bottom).

In general, the height of the main structure of the adsorption tower is 6 to 60 m (meter), preferably 8 to 55 m (meter), preferably 10 to 50 m, preferably 15 to 45 m, 18 to 40 m, preferably 20 to 35 m , 22 to 30 m. The height of the main body structure of the adsorption tower means the height between the inlet and the outlet of the adsorption tower (main body structure).

The ratio of the fill height of the solid adsorption medium or solid adsorbent (such as activated carbon) of the lower activated carbon bed layer portion (A) to the fill (fill) height of the solid adsorption medium or solid adsorbent (such as activated carbon) of the upper activated carbon bed layer portion (B). Is 3: 1 to 1: 3, preferably 2: 1 to 1: 2, preferably 1.8: 1 to 1: 1.8, more preferably 1.5: 1 to 1: 1.5, more preferably 1.2: 1 To 1: 1.2, for example 1: 1.

As used herein, activated carbon refers to generalized activated carbon, including conventional activated carbon, activated coke, carbon-based adsorption media, carbon-based catalysts, and the like. In addition, solid adsorbents or solid adsorption media can also replace generalized activated carbon, which is within the protection scope herein.

In addition, the flue gas herein generally comprises a conventional industrial flue gas or industrial waste gas.

According to the above structural design, in the adsorption column, the descent rate or feed rate of activated carbon, or each residence time of activated carbon of each activated carbon bed layer at the top and each activated carbon bed layer at the bottom can be controlled independently or individually. . Further, during the calm operation, it can be ensured that, in unit time, the total activated carbon supply amount of all activated carbon bed layers at the top is the same as the total activated carbon supply amount of all activated carbon bed layers at the bottom. In addition, the feed may be controlled only by the rolled feeder in the lower activated carbon bed layer portion A (ie, A bed layer). Whatever kind of feed rate control scheme is employed, the moving speed of the solid medium in the front chamber is faster than or equal to the moving speed of the solid medium in the rear chamber.

According to a second solution of the present application, there is provided a flue gas purification method using a flue gas purification method (or flue gas or sintered flue gas desulfurization and denitrification method using the device), the method comprising:

1) transporting flue gas or sintered flue gas (hereinafter collectively referred to as flue gas) to an activated carbon adsorption tower of a desulfurization and denitrification apparatus having an activated carbon adsorption tower and a (conventional) desorption tower, wherein flue gas is Passed sequentially through the lower activated carbon bed layer portion (A) and the upper activated carbon bed layer portion (B) at the top, and transported from the top of the adsorption tower to the lower activated carbon bed layer portion (A) and the upper activated carbon bed layer portion (B). A transportation step, wherein the activated carbon is brought into contact with the activated carbon to adsorb contaminants including sulfur oxides, nitrogen oxides, and dioxins;

2) moving the activated carbon in the activated carbon adsorption tower of the desulfurization and denitrification apparatus which has adsorbed contaminants from the flue gas or the sintered flue gas to a heating zone of the activated carbon desorption tower having a heating zone at the top and a cooling zone at the bottom; Here, activated carbon is heated or elevated to an activated carbon desorption temperature Td (for example, Td = 390 to 450 ° C) by performing indirect heat exchange with a hot gas serving as a heating gas, thereby deactivating and regenerating activated carbon under the temperature Td. A moving step;

3) Activated carbon desorbed and regenerated in the heating zone at the top of the desorption tower is introduced into the cooling zone at the bottom of the desorption tower via an intermediate buffer zone, ie an intermediate section, while from the cooling air inlet of the cooling zone of the desorption tower Introducing and cooling steps by injecting room temperature air (acting as cooling wind or cooling air) into the cooling zone of the cooling zone to cool the activated carbon by performing indirect heat exchange with the activated carbon moving downward in the cooling zone;

4) Cooled activated carbon discharged from the bottom of the desorption tower (e.g. after ash is removed by sieving), from the top of the activated carbon adsorption tower (e. G. Moving to).

In general, the activated carbon regeneration temperature (Td) is 390 to 500 ° C, preferably 400 to 470 ° C, more preferably 405 to 450 ° C, more preferably 410 to 440 ° C, more preferably 410 to 430 ° C. .

Usually, the hot gas introduced into the heating zone of the desorption tower is 400 to 500 ° C., preferably 410 to 480 ° C., more preferably 415 to 470 ° C., more preferably 420 to 460 and even more preferably 420 to 450 Have a temperature in the range of ° C.

In the above method, in the adsorption column, the descent rate or feed rate of the activated carbon, or each residence time of the activated carbon of each activated carbon bed layer in the upper part and each activated carbon bed layer in the lower part can be controlled independently or individually. In addition, in the period of calm operation, the total activated carbon supply amount of all activated carbon bed layers at the upper part is the same as the total activated carbon supply amount of all activated carbon bed layers at the lower part.

The desorption tower according to the present invention is a desorption tower or regeneration tower in a dry desulfurization and denitrification apparatus used for waste gas treatment in the steel industry, and typically has a height of 10 to 40 meters, preferably 15 to 40 meters, more preferably. 20 to 35 meters. The desorption tower usually has a body cross-sectional area of from 6 to 100 m 2, preferably from 8 to 50 m 2, more preferably from 10 to 30 m 2, even more preferably from 15 to 20 m 2. The (desulfurization and denitrification) adsorption tower (or reaction tower) in the desulfurization and denitrification apparatus typically has a tower height of, for example, 6 to 60 m (meters), preferably 8 to 55 m (meters), preferably 10 To 50 m, preferably 15 to 45 m, 18 to 40 m, preferably 20 to 35 m, preferably 22 to 30 m. The tower height of the adsorption tower refers to the height between the activated carbon outlet at the bottom of the adsorption tower and the activated carbon inlet at the top of the adsorption tower, that is, the height of the body structure of the tower.

The design and adsorption techniques for flue gas (or waste gas) adsorption towers are known in the art, for example in US 5932179, JP 2004209332 A, JP 3581090 B2 (JP 2002095930 A), JP 3351658 B2 (JP H 08332347 A) and JP. 2005313035 A, which will not be described in detail herein.

There is no particular requirement for the desorption tower according to the present application, but all of the desorption towers in the prior art can be used herein. Preferably, the desorption tower is a tube-and-shell vertical desorption tower, wherein the activated carbon flows from the top of the tower, passes downward through the pipe side and reaches the bottom of the tower, while heating The gas passes through the shell side, and the heating gas is introduced from the side of the tower, cooled by performing heat exchange with activated carbon passing through the tube side, and then discharged from the other side of the tower. Preferably, the desorption tower is a tube-shell (or shell-tubular) or tube-array vertical desorption tower, where activated charcoal is introduced from the top of the tower and the observation of the heating zone at the top downwards. After passing, it reaches a buffer zone located between the heating zone at the top and the cooling zone at the bottom, then passes the observation of the cooling zone at the bottom and then reaches the bottom of the tower, while heating gas (or High temperature hot gas) is passed through the shell side of the heating zone, and the heating gas (400-500 ° C.) is introduced from the side of the heating zone of the desorption tower and performs indirect heat exchange with the activated carbon passing through the observation of the heating zone. Is cooled and then discharged from the other side of the heating zone of the tower. Cooling air enters from the side of the cooling zone of the desorption tower and undergoes indirect heat exchange with the desorbed and regenerated activated carbon passing through the tube side of the cooling zone. After indirect heat exchange, the cooling air is raised to 120 ± 20 ° C, for example approximately 120 ° C.

Design of activated carbon desorption towers and methods of activated carbon regeneration are disclosed in the literature of many prior art. JP 3217627 B2 (JP H 08155299 A) discloses a desorption tower (i.e. stripping tower) utilizing a double seal valve, inert gas seal, sieve manure and water cooling (see Figure 3 of that patent). JP 3485453 B2 (JP H 11104457 A) discloses a regeneration tower (see FIGS. 23 and 24) that can utilize a preheating section, a double sealed valve, an inert gas, air or water cooling. JP S 59142824 A discloses that the gas from the cooling section is used to preheat the activated carbon. Chinese patent application 201210050541.6 (Shanghai clear science company) has disclosed an energy reuse solution for a regeneration tower using a dryer (2). JP S 4918355 B discloses that blast furnace gas is used for activated carbon regeneration. JP H 08323144 A is used by a regeneration tower using fuel (heavy oil or light oil), and an air heating furnace (11-hot air, 12-fuel supply device, referring to FIG. 2 of the patent). It started to become. Chinese utility model 201320075942.7, referring to FIG. 2 of the utility model, relates to a waste gas treatment device (heated by fuel coal and air) having a heating device and a heating device.

The desorption tower of the present application uses air cooling (air cooling).

When the desorption capacity of the desorption tower is 10 tons of activated carbon per hour, according to the prior art, in order to maintain the temperature of the desorption tower at 420 ° C., the required amount of coke oven gas is approximately 400 Nm 3 / h and the required amount of combustion air is The required temperature of approximately 2200 Nm 3 / h, the exhaust hot gas is approximately 2500 Nm 3 / h, the required amount of cooling air is 3000 Nm 3 / h, and the required temperature of activated carbon after cooling is 140 ° C.

As used herein, with respect to the term "optional," it is indicated whether or not there is an indication of "optional" whether or not to proceed. The terms desorption tower and regeneration tower may be used interchangeably. The terms regeneration and desorption may be used interchangeably. Desorption and stripping also have the same concept. The terms "heating section" and "heating section" have the same concept. The terms "cooling section" and "cooling section" have the same concept.

The thickness of the activated carbon chamber means the distance or spacing between two porous partitions of the activated carbon chamber.

Advantages or advantageous technical effects of the present application are as follows:

1. The adsorption tower according to the present application on the one hand significantly improves the flue gas throughput, on the other hand reduces the manufacturing, operating and maintenance costs of the device, and saves electrical and thermal energy.

2. The process is easy to control, so dead angle of air flow can be avoided.

3. The device is compact and easy to maintain.

4. The residence time of activated carbon is almost the same as the adsorption amount of activated carbon in each part of the adsorption tower, so the utilization rate of activated carbon is high.

5. The present application reduces the initial charge of activated carbon, reduces the investment cost, while also reducing the residence time of activated carbon that is not in contact with the flue gas.

1 is a schematic diagram illustrating a desulfurization and denitrification apparatus and a technical process including an activated carbon adsorption tower and an activated carbon regeneration tower according to the prior art.
2 is a schematic diagram of an adsorption tower according to the prior art.
3 is a schematic view of another adsorption tower according to the prior art.
4 is a schematic view of a adsorption tower of a first type according to the present application.
5 is a schematic view of a adsorption tower of a second type according to the present application.
6 is a schematic view of a third type of adsorption tower according to the present application.

The desulfurization and denitrification apparatus used in the embodiment includes an activated carbon adsorption tower and a desorption tower. The activated carbon desorption tower has an upper heating zone and a lower cooling zone, and an intermediate buffer zone located between them.

The sinter flue gas that needs to be treated in this embodiment is the sinter flue gas from the steel industry.

In this embodiment, the size of the desorption tower has a tower height of 20 m and a body cross section of 15 m ² .

The structures of three types of adsorption towers are shown in FIGS. 4 to 6.

The activated carbon flue gas purification device including the activated carbon adsorption tower is a desulfurization and denitrification device including the activated carbon adsorption tower and the desorption tower, or the activated carbon flue gas purification device including the activated carbon adsorption tower and the desorption tower. The activated carbon adsorption tower comprises a lower activated carbon bed layer portion (A) at the bottom, an upper activated carbon bed layer portion (B) at the bottom, and a transition zone (C) or intermediate zone (C) located between these two portions. The activated carbon adsorption tower comprises a feed canister 3 located above or on top of the adsorption tower, a flue gas inlet 1 located at the bottom of the adsorption tower, and a flue gas outlet 2 located at the top of the adsorption tower. The flue gas outlet end G2 of the lower activated carbon bed layer part A communicates with the flue gas inlet end G3 of the upper activated carbon layer part B through the flue gas channel 5. The lower activated carbon bed layer portion A is divided into two to seven (preferably three to five, for example, three, formed by being divided by the porous partition 4 or by the porous partition 4). Four, five, six or seven activated carbon chambers (eg, there are seven activated carbon chambers sequentially numbered a1, a2, a3, a4, a5, a6, a7, etc.). In addition, along the flue gas flow direction (in this order), the lower activated carbon chambers may sequentially increase in thickness, or along the flue gas flow direction, in the lower part behind the first activated carbon chamber a1 located below. In any two adjacent activated carbon chambers (eg a2 and a3, or a3 and a4), the rear activated carbon chamber (eg a3 or a4) is the front activated carbon chamber (eg a2 or a3). Greater than or equal in thickness. The upper activated carbon bed layer part B is comprised of two to seven (preferably three to five, for example three, formed by being divided by the porous diaphragm 4 or by the porous diaphragm 4). There are four, five, six or seven activated carbon chambers (eg there are seven activated carbon chambers sequentially numbered b1, b2, b3, b4, b5, b6, b7, etc.). Also along the flue gas flow direction, the activated carbon chambers located at the top sequentially increase in thickness, or along the flue gas flow direction, any two at the top behind the first activated carbon chamber b1 located at the top. In adjacent activated carbon chambers (e.g., b2 and b3, or b3 and b4), the rear activated carbon chamber (e.g., b3 or b4) is thicker than the front activated carbon chamber (e.g., b2 or b3). Or the same.

Preferably, flue gas flow direction in two to seven (eg three) activated carbon chambers located at the bottom or in two to seven (eg three) activated carbon chambers located at the top In the order of, the thickness of the second chamber a2 or b2 is 1 to 9 times, for example 1.5 to 7 times, or 2 times, 3 times, 4 times the thickness of the first chamber a1 or b1. Pear, 5 or 6 times. Furthermore, when there is a third chamber a3 or b3, the thickness of the third chamber a3 or b3 is 1 to 2.5 times the thickness of the second chamber a2 or b2, preferably 1.2 to 2 times. Pear, for example 1.3, 1.5 or 1.8 times.

In general, the lower part has three activated carbon chambers and, in the order of flue gas flow direction, the thickness of the first chamber a1, ie the front chamber, is 90 to 250 mm, preferably 100 to 230 mm, for example 120. , 150, 200 or 220 mm; The thickness of the second chamber a2, ie the intermediate chamber, is from 360 to 1000 mm, preferably from 400 to 950 mm, for example 450, 600, 700, 800 or 900 mm; The thickness of the third chamber a3, ie the rear chamber, is 432 to 1200 mm, preferably 450 to 1150 mm, for example 500, 600, 700, 800, 900, 1000 or 1100 mm.

In general, the upper part has three activated carbon chambers, and in the order of the flue gas flow direction, the thickness of the first chamber b1, ie the front chamber, is 90 to 250 mm, preferably 100 to 230 mm, for example 120. , 150, 200 or 220 mm and the thickness of the second chamber b2, ie the intermediate chamber, is from 360 to 1000 mm, preferably from 400 to 950 mm, for example 450, 600, 700, 800 or 900 mm; The thickness of the third chamber b3, ie the rear chamber, is 432 to 1200 mm, preferably 450 to 1150 mm, for example 500, 600, 700, 800, 900, 1000 or 1100 mm.

Preferably, the flue gas inlet 1 located at the bottom of the adsorption tower and the flue gas outlet 2 located at the top of the adsorption tower are located on the same side of the adsorption tower.

Preferably, a roll feeder 6 is arranged at the bottom of each chamber of the lower activated carbon bed layer portion A. As shown in FIG.

Preferably, one or more discharge rotary valves 7 are arranged in the bottom barrel of the adsorption tower.

Generally, for example 2 to 7 activated carbon channels 10 are arranged in the transition zone C, such as a plurality of activated carbon channels 10, 3, 4, 5, 6. Preferably, the activated carbon channel 10 is formed by a separator wall 9 and a tower wall of an adsorption tower, a cylinder 9 having a circular cross section or a cone cylinder 9, a tube having an elliptical cross section or It is formed by the cylinder 9 or by the tube or cylinder 9 which has a cross section of a polygon, for example, triangular or rectangular or pentagonal or hexagonal. More preferably, the separator plate 9 is a nonporous plate, or the cylinder 9 or the cone cylinder 9 is made of a nonporous plate. More preferably, the tube or cylinder 9 is made of a nonporous plate.

Preferably, two to seven activated carbon chambers at the top, preferably three to five, for example three, four, five, six or seven activated carbon chambers are provided at the bottom through each activated carbon channel 10. In communication with the corresponding two to seven activated carbon chambers, preferably three to five, for example three, four, five, six or seven activated carbon chambers.

Preferably, at the intermediate position in the vertical direction of the transition zone C, the sum of the cross-sectional areas of all activated carbon channels 10 is equal to or less than the sum of the cross-sectional areas of all activated carbon chambers at the top or the sum of the cross-sectional areas of all activated carbon chambers at the bottom, Preferably the former is 20% to 60% of the latter, preferably 20% to 50%.

The height of the transition zone C of the adsorption tower or the length of the vertical direction of the transition zone C of the adsorption tower is 1 to 5 m, preferably 1.2 to 4 m, more preferably 1.5 to 3 m.

The rolled feeder 6 is preferably arranged at the bottom of each activated carbon chamber at the top. Preferably, the rolled feeder 6 is located in the transition zone C of the adsorption tower and a gap or vertical distance is maintained between the rolled feeder 6 and the activated carbon layer of each activated carbon chamber at the bottom, ie the rolled feeder 6 The roll of) does not contact the activated carbon layer of each activated carbon chamber at the bottom.

In general, the height of the main structure of the adsorption tower is 6 to 60 m (meter), preferably 8 to 55 m (meter), preferably 10 to 50 m, preferably 15 to 45 m, preferably 18 to 40 m, preferably 20 to 35 m, preferably 22 to 30 m.

According to a second solution of the present application, there is provided a flue gas purification method or a sintered flue gas desulfurization and denitrification method using the apparatus, the method comprising:

1) transporting flue gas (containing contaminants) or sintered flue gas (hereinafter, collectively referred to as flue gas) to the activated carbon adsorption tower of the desulfurization and denitrification apparatus having the above-described activated carbon adsorption tower and (conventional) desorption tower. Wherein flue gas is sequentially passed through the lower activated carbon bed layer portion (A) and the upper activated carbon bed layer portion (B) to come into contact with the activated carbon transported from the top of the adsorption tower to the two portions (A, B), A transport step, wherein the activated carbon adsorbs contaminants including sulfur oxides, nitrogen oxides, and dioxins;

2) moving activated carbon in the activated carbon adsorption tower of the desulfurization and denitrification apparatus which has adsorbed contaminants from flue gas or sintered flue gas to a heating zone of an activated carbon desorption tower having an upper heating zone and a lower cooling zone, wherein the activated carbon is heated A transfer step in which the activated carbon desorption temperature Td (e.g., Td = 390 to 450 ° C) is heated or elevated by performing indirect heat exchange with a hot gas acting as a gas to desorb and regenerate the activated carbon under the temperature Td. Wow;

3) Activated carbon desorbed and regenerated in the upper heating zone of the desorption tower is introduced into the lower cooling zone of the desorption tower via an intermediate buffer zone, ie an intermediate section, while the cooling zone of the desorption tower from the cooling air inlet of the desorption tower cooling zone. An introduction and cooling step of supplying room temperature air (acting as cooling wind or cooling air) to cool the activated carbon by performing indirect heat exchange with activated carbon moving downward in the cooling zone;

4) move the cooled activated carbon discharged from the bottom of the desorption tower after the ash has been removed, for example by sieving, to the top of the activated carbon adsorption tower in step 1), for example at the top of the activated carbon adsorption tower Moving to a supply container of the.

In general, the activated carbon regeneration temperature (Td) is from 390 to 500 ° C, preferably from 400 to 470 ° C, more preferably from 405 to 450 ° C, more preferably from 410 to 440 ° C, more preferably from 410 to 430 ° C. Range.

Usually, the temperature of the hot gas introduced into the heating zone of the desorption tower is 400 to 500 ° C, preferably 410 to 480 ° C, more preferably 415 to 470 ° C, more preferably 420 to 460, more preferably 240 To 450 ° C.

First embodiment

The adsorption tower is shown in FIG. The desulfurization and denitrification apparatus includes an activated carbon adsorption tower (the tower height is 30 meters and the cross section is 120 square meters), and an activated carbon desorption tower (the tower height is 20 meters and the cross section is 15 square meters).

The lower activated carbon bed layer portion A has three activated carbon chambers a1, a2, a3, and the upper activated carbon bed layer portion B has three activated carbon chambers b1, b2, b3.

According to the gas flow direction, according to the order of the respective activated carbon layers which come into contact with the flue gas, the layers are respectively composed of a lower front chamber, a lower middle chamber, a lower rear chamber, an upper front chamber, an upper middle chamber and an upper rear chamber. . The lower front chamber, lower middle chamber and lower rear chamber are 150 mm, 450 mm and 900 mm, respectively, and the total thickness is 1500 mm. The upper front chamber, upper middle chamber and upper rear chamber are 150 mm, 450 mm and 900 mm, respectively, and the total thickness is 1500 mm. Thus, the activated carbon residence time in the front, middle and rear chambers of the upper and lower layers can be controlled, for example, 40 hours, 120 hours or 240 hours.

Upper and lower discharges are adjustable.

The apparatus according to the present embodiment divides the adsorption tower into an upper layer and a lower layer, divides the activated carbon of each layer into a plurality of chambers by a porous partition, and arranges a roll-type feeder at the bottom of each chamber, thereby enabling activated carbon flow in each chamber. The speed (or residence time) is individually controlled.

The activated carbon chamber a1 or b1, which is first in contact with the flue gas, is relatively thin and a relatively fast feed rate is used to discharge the activated carbon saturated by adsorption as soon as possible; The activated carbon chamber which comes into last contact with the flue gas in the layers is relatively thick, and the activated carbon has a long residence time in the chamber, which can effectively reduce the dust concentration in the flue gas.

At the intermediate position in the vertical direction of the transition zone C, the sum of the cross-sectional areas of all activated carbon channels 10 is approximately 55% of the sum of the cross-sectional areas of all activated carbon chambers at the top or the sum of the cross-sectional areas of all activated carbon chambers at the bottom. The height of the transition zone C of the adsorption tower or the length in the vertical direction of the transition zone C of the adsorption tower is 2 m.

After being discharged by the rolled feeder, the upper activated carbon is placed on top of the lower activated carbon chamber and temporarily stored.

Since the lower part of the roll of the roll-type feeder does not come into contact with the activated carbon, it is possible to prevent the high temperature or spark caused by the friction between the circular roll and the activated carbon.

2nd Embodiment

The adsorption tower is shown in FIG. For flue gas having a contaminant composition with little fluctuation, the rolled feeder for supplying the upper layer can be omitted, and the residence time of the material in each layer can be realized by controlling the width of each chamber of the upper and lower layers. The height of the transition zone C of the adsorption tower or the length in the vertical direction of the transition zone C of the adsorption tower is 3 m.

According to the gas flow direction, according to the order of the respective activated carbon layers which come into contact with the flue gas, the layers are respectively defined as a lower front chamber, a lower middle chamber, a lower rear chamber, an upper front chamber, an upper middle chamber and an upper rear chamber. . The lower front chamber, lower middle chamber and lower rear chamber are 150 mm, 450 mm and 900 mm, respectively, and the total thickness is 1500 mm. The upper front chamber, upper middle chamber and upper rear chamber are 150 mm, 450 mm and 900 mm, respectively, and the total thickness is 1500 mm. Thus, the activated carbon residence time in the front, middle and rear chambers of the upper and lower layers can be controlled, for example, 40 hours, 120 hours or 240 hours.

Third embodiment

The adsorption tower is shown in FIG. 6. In order to reduce the initial charge of activated carbon, reduce the investment cost, and to reduce the residence time of activated carbon not in contact with the flue gas, the length of the activated carbon channel between the upper and lower layers can be shortened.

According to the gas flow direction, according to the order of the respective activated carbon layers which come into contact with the flue gas, the layers are respectively defined as a lower front chamber, a lower middle chamber, a lower rear chamber, an upper front chamber, an upper middle chamber and an upper rear chamber. . The lower front chamber, lower middle chamber and lower rear chamber were 150 mm, 450 mm and 900 mm, respectively, with a total thickness of 1500 mm. The upper front chamber, upper middle chamber and upper rear chamber are 150 mm, 450 mm and 900 mm, respectively, and the total thickness is 1500 mm. Thus, the activated carbon residence time in the front, middle and rear chambers of the upper and lower layers can be controlled, for example, 40 hours, 120 hours or 240 hours.

Since the intermediate activated carbon channel 10 is an invalid zone, the height or length of the activated carbon channel and the total cross-sectional area of the activated carbon channel need to be reduced as much as possible, provided that the supply speed of the activated carbon is secured (small resistance). At the intermediate position in the vertical direction of the transition zone C, the sum of the cross sectional areas of all activated carbon channels 10 is approximately 22% of the sum of the cross sectional areas of all activated carbon chambers at the top or the sum of the cross sectional areas of all activated carbon chambers at the bottom. The height of the transition zone C of the adsorption tower or the vertical length of the transition zone C of the adsorption tower is 1.8 m.

A, lower activated carbon bed layer part,
B, part of the upper activated carbon bed layer,
C, transition zone in the middle part of the adsorption tower,
1, flue gas inlet,
2, flue gas outlet,
3, supply barrel,
4, porous plate,
4 ', porous diaphragm or louver,
5, flue gas channel,
6, roll feeder,
7, rotary valve,
8, transportation device,
9, cylinder or cone made of nonporous separator or nonporous plate,
10, activated carbon channel in transition zone (C),
A1, lower first activated carbon chamber
a2, lower second activated carbon chamber
a3, lower third activated carbon chamber
b1, upper first activated carbon chamber
b2, upper second activated carbon chamber,
b3: upper third activated carbon chamber.
G1, the flue gas inlet end of the lower activated carbon bed layer part A,
G2, flue gas outflow end of lower activated carbon bed layer portion (A),
G3, flue gas inlet end of the upper activated carbon bed layer part B,
G4, flue gas outflow end of the upper activated carbon bed layer part (B).

Claims (16)

In the activated carbon flue gas purification device comprising an activated carbon adsorption column,
The activated carbon adsorption tower has a lower activated carbon bed layer portion (A) at the bottom, an upper activated carbon bed layer portion (B) at the top, and the lower activated carbon bed layer portion (A) and the upper activated carbon bed layer portion (B). A transition zone (C) located, wherein the activated carbon adsorption tower comprises a supply vessel (3) located above or on top of the adsorption tower, a flue gas inlet (1) located below the adsorption tower, and Further comprising a flue gas outlet (2) located at the top,
The flue gas outlet end G2 of the lower activated carbon bed layer part A communicates with the flue gas inlet end G3 of the upper activated carbon bed layer part B through the flue gas channel 5, and the lower activated carbon bed layer The portion A has a plurality of activated carbon chambers divided by the porous partition 4, and the upper activated carbon bed layer part B has a plurality of activated carbon chambers divided by the porous partition 4,
The plurality of activated carbon chambers in the upper portion communicate with the corresponding plurality of activated carbon chambers in the lower portion through respective activated carbon channels 10.
Activated Carbon Flue Gas Purifier. The method of claim 1,
The number of the plurality of activated carbon chambers of the lower activated carbon bed layer portion (A) is in the range of 2 to 7, and the number of the plurality of activated carbon chambers of the upper activated carbon bed layer portion (B) is in the range of 2 to 7
Activated Carbon Flue Gas Purifier. The method of claim 2,
The number of the plurality of activated carbon chambers of the lower activated carbon bed layer portion A is in the range of 3 to 5, and the number of the plurality of activated carbon chambers of the upper activated carbon bed layer portion B is in the range of 3 to 5.
Activated Carbon Flue Gas Purifier. The method of claim 2,
The lower activated carbon bed layer portion (A) has a plurality of activated carbon chambers divided by porous partitions (4), and along the flue gas flow direction, the plurality of activated carbon chambers located in the lower portion sequentially increase in thickness, or In any two adjacent activated carbon chambers behind the first activated carbon chamber a1 located below, along the flue gas flow direction, the rear one of the two adjacent activated carbon chambers is greater than the one in front of the two adjacent activated carbon chambers. The thickness is greater than or equal to; The upper activated carbon bed layer part B has a plurality of activated carbon chambers divided by the porous partition 4, and along the flue gas flow direction, the plurality of activated carbon chambers located at an upper portion thereof increase in thickness sequentially, or In any two adjacent activated carbon chambers behind the first activated carbon chamber b1 located above, along the gas flow direction, the rear one of the two adjacent activated carbon chambers is thicker than the front one of the two adjacent activated carbon chambers. Is greater than or equal to
Activated Carbon Flue Gas Purifier. The method of claim 4, wherein
Among the plurality of activated carbon chambers located at the bottom or the plurality of activated carbon chambers located at the top, depending on the order of flue gas flow direction, the thickness of the second chamber is 1 to 9 times the thickness of the first chamber; If there is a third chamber, the thickness of the third chamber is 1 to 2.5 times the thickness of the second chamber.
Activated Carbon Flue Gas Purifier. The method of claim 5,
According to the order of the flue gas flow direction, the thickness of the second chamber is 1.5 to 7 times the thickness of the first chamber; If there is a third chamber, the thickness of the third chamber is 1.2 to 2 times the thickness of the second chamber.
Activated Carbon Flue Gas Purifier. The method of claim 6,
The lower part has three activated carbon chambers, and the thicknesses of the first chamber a1, the second chamber a2, and the third chamber a3 are in the order of 90 to 250 mm and 360 to 300, respectively, in the order of flue gas flow direction. 1000 mm, and in the range of 432 to 1200 mm; And / or
The upper portion has three activated carbon chambers, and the thicknesses of the first chamber b1, the second chamber b2, and the third chamber b3 in the order of flue gas flow direction are 90 to 250 mm and 360 to 360, respectively. 1000 mm, and in the range of 432 to 1200 mm
Activated Carbon Flue Gas Purifier. The method of claim 7, wherein
The thicknesses of the first chamber a1, the second chamber a2, and the third chamber a3 are in the range of 100 to 230 mm, 400 to 950 mm, and 450 to 1150 mm, respectively; And / or
The upper portion has three activated carbon chambers, and the thicknesses of the first chamber b1, the second chamber b2, and the third chamber b3 in the order of flue gas flow direction are 100 to 230 mm and 400 to 400, respectively. 950 mm, and in the range of 450 to 1150 mm
Activated Carbon Flue Gas Purifier. The method according to any one of claims 1 to 8,
The flue gas inlet 1 located at the bottom of the adsorption tower and the flue gas outlet 2 located at the top of the adsorption tower are placed on the same side of the adsorption tower.
Activated Carbon Flue Gas Purifier. The method according to any one of claims 1 to 8,
A rolled feeder 6 is disposed at the bottom of each chamber of the lower activated carbon bed layer portion A; And / or
One or more discharge rotary valves 7 are arranged in the bottom bin of the adsorption tower.
Activated Carbon Flue Gas Purifier. The method according to any one of claims 1 to 8,
A plurality of activated carbon channels 10 are arranged in the transition zone C; The activated carbon channel 10 is formed by the separator wall 9 and the tower wall of the adsorption tower, formed by the cylinder 9 or the cone 9 having a circular cross section, or a tube or cylinder 9 having an elliptical cross section. Or by a tube or cylinder 9 having a polygonal cross section; The separator plate 9 is a nonporous plate, or the cylinder 9 or the cone cylinder 9 is made of a nonporous plate, or the tube or cylinder 9 is made of a nonporous plate.
Activated Carbon Flue Gas Purifier. delete The method according to any one of claims 1 to 8,
At the intermediate position in the vertical direction of the transition zone C, the sum of the cross-sectional areas of all activated carbon channels 10 is less than or equal to the sum of the cross-sectional areas of all activated carbon chambers at the top or the sum of the cross-sectional areas of all activated carbon chambers at the bottom, The former is 20% to 60% of the latter
Activated Carbon Flue Gas Purifier. The method according to any one of claims 1 to 8,
A rolled feeder 6 is arranged at the bottom of each activated carbon chamber at the top; The rolled feeder 6 is located in the transition zone C and a gap or vertical distance is maintained between the rolled feeder 6 and the activated carbon layer of each activated carbon chamber at the bottom.
Activated Carbon Flue Gas Purifier. In the flue gas purification method using the apparatus according to claim 1,
1) transporting flue gas or sintered flue gas to said activated carbon adsorption tower of a desulfurization and denitrification apparatus having an activated carbon adsorption tower and a desorption tower, wherein said flue gas is at the lower activated carbon bed layer portion (A) at the Passing through the upper activated carbon bed layer portion B sequentially, the activated carbon is brought into contact with activated carbon transported from the top of the adsorption tower to the lower activated carbon bed layer portion A and the upper activated carbon bed layer portion B. A transport step to adsorb contaminants including nitrogen oxides and dioxins;
2) moving activated carbon in the activated carbon adsorption tower of the desulfurization and denitrification apparatus which has adsorbed contaminants from flue gas or sintered flue gas to a heating zone of an activated carbon desorption tower having a heating zone at the top and a cooling zone at the bottom; Wherein the activated carbon is heated or raised to an activated carbon desorption temperature Td by performing indirect heat exchange with a hot gas serving as a heating gas, thereby desorbing and regenerating the activated carbon under the temperature Td;
3) Activated carbon desorbed and regenerated in the heating zone at the top of the desorption tower is introduced into the cooling zone at the bottom of the desorption tower via an intermediate buffer zone, i. Injecting and cooling the air by injecting room temperature air into the cooling zone, thereby cooling the activated carbon by performing indirect heat exchange with the activated carbon moving downward in the cooling zone;
4) moving the cooled activated carbon discharged from the bottom of the desorption tower to the top of the activated carbon adsorption tower in step 1) above;
Activated Carbon Flue Gas Purification Method. The method of claim 15,
The activated carbon desorption temperature Td is 390 ℃ to 450 ℃
Activated Carbon Flue Gas Purification Method.

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