CN209310573U - A kind of purification of Analytic Tower heat supply hot-air system discharged gas fume and waste-heat recovery device - Google Patents

Abstract

A kind of purification of Analytic Tower heat supply hot-air system discharged gas fume and waste-heat recovery device, the device include Analytic Tower, hot-blast stove, hot air circulation blower, heat exchanger.Analytic Tower includes the bringing-up section on top and the cooling section of lower part.Wherein, the hot-blast outlet of hot-blast stove is connected to the bringing-up section gas access of heating pars infrasegmentalis via first pipe.The bringing-up section gas vent on bringing-up section top is connected to the hot-wind inlet of hot-blast stove via second pipe.Second pipe is equipped with hot air circulation blower.Third pipeline is separated from second pipe, third pipeline is connected to the heat transferring medium entrance of heat exchanger.The utility model rationally utilizes Analytic Tower discharged gas fume waste heat, while removing the harmful substance in discharged gas fume.

Description

A device for purification of flue gas exhausted from the heat supply and hot air system of the analytical tower and waste heat recovery device

technical field

The utility model relates to a device for purifying flue gas and recovering waste heat, in particular to a device for purifying flue gas and recovering waste heat outside a heating and air system of an analysis tower, and belongs to the field of purifying flue gas and utilizing waste heat.

Background technique

The flue gas activated carbon (activated coke) desulfurization technology of the sintering and coking process of iron and steel enterprises, the activated carbon (activated coke) of this technology needs to be heated to a certain temperature (usually about 430°C) in the desorption tower for desulfurization, and the activated carbon will absorb the acidic substance SO ₂ When it is released, the ability of activated carbon to absorb acidic substances will be restored, and the released sulfur-rich gas can be directly used for acid production. In this process, the desorption tower needs an external heat source.

In order to improve the heat supply efficiency of the external heat supply source, the desorption tower usually adopts the heat supply method of hot flue gas circulation. The circulating hot air system supporting the desorption tower, the temperature of the circulating flue gas entering the desorption tower is about 450 ℃, and the temperature of the desorption tower is about 340 ℃. Coal gas is used as fuel, and the high-temperature flue gas generated by combustion in the hot blast stove is directly mixed with the circulating flue gas. After mixing, the flue gas must meet the heat supply requirements of the desorption tower. Due to the increase in the amount of flue gas after mixing, the pressure of the circulation pipeline system will increase accordingly. In order to ensure the stability of the pipeline pressure, a flue gas release pipeline is installed on the pipeline. Through the pipeline pressure detection, the regulating valve of the release pipeline is controlled. The opening can discharge the same volume of flue gas outside. In order to reduce heat loss, the evacuation pipe is usually installed in the low-temperature section of the flue gas, specifically on the pipe before the outlet of the desorption tower and the circulation fan. The exhausted flue gas is consistent with the amount of new high-temperature flue gas required after fuel combustion, accounting for about 10-15% of the total circulation. At present, the emission of the project is to use the chimney to discharge directly, and the waste heat resources carried by this part of the external flue gas are wasted. At the same time, although the amount of exhausted flue gas is not large, the content and concentration of harmful substances in the flue gas cannot meet the emission requirements because no treatment has been carried out.

In the prior art, the amount of circulating flue gas exhausted is relatively small. At present, similar projects adopt chimney direct discharge. The temperature of the diffused flue gas is about 300°C, the gas volume is small, the flue gas temperature is low, the fluctuation is large, and the utilization of waste heat is limited. At the same time, considering the addition of waste heat utilization in the release pipeline, in order to ensure a sufficient amount of flue gas discharge, the resistance of the pipeline will inevitably increase, which may outweigh the gain for the entire circulation pipeline.

Utility model content

Aiming at the deficiencies of the above-mentioned prior art, the purpose of the utility model is to rationally utilize the waste heat of the exhausted combustion flue gas and effectively remove harmful substances in the exhausted flue gas. The utility model provides a device for purifying exhausted flue gas and recovering waste heat in a heat supply and hot air system of an analysis tower. The device is provided with a heat exchanger on the discharge pipeline to preheat the combustion-supporting air of the hot blast stove, and then discharges the flue gas in the discharge pipeline. Mixed with the original sintering flue gas, under the action of the sintering booster fan, the diffused flue gas and the original sintering flue gas enter the adsorption tower for purification.

Since the total amount of vented flue gas is less than 1% of the original sintering flue gas, the introduction of vented flue gas will not have any impact on the desulfurization and denitrification process of sintering flue gas. That is, on the premise of not adding facilities, the exhausted flue gas is purified, and the harmful substances in the flue gas are removed to the maximum; at the same time, the waste heat resources of the exhausted flue gas are also rationally utilized.

According to the embodiment of the present utility model, a device for purifying flue gas exhausted from the heat supply and hot air system of the analytical tower and recovering waste heat is provided:

A device for purifying flue gas exhausted from a heat-supply hot air system of a desorption tower and utilizing waste heat, the device comprising a desorption tower, a hot blast stove, a hot blast circulation fan, and a heat exchanger. The desorption tower includes an upper heating section and a lower cooling section. Wherein, the hot blast outlet of the hot blast stove is connected to the gas inlet of the heating section at the lower part of the heating section via the first pipeline. The gas outlet of the heating section on the upper part of the heating section is connected to the hot blast inlet of the hot blast stove through the second pipeline. The second pipeline is provided with a hot air circulation fan. A third pipeline is branched from the second pipeline, and the third pipeline is connected to the heat exchange medium inlet of the heat exchanger.

Preferably, the device also includes an adsorption tower. The adsorption tower is provided with the flue gas inlet of the adsorption tower. The flue gas inlet of the adsorption tower is connected with the original flue gas conveying pipeline. The sixth pipe leading from the heat exchange medium outlet of the heat exchanger is connected to the raw flue gas delivery pipe.

Preferably, the heat exchange gas inlet on the heat exchanger is connected with the combustion-supporting gas pipeline. The heat exchange gas outlet on the heat exchanger is connected to the supplementary air outlet of the hot blast stove through the fourth pipeline.

The heat exchanger is used for indirect heat exchange between the heat exchange medium (ie, hot flue gas) and the heat exchange gas (ie, air).

Preferably, a combustion-supporting fan is provided on the combustion-supporting gas pipeline.

Preferably, the position where the third pipeline is separated from the second pipeline is located upstream of the hot air circulation fan.

Preferably, the device also includes a booster fan. The booster fan is arranged on the original flue gas conveying pipeline.

Preferably, the position where the sixth pipeline is connected to the raw flue gas delivery pipeline is located upstream of the booster fan.

Preferably, the heat exchanger is a tube heat exchanger; preferably a metal tube heat exchanger.

In the present utility model, the top of the adsorption tower is provided with an inlet for the activated carbon of the adsorption tower, and the bottom of the adsorption tower is provided with an outlet for the activated carbon of the adsorption tower. The top of the analysis tower is provided with the inlet of the activated carbon of the analysis tower, and the bottom of the analysis tower is provided with the outlet of the activated carbon of the analysis tower.

Wherein, the activated carbon outlet of the adsorption tower is connected with the activated carbon inlet of the desorption tower through the first conveyor, and the activated carbon outlet of the desorption tower is connected with the activated carbon inlet of the adsorption tower through the second conveyor.

In the utility model, the device also includes a cooling fan. The lower part of the cooling section of the desorption tower is provided with a cooling section gas inlet, and the upper part of the cooling section is provided with a cooling section gas outlet. The air outlet of the cooling fan is connected to the gas inlet of the cooling section via the seventh pipeline.

In the present invention, the desorption tower further includes a transition section between the heating section and the cooling section. An SRG gas outlet is provided on the side wall of the transition section.

Preferably, the SRG gas outlet is delivered to the acid system through the SRG gas delivery pipeline.

Preferably, the device further includes a chimney; the flue gas outlet of the adsorption tower is connected to the chimney through a flue gas discharge pipe.

Activated carbon dry process is currently the main promotion technology for sintering flue gas purification treatment, which can simultaneously realize desulfurization, denitrification, dioxin removal, heavy metal removal and dust removal in the process of sintering flue gas purification. In the flue gas purification process of the utility model, after the flue gas exhausted from the heat supply and hot air system of the analysis tower is preheated by the heat exchanger to the combustion air of the hot blast stove, under the action of the sintering booster fan, it is mixed with various pollutants The original sintering flue gas is mixed and enters the adsorption tower for purification treatment. After the activated carbon in the adsorption tower absorbs and purifies the flue gas, it is transported to the desorption tower through the first conveyor. After being decomposed in the desorption tower, the activated carbon is transported to the adsorption tower through the second conveyor to complete a complete material cycle.

The main purpose of the desorption tower is to heat and regenerate the activated carbon that has adsorbed pollutants. The desorption tower includes an upper heating section and a lower cooling section, and the heating section and the cooling section have a shell-and-tube or tube-and-tube heat exchanger structure. The activated carbon passes through the tube side of the heating section and the cooling section respectively, while the heating gas passes through the shell side in the heating section, and the cooling air passes through the shell side in the cooling section. There is a transition section containing activated carbon between the heating section and the cooling section. The side wall of the transition section is provided with an SRG gas outlet, and the SRG gas is transported to the acid system through a pipeline.

The heat used to heat the regenerated activated carbon in the desorption tower comes from the combustion heat of blast furnace gas or coke oven gas or other substances, such as hot blast furnace exhaust or hot air or hot air. The hot air enters the desorption tower from the gas inlet of the heating section of the desorption tower, and The desorbed activated carbon performs indirect heat exchange. The temperature of the hot air entering the desorption tower is 400-500°C, preferably 410-470°C, more preferably 430-450°C, and the exhaust temperature of the gas outlet of the heating section after heat exchange is 300-380°C, preferably 320-375°C , more preferably 340-370°C. Usually, the hot air enters the desorption tower to exchange heat indirectly with the activated carbon, and the hot air after the heat exchange is heated by the hot air stove for recycling. In order to maintain the stability of the pressure and oxygen content in the hot air circulation system, the utility The low-temperature air section (i.e. the second pipeline) draws the third pipeline, and part of the hot air (5-40%, preferably 8-30%, more preferably 10-20%) after the heat exchange with the activated carbon is discharged, and at the same time A heat exchanger is arranged on the third pipe to effectively use the heat of this part of the externally discharged hot air to preheat the combustion-supporting air of the hot blast stove (or input water from the outside to heat it, and even provide steam). After heat exchange, the exhaust temperature of the gas outlet in the heating section is relatively high, and the combustion-supporting air can usually be preheated to 120-180°C (for example, 150°C). Generally, the consumption of coke oven gas can be reduced by 10-20%.

As a preference, this part of the hot air exhausted from the hot air circulation system passes through the heat exchanger to exchange heat with the combustion-supporting air, and then, under the action of the sintering booster fan, introduces the original flue gas delivery pipeline to mix with the original sintering flue gas, and enters the adsorption tower together. Purification treatment, on the one hand, can effectively remove harmful substances in this part of the hot air, on the other hand, because the negative pressure of the flue in front of the sintering booster fan is very large, it can reduce the internal pressure of the hot air circulation system, thereby effectively solving the third problem. The problem of increased pipeline resistance after the pipeline is set to utilize waste heat.

In the heat-supply hot air system of the analytical tower, the amount of flue gas discharged through the third pipe is about 10-15% of the circulation amount, but because the amount of exhaust gas is far less than the amount of the original sintering flue gas to be treated (entering the activated carbon adsorption tower flue gas volume), so mixing this part of the exhausted flue gas with the original sintering flue gas and entering the adsorption tower for treatment will not have any impact on the desulfurization and denitrification process of the sintering flue gas. That is, on the premise of not adding facilities, the exhaust gas is purified, and harmful substances such as SO ₂ in the flue gas are removed to the maximum extent.

In the device of the utility model, the part of the hot air discharged from the hot air supply system of the analysis tower through the third pipe passes through the heat exchanger to preheat the combustion air of the hot blast stove, and then mixes with the original sintering flue gas and enters the adsorption tower for purification treatment, which changes the In the prior art, there is a technical solution for directly discharging the part of the hot air. On the one hand, through the purification treatment of the adsorption tower, the pollution of SO2 and other harmful substances in the hot air to the environment is avoided _; at the same time, because the temperature of this part of the hot air is relatively high, the combustion-supporting air of the hot blast stove is preheated by the heat of this part of the hot air and then Participating in combustion, the waste heat of this part of hot air can be rationally utilized, and the consumption of coke oven gas can also be reduced. Of course, there are many ways to utilize the waste heat of this part of the hot air. In addition to preheating the combustion-supporting air of the hot blast stove, it can also provide hot water or even steam.

In addition, in the prior art, due to the direct discharge of part of the circulating hot air, in order to control the amount of harmful substances such as _SO2 , only a very small part of the hot air can be discharged, which restricts the heat exchange efficiency between the circulating hot air and activated carbon; Since the amount of hot air exhausted outside is consistent with the amount of new high-temperature flue gas required after fuel combustion, the amount of hot air exhausted outside is less, and the amount of combustion-supporting air supplemented into the hot blast stove is also small. Therefore, in this scheme, the hot blast stove is always in low oxygen State combustion, resulting in fuel can not be fully burned, resulting in waste of resources. With the design of this application, since the part of the exhausted hot air is mixed with the original sintering flue gas and then enters the adsorption tower for treatment, and then discharged from the chimney after treatment, the amount of hot air transported to the adsorption tower can be increased as required Therefore, a larger amount of air can be added from the air inlet of the hot blast stove, which increases the oxygen content in the hot blast stove, improves the combustion rate of the fuel, makes it fully combustible, and saves fuel resources; at the same time, due to the full combustion of the fuel, the heat The higher value also improves the heat exchange efficiency between the hot air and activated carbon after the hot air transported from the hot air stove enters the desorption tower.

In this application, "parse" and "regenerate" are used interchangeably. "Analysis tower heating and hot air system" and "analysis tower hot air circulation system" are the same concept. "Exhausting hot air outside the analysis tower" and "exhausting flue gas outside the analysis tower" are the same concept.

Compared with the prior art, the utility model has the following beneficial effects:

1. In the utility model, a heat exchanger is arranged on the release pipeline (that is, the third pipeline) to preheat the combustion-supporting air of the hot blast stove, making full use of the waste heat resources of the external flue gas exhausted by the heat supply and hot air system of the desorption tower;

2. In this utility model, after preheating the combustion-supporting air of the hot blast furnace, the flue gas exhausted from the heating and hot air system of the analysis tower is mixed with the original sintering flue gas, and then enters the adsorption tower for purification treatment together, without increasing the facilities. Under the premise, the harmful substances in the exhausted flue gas are removed to the greatest extent;

3. Since the negative pressure of the flue in front of the sintering booster fan is very large, the utility model introduces the flue gas exhausted from the heating and hot air system of the analysis tower into the original flue in front of the sintering booster fan, which can reduce the internal pressure of the hot air circulation system, thereby Effectively solve the disadvantages of increased pipeline resistance after the exhaust pipeline (that is, the third pipeline) is set for waste heat utilization;

4. In the utility model, the combustion-supporting air of the hot blast stove is preheated and then participates in combustion, which saves 10-20% of coke oven gas consumption and reduces the emission of harmful substances.

Description of drawings

Fig. 1 is a structural schematic diagram of the exhaust gas purification and waste heat recovery device of the utility model for the heat supply and hot air system of the analytical tower.

Reference signs:

A: desorption tower; A01: activated carbon inlet of desorption tower; A02: activated carbon outlet of desorption tower; 1: hot blast furnace; 101: hot air inlet; 102: hot air outlet; 103: supplementary air outlet; 2: hot air circulation fan; 3: heat exchanger ;301: Heat exchange medium inlet; 302: Heat exchange gas outlet; 303: Heat exchange gas inlet; 304: Heat exchange medium outlet; 4: Combustion fan; 5: Heating section; 501: Heating section gas inlet; 502: Heating section Gas outlet; 6: cooling section; 601: gas inlet of cooling section; 602: gas outlet of cooling section; 7: adsorption tower; 701: flue gas inlet of adsorption tower; 702: flue gas outlet of adsorption tower; 703: activated carbon inlet of adsorption tower; 704: activated carbon outlet of adsorption tower; 8: booster fan; 9: first conveyor; 10: second conveyor; 11: cooling fan; 12: transition section; 1201: SRG gas outlet; 13: chimney;

L0: original flue gas pipeline; L1: first pipeline; L2: second pipeline; L3: third pipeline; L4: fourth pipeline; L5: combustion-supporting gas pipeline; L6: sixth pipeline; L7: seventh pipeline; L8: SRG gas delivery pipe; L9: flue gas discharge pipe.

Detailed ways

According to the embodiment of the present utility model, a device for purifying flue gas exhausted from the heat supply and hot air system of the analytical tower and recovering waste heat is provided:

A device for purifying flue gas exhausted from a heat-supply hot air system of a desorption tower and utilizing waste heat, the device comprising a desorption tower A, a hot blast stove 1, a hot air circulation fan 2, and a heat exchanger 3. The desorption tower A includes an upper heating section 5 and a lower cooling section 6 . Wherein, the hot blast outlet 102 of the hot blast stove 1 is connected to the gas inlet 501 of the heating section at the lower part of the heating section 5 via the first pipeline L1. The heating section gas outlet 502 on the heating section 5 top is connected to the hot blast inlet 101 of the hot blast stove 1 via the second pipeline L2. A hot air circulation fan 2 is provided on the second pipeline L2. A third pipeline L3 is branched from the second pipeline L2, and the third pipeline L3 is connected to the heat exchange medium inlet 301 of the heat exchanger 3 .

Preferably, the device also includes an adsorption tower 7 . The adsorption tower 7 is provided with an adsorption tower flue gas inlet 701 . The flue gas inlet 701 of the adsorption tower is connected to the raw flue gas delivery pipeline L0. The sixth pipeline L6 drawn from the heat exchange medium outlet 304 of the heat exchanger 3 is connected to the raw flue gas transmission pipeline L0.

Preferably, the heat exchange gas inlet 303 on the heat exchanger 3 is connected to the combustion-supporting gas pipeline L5. The heat exchange gas outlet 302 on the heat exchanger 3 is connected to the supplementary air outlet 103 of the hot blast stove 1 through the fourth pipeline L4.

The heat exchanger 3 is used for indirect heat exchange between the heat exchange medium (ie, the hot flue gas output from the heating section of the desorption tower) and the heat exchange gas (ie, air). The hot flue gas is used to preheat the air in the heat exchanger 3 , and the preheated air is input into the hot blast stove 1 .

Preferably, a combustion-supporting blower 4 is provided on the combustion-supporting gas pipeline L5.

Preferably, the location where the third pipeline L3 branches off from the second pipeline L2 is located upstream of the hot air circulation fan 2 .

Preferably, the device also includes a booster blower 8 . The booster fan 8 is arranged on the raw flue gas conveying pipeline L0.

Preferably, the position where the sixth pipeline L6 is connected to the raw flue gas delivery pipeline L0 is located upstream of the booster fan 8 .

Preferably, the heat exchanger 3 is a tube heat exchanger; preferably a metal tube heat exchanger.

In the present utility model, the top of the adsorption tower 7 is provided with an inlet 703 for the activated carbon of the adsorption tower, and the bottom of the adsorption tower 7 is provided with an outlet 704 for the activated carbon of the adsorption tower. The top of the analysis tower A is provided with the inlet A01 of the activated carbon of the analysis tower, and the bottom of the analysis tower A is provided with the outlet A02 of the activated carbon of the analysis tower.

Wherein, the activated carbon outlet 704 of the adsorption tower is connected with the activated carbon inlet A01 of the analysis tower through the first conveyor 9, and the activated carbon outlet A02 of the analysis tower is connected with the activated carbon inlet 703 of the adsorption tower through the second conveyor 10.

In the present invention, the device also includes a cooling fan 11 . The lower part of the cooling section 6 of the desorption tower A is provided with a cooling section gas inlet 601 , and the upper part of the cooling section 6 is provided with a cooling section gas outlet 602 . The air outlet of the cooling fan 11 is connected to the gas inlet 601 of the cooling section via the seventh pipeline L7.

In the present invention, the desorption tower A further includes a transition section 12 between the heating section 5 and the cooling section 6 . An SRG gas outlet 1201 is provided on the side wall of the transition section 12 .

Preferably, the SRG gas outlet 1201 is delivered to the acid production system through the SRG gas delivery pipeline L8.

Preferably, the device further includes a chimney 13; the adsorption tower flue gas outlet 702 of the adsorption tower 7 is connected to the chimney 13 via the flue gas discharge pipe L9.

Example 1

As shown in FIG. 1 , a device for purifying flue gas exhausted from a heat-supply hot air system of a desorption tower and utilizing waste heat, the device includes a desorption tower A, a hot blast stove 1 , a hot air circulation fan 2 , and a heat exchanger 3 . The desorption tower A includes an upper heating section 5 and a lower cooling section 6 . Wherein, the hot blast outlet 102 of the hot blast stove 1 is connected to the gas inlet 501 of the heating section at the lower part of the heating section 5 via the first pipeline L1. The heating section gas outlet 502 on the upper part of the heating section 5 is connected to the hot blast inlet 101 of the hot blast stove 1 via the second pipeline L2. A hot air circulation fan 2 is provided on the second pipeline L2. A third pipeline L3 is branched from the second pipeline L2, and the third pipeline L3 is connected to the heat exchange medium inlet 301 of the heat exchanger 3 .

The device also includes an adsorption tower 7 . The top of the adsorption tower 7 is provided with an adsorption tower activated carbon inlet 703, and the bottom of the adsorption tower 7 is provided with an adsorption tower activated carbon outlet 704. The top of the analysis tower A is provided with the inlet A01 of the activated carbon of the analysis tower, and the bottom of the analysis tower A is provided with the outlet A02 of the activated carbon of the analysis tower. The device also includes a first conveyor 9 for transporting the activated carbon to be regenerated from the activated carbon outlet 704 of the adsorption tower to the activated carbon inlet A01 of the desorption tower. The device also includes a second conveyor 10 for transporting the regenerated activated carbon from the activated carbon outlet A02 of the desorption tower to the activated carbon inlet 703 of the adsorption tower.

The device also includes a cooling fan 11 . The lower part of the cooling section 6 of the desorption tower A is provided with a cooling section gas inlet 601 , and the upper part of the cooling section 6 is provided with a cooling section gas outlet 602 . The air outlet of the cooling fan 11 is connected to the gas inlet 601 of the cooling section via the seventh pipeline L7.

The desorption tower A also includes a transition section 12 between the heating section 5 and the cooling section 6 . An SRG gas outlet 1201 is provided on the side wall of the transition section 12 . The SRG gas outlet 1201 is delivered to the acid production system through the SRG gas delivery pipeline L8.

The heat exchanger 3 is a metal tube heat exchanger.

Example 2

Repeat Example 1, except that the adsorption tower 7 is provided with an adsorption tower flue gas inlet 701 . The flue gas inlet 701 of the adsorption tower is connected to the raw flue gas delivery pipeline L0. The sixth pipeline L6 drawn from the heat exchange medium outlet 304 of the heat exchanger 3 is connected to the raw flue gas transmission pipeline L0.

Example 3

Embodiment 2 is repeated, except that the heat exchange gas inlet 303 on the heat exchanger 3 is connected to the combustion-supporting gas pipeline L5. The heat exchange gas outlet 302 on the heat exchanger 3 is connected to the supplementary air outlet 103 of the hot blast stove 1 via the fourth pipeline L4. A combustion-supporting fan 4 is provided on the combustion-supporting gas pipeline L5.

Example 4

Embodiment 3 is repeated, except that the position where the third pipeline L3 is branched from the second pipeline L2 is located upstream of the hot air circulation fan 2 . The device also includes a booster blower 8 . The booster fan 8 is arranged on the raw flue gas conveying pipeline L0. The position where the sixth pipeline L6 is connected to the raw flue gas delivery pipeline L0 is located upstream of the booster fan 8 .

Example 5

Repeat Example 4, except that the device also includes a chimney 13; the adsorption tower flue gas outlet 702 of the adsorption tower 7 is connected to the chimney 13 via the flue gas discharge pipe L9.

Use the device of embodiment 4 to process the sintering flue gas, wherein, 10% of the gas discharged from the hot blast outlet 502 of the desorption tower is connected to the heat exchanger 3 through the third pipeline L3, and this part of the gas is connected to the heat exchanger 3 in the heat exchanger 3. The combustion-supporting air used to add the circulating gas to the hot blast stove 1 is used for heat exchange. The combustion-supporting air can be preheated to about 150° C., and then participates in the combustion in the heat exchanger 3 . Using the device of this embodiment, compared with the prior art of adding normal temperature air, can save about 10% of the gas consumption in the hot blast stove.

At the same time, the medium gas after heat exchange is transported to the original flue gas pipeline L0 through the sixth pipeline L6, and this part of the gas is processed through the activated carbon adsorption tower to avoid the direct discharge of polluted flue gas and protect the environment.

Claims (27)

1. a kind of Analytic Tower heat supply hot-air system discharged gas fume purification and waste-heat recovery device, which includes Analytic Tower (A), heat Wind furnace (1), hot air circulation blower (2), heat exchanger (3)；Analytic Tower (A) includes the cooling section of bringing-up section (5) and lower part on top (6)；Wherein, the hot-blast outlet (102) of hot-blast stove (1) is connected to the bringing-up section of bringing-up section (5) lower part via first pipe (L1) The bringing-up section gas vent (502) of gas access (501), bringing-up section (5) top is connected to hot-blast stove via second pipe (L2) (1) hot-wind inlet (101)；Second pipe (L2) is equipped with hot air circulation blower (2)；Third is separated from second pipe (L2) Pipeline (L3), third pipeline (L3) are connected to the heat transferring medium entrance (301) of heat exchanger (3).

2. gas cleaning according to claim 1 and waste-heat recovery device, it is characterised in that: the device further includes adsorption tower (7)；Adsorption tower (7) is equipped with adsorption tower smoke inlet (701), adsorption tower smoke inlet (701) and former smoke conveying duct (L0) it connects；The 6th pipeline (L6) drawn from the heat transferring medium of heat exchanger (3) outlet (304) is connected to former smoke conveying duct (L0)。

3. gas cleaning according to claim 1 or 2 and waste-heat recovery device, it is characterised in that: changing on heat exchanger (3) Heater gas inlet port (303) is connect with combustion gas duct (L5), and the recuperated gas outlet (302) on heat exchanger (3) is via the 4th Pipeline (L4) is connected to the wind-supplying mouth (103) of hot-blast stove (1).

4. gas cleaning according to claim 3 and waste-heat recovery device, it is characterised in that: on combustion gas duct (L5) Equipped with combustion fan (4).

5. gas cleaning according to claim 3 and waste-heat recovery device, it is characterised in that: divide from second pipe (L2) The position of third pipeline (L3) is located at the upstream of hot air circulation blower (2) out；And/or

The device further includes booster fan (8), and booster fan (8) is arranged on former smoke conveying duct (L0).

6. gas cleaning according to claim 4 and waste-heat recovery device, it is characterised in that: divide from second pipe (L2) The position of third pipeline (L3) is located at the upstream of hot air circulation blower (2) out；And/or

The device further includes booster fan (8), and booster fan (8) is arranged on former smoke conveying duct (L0).

7. gas cleaning according to claim 5 or 6 and waste-heat recovery device, it is characterised in that: the 6th pipeline (L6) is even The position for being connected to former smoke conveying duct (L0) is located at the upstream of booster fan (8).

8. according to claim 1-2, gas cleaning and waste-heat recovery device described in any one of 4-6, it is characterised in that: described Heat exchanger (3) is pipe heat exchanger.

9. gas cleaning according to claim 3 and waste-heat recovery device, it is characterised in that: the heat exchanger (3) is pipe Formula heat exchanger.

10. gas cleaning according to claim 7 and waste-heat recovery device, it is characterised in that: the heat exchanger (3) is pipe Formula heat exchanger.

11. gas cleaning according to claim 8 and waste-heat recovery device, it is characterised in that: the heat exchanger (3) is gold Belong to pipe heat exchanger.

12. gas cleaning according to claim 9 or 10 and waste-heat recovery device, it is characterised in that: the heat exchanger (3) For metal pipe type heat exchanger.

13. gas cleaning according to claim 2 and waste-heat recovery device, it is characterised in that: the top of the adsorption tower (7) Portion is equipped with adsorption tower active carbon entrance (703), and the bottom of adsorption tower (7) is equipped with adsorption tower active carbon outlet (704)；Analytic Tower (A) top is equipped with Analytic Tower active carbon entrance (A01), and the bottom of Analytic Tower (A) is equipped with Analytic Tower active carbon outlet (A02)；

Wherein, adsorption tower active carbon outlet (704) is connect by the first conveyer (9) with Analytic Tower active carbon entrance (A01), is solved Analysis tower active carbon outlet (A02) is connect by second conveyor (10) with adsorption tower active carbon entrance (703).

14. according to claim 1-2, gas cleaning and waste-heat recovery device described in any one of 4-6,9-11,13, feature Be: the device further includes cooling blower (11)；The lower part of the cooling section (6) of Analytic Tower (A) is equipped with cooling section gas access (601), the top of cooling section (6) is equipped with cooling section gas vent (602)；The air outlet of cooling blower (11) is via the 7th pipeline (L7) cooling section gas access (601) are connected to.

15. gas cleaning according to claim 3 and waste-heat recovery device, it is characterised in that: the device further includes cooling Blower (11)；The lower part of the cooling section (6) of Analytic Tower (A) is equipped with cooling section gas access (601), and the top of cooling section (6) is set There are cooling section gas vent (602)；The air outlet of cooling blower (11) is connected to cooling section gas via the 7th pipeline (L7) and enters Mouth (601).

16. gas cleaning according to claim 7 and waste-heat recovery device, it is characterised in that: the device further includes cooling Blower (11)；The lower part of the cooling section (6) of Analytic Tower (A) is equipped with cooling section gas access (601), and the top of cooling section (6) is set There are cooling section gas vent (602)；The air outlet of cooling blower (11) is connected to cooling section gas via the 7th pipeline (L7) and enters Mouth (601).

17. gas cleaning according to claim 8 and waste-heat recovery device, it is characterised in that: the device further includes cooling Blower (11)；The lower part of the cooling section (6) of Analytic Tower (A) is equipped with cooling section gas access (601), and the top of cooling section (6) is set There are cooling section gas vent (602)；The air outlet of cooling blower (11) is connected to cooling section gas via the 7th pipeline (L7) and enters Mouth (601).

18. according to claim 1-2, gas cleaning and waste-heat recovery device described in any one of 4-6,9-11,13,15-17, It is characterized by: the Analytic Tower (A) further includes the changeover portion (12) between bringing-up section (5) and cooling section (6)；Changeover portion (12) Side wall be equipped with SRG gas vent (1201).

19. gas cleaning according to claim 3 and waste-heat recovery device, it is characterised in that: the Analytic Tower (A) is also Including the changeover portion (12) between bringing-up section (5) and cooling section (6)；The side wall of changeover portion (12) is equipped with SRG gas vent (1201)。

20. gas cleaning according to claim 7 and waste-heat recovery device, it is characterised in that: the Analytic Tower (A) is also wrapped Include the changeover portion (12) between bringing-up section (5) and cooling section (6)；The side wall of changeover portion (12) is equipped with SRG gas vent (1201)。

21. gas cleaning according to claim 8 and waste-heat recovery device, it is characterised in that: the Analytic Tower (A) is also wrapped Include the changeover portion (12) between bringing-up section (5) and cooling section (6)；The side wall of changeover portion (12) is equipped with SRG gas vent (1201)。

22. gas cleaning according to claim 18 and waste-heat recovery device, it is characterised in that: the SRG gas vent (1201) acid making system is delivered to by SRG gas transmission pipeline (L8).

23. gas cleaning and waste-heat recovery device described in any one of 9-21 according to claim 1, it is characterised in that: described SRG gas vent (1201) is delivered to acid making system by SRG gas transmission pipeline (L8).

24. the gas cleaning according to any one of claim 2,4-6,9-11,13,15-17,19-22 and waste heat recycling Device, it is characterised in that: the device further includes chimney (13)；The adsorption tower exhanst gas outlet (702) of adsorption tower (7) is arranged via flue gas It puts pipeline (L9) and is connected to chimney (13).

25. gas cleaning according to claim 3 and waste-heat recovery device, it is characterised in that: the device further includes chimney (13)；The adsorption tower exhanst gas outlet (702) of adsorption tower (7) is connected to chimney (13) via flue gas exhausting pipe line (L9).

26. gas cleaning according to claim 7 and waste-heat recovery device, it is characterised in that: the device further includes chimney (13)；The adsorption tower exhanst gas outlet (702) of adsorption tower (7) is connected to chimney (13) via flue gas exhausting pipe line (L9).

27. gas cleaning according to claim 8 and waste-heat recovery device, it is characterised in that: the device further includes chimney (13)；The adsorption tower exhanst gas outlet (702) of adsorption tower (7) is connected to chimney (13) via flue gas exhausting pipe line (L9).