CN210645756U - Device for cooperatively treating acid mist in acid production tail gas wet desulphurization - Google Patents
Device for cooperatively treating acid mist in acid production tail gas wet desulphurization Download PDFInfo
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- CN210645756U CN210645756U CN201921248090.0U CN201921248090U CN210645756U CN 210645756 U CN210645756 U CN 210645756U CN 201921248090 U CN201921248090 U CN 201921248090U CN 210645756 U CN210645756 U CN 210645756U
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Abstract
The utility model discloses a device of sour tail gas wet flue gas desulfurization administers acid mist in coordination, inhale the tower including the tail, still including arranging in acid mistA secondary process water tank and a flushing water tank outside the tail absorption tower; the tail gas absorption tower is provided with a tail gas inlet and a tail gas outlet; and a concentration cooling section, an absorption section, an ammonia demisting section and a combined super demister are sequentially arranged in the tail absorption tower according to the tail gas flowing direction between the tail gas inlet and the tail gas outlet. The utility model has the advantages that: the removal rate of acid mist in the tail gas exceeds 90 percent, and the acid mist is controlled to be 25mg/Nm3The following; can also control the sulfur dioxide in the clean tail gas after desulfurization to be 15mg/Nm3Free NH3≤2mg/Nm3。
Description
Technical Field
The utility model belongs to the technical field of the chemical industry is equipped with, especially indicate a device of sour fog is administered in coordination in sour tail gas wet flue gas desulfurization.
Background
At present, the tail gas desulfurization process is mature, but the requirement for acid mist removal is stricter and stricter along with the continuous deepening of the concept of resource recycling. The standard implementation of ion chromatography (HJ544-2016) for measuring the sulfuric acid mist in the waste gas of a fixed pollution source improves the detection requirement of the acid mist, and tail gas (such as sulfuric acid tail gas and the like) containing the acid mist cannot meet the environmental protection requirement through the traditional wet desulphurization. Compared with the prior detection method, the acid mist detection method adds two alkali liquor (NaOH or KOH) impact type absorption bottles for continuous sampling, so that the acid mist content of partial tail gas is increased by multiple times, and the numerical value is dozens of mg/m3Increased to several hundred mg/m3Thus, the requirement for acid mist removal is increased.
(HJ544-2016) sulfuric acid mist definition: "sulfuric acid mist" includes small droplets of sulfuric acid, sulfur trioxide, and soluble sulfates in the particulate matter. "therefore, the control of the acid mist content requires the control of both the inlet acid mist and the soluble sulfate produced during the desulfurization process.
The tail gas inlet temperature is generally below the acid dew point temperature. Gaseous SO3Or H2SO4As the tail gas passes through the desulfurization system, the tail gas is rapidly cooled to below the acid dew point, and the cooling rate is higher than that of the gaseous SO3Or H2SO4The absorption rate by the absorbent in the absorption tower is much faster, SO3Or H2SO4Submicron sulfuric acid mist which is difficult to catch is rapidly formed. Most of the existing tail gas desulfurization devices are concentrated, absorbed, built-in and simply demisted, and cannot meet the environmental protection requirement. The tower top acid mist removal of the tail absorption tower adopts a conventional wet electric demister or a fiber demister. At present, wet-type electric demisting has higher fog drop stripping rate but lower acid mist stripping rate, and single-stage wet-type electric demisting has about acid mist stripping efficiency30-60%, and even the removal rate of acid mist with lower particle size is lower than 30%. Because the tail gas at the outlet of the wet desulphurization is entrained with gas and liquid, water mist and gas-liquid entrainment can be preferentially removed by wet electricity, and the acid mist removal rate is low. Therefore, the acid making tail gas generally needs to be provided with two stages of wet type electric demisters to meet the existing environmental protection requirements, and has the advantages of large investment, large occupied area, high energy consumption and high operation cost; the fiber demister has higher removal rate to acid mist with larger particle size, but the actual removal rate of the fiber demister is less than a theoretical calculated value under the influence of other conditions, (HJ544-2016) standard implementation, the fiber demister is difficult to discharge up to the standard, the fiber demister has large investment, large occupied area, large resistance (possibly needing to transform an induced draft fan or increase a booster fan), and higher operation cost.
SUMMERY OF THE UTILITY MODEL
The to-be-solved technical problem of the utility model is to provide a method for treating acid mist in coordination with acid making tail gas wet desulphurization which can effectively remove acid mist.
In order to solve the technical problem, the utility model discloses a technical scheme does:
a method for cooperatively treating acid mist by wet desulphurization of acid production tail gas comprises the following steps:
(1) spraying tail gas to be treated by using an ammonium sulfate solution with the mass percent concentration of less than 35%, carrying out gas-liquid contact collision, and then carrying out countercurrent contact on the tail gas and an aqueous solution containing ammonium sulfate and ammonium sulfite with the pH value of 2-4 to obtain tail gas at the temperature of 20-30 ℃;
(2) then reacting with an absorption liquid with a pH value of 4-6 to obtain tail gas after tail absorption; the absorption liquid is an aqueous solution containing ammonium sulfate and ammonium sulfite with the mass percentage concentration of 10-25%;
(3) and spraying and washing the tail gas after tail absorption by using an ammonium sulfate aqueous solution with the density of 1.02-1.06 kg/L, then spraying and washing by using an ammonium sulfate aqueous solution with the density of less than 1.02kg/L, and then discharging by using a demisting device.
Preferably, the mass ratio of the ammonium sulfate to the ammonium sulfite in the step (1) or the step (2) is 1-5: 1.
Particularly preferably, the mass ratio of the ammonium sulfate to the ammonia sulfite in the step (1) or the step (2) is 3: 1.
The utility model also provides a device for the acid mist treatment by the acid making tail gas wet desulphurization, which comprises a tail absorption tower, a secondary process water tank and a flushing water tank, wherein the secondary process water tank and the flushing water tank are arranged outside the tail absorption tower; the tail gas absorption tower is provided with a tail gas inlet and a tail gas outlet; a concentration cooling section, an absorption section, an ammonia demisting section and a combined super demister are sequentially arranged in the tail absorption tower according to the tail gas flowing direction between the tail gas inlet and the tail gas outlet;
the combined super demister sequentially comprises a primary demister, a primary demisting section spraying device, a secondary demister spraying device, a tertiary demister and a tertiary demister spraying device according to the flow direction of tail gas; the secondary process water tank is connected with the primary demisting section spraying device through a secondary process water pump; and the flushing water tank is respectively connected with the second-stage demister spraying device and the third-stage demister spraying device through a third flushing water pump.
Preferably, the number of the secondary demisters is three, and the number of the spraying devices of the secondary demisters is matched with that of the secondary demisters; the number of the three-stage demisters is two, and the number of the three-stage demister spraying devices is matched with that of the three-stage demisters.
Preferably, the tail absorption tower also comprises a primary process water tank arranged outside the tail absorption tower; the primary process water tank is respectively communicated with the secondary process water tank and the tail absorption tower through pipelines; and the secondary process water tank is communicated with an external device for containing flushing liquid through a first process water pipe.
Preferably, the tail gas recovery device also comprises a concentration circulation tank which is arranged in the tail gas absorption tower and is positioned below the tail gas inlet;
the concentration cooling section sequentially comprises a concentration cooling section reverse spraying sprayer, a concentration cooling section forward spraying sprayer and a first air lifting disc according to the tail gas flowing direction;
the absorption section comprises a plurality of absorption section spraying devices and a second air lifting disc in sequence according to the tail gas flowing direction;
the ammonia demisting section sequentially comprises an ammonia demister, an ammonia demister section spray device and a third air lifting disc according to the flow direction of the tail gas;
the tail absorption tower is characterized by also comprising an oxidation circulation tank arranged outside the tail absorption tower; the oxidation circulation tank is divided into an absorption circulation tank and an oxidation tank by a clapboard with holes; the absorption circulation tank is respectively communicated with the first gas lifting disc and the ammonia water pipeline through pipelines and is also communicated with the absorption section spraying device through an absorption pump; the oxidation tank is respectively communicated with the absorption section and the concentration circulating tank through pipelines;
the primary process water tank is communicated with the second air lifting disc through a pipeline; the secondary process water tank is communicated with the third gas lifting disc through a pipeline;
the system also comprises a first-stage process water pump; the primary process water pump is respectively communicated with the primary process water tank and the ammonia demister section spray device through pipelines;
the device also comprises a concentration pump; the concentration pump is respectively communicated with the concentration circulating tank and the concentration cooling section reverse spraying sprayer through pipelines;
the device also comprises a delivery pump; the delivery pump is communicated with the concentration circulating tank through a pipeline;
the device also comprises a stirring pump; the stirring pump is respectively communicated with the concentration circulating tank through a pipeline;
the system also comprises a secondary process water pump; and the secondary process water pump is respectively communicated with the secondary process water tank and the primary demisting section spraying device through pipelines.
Preferably, the number of the spraying devices of the absorption section is 3 groups.
Preferably, the flushing water tank is communicated with an external device for containing flushing liquid through a second process water pipe.
By adopting the technical scheme, through the contact collision of solutions with different pH values, the high-density and low-density ammonium sulfate aqueous solution is combined for water washing and demisting, the detection is carried out by the standard of 'ion chromatography for measuring the waste gas sulfuric acid mist of the fixed pollution source' (HJ544-2016), compared with the tail gas at the gas inlet, the removal rate of the acid mist in the tail gas at the gas outlet exceeds 90 percent, the removal rate of the acid mist completely meets the acid mist removal requirement of the latest standard, and the acid mist is controlled at 25mg/Nm3The following. Can also control the sulfur dioxide in the clean tail gas after desulfurization to be 15mg/Nm3Free NH3≤2mg/Nm3. In order to improve the acid mist removal rate and the desulfurization rate from the source and reduce the acid mist, the aerosol and the free ammonia, an external oxidation circulation tank is independently arranged; equipment type selection can be more reasonably carried out according to different tail gas conditions, and investment is reduced; the height of the tail absorption tower is reduced, the energy consumption is reduced, and the tail absorption tower is suitable for different SO2Concentration and acid mist concentration.
Drawings
Fig. 1 is a schematic structural diagram of the present invention.
In the figure, 1-tail absorption tower, 2-tail gas inlet, 3-concentration circulation tank, 5-concentration cooling section, 6-concentration cooling section reverse spray sprayer, 7-concentration cooling section forward spray sprayer, 8-first air lifting disc, 9-absorption section, 10-absorption section spray device, 11-second air lifting disc, 12-ammonia demisting section, 13-ammonia demister, 14-ammonia demister section spray device, 15-third air lifting disc, 16-combined super demister, 17-first-stage demister, 18-first-stage demisting section spray device, 19-second-stage demister, 20-second-stage demister spray device, 21-third-stage demister, 22-third-stage demister spray device, 23-tail gas outlet, 24-oxidation circulation tank, 25-absorption pump, 26-an absorption circulating tank, 27-a perforated partition board, 28-an oxidation tank, 29-a primary process water tank, 30-a primary process water pump, 31-a concentration pump, 32-a delivery pump, 33-a stirring pump, 34-a secondary process water tank, 35-a secondary process water pump, 36-a flushing water tank, 37-a third washing water pump, 38-a first process water pipe, 39-a second process water pipe and 40-an ammonia water pipe.
Detailed Description
The following describes the present invention with reference to the accompanying drawings. It should be noted that the description of the embodiments is provided to help understanding of the present invention, but the present invention is not limited thereto. In addition, the technical features related to the embodiments of the present invention described below may be combined with each other as long as they do not conflict with each other.
Example 1
A method for cooperatively treating acid mist by wet desulphurization of acid production tail gas comprises the following steps:
(1) removing in a concentration section; spraying tail gas to be treated (at 70-100 ℃) by using an ammonium sulfate solution with the mass percent concentration of less than 35%, carrying out gas-liquid contact collision, and then carrying out countercurrent contact with an aqueous solution containing ammonium sulfate and ammonium sulfite with the pH value of 3 to obtain the tail gas with the temperature of 20-30 ℃; the mass ratio of the ammonium sulfate to the ammonium sulfite is 3: 1.
(2) Removing in an absorption section; then reacting with absorption liquid with pH value of 5 to obtain tail gas after tail absorption; the absorption liquid is an aqueous solution containing ammonium sulfate and ammonium sulfite with the mass percentage concentration of 20%; the mass ratio of the ammonium sulfate to the ammonium sulfite is 3: 1.
(3) Removing in a washing demisting section; and spraying and washing the tail gas after tail absorption by using an ammonium sulfate aqueous solution with the density of 1.02-1.06 kg/L, then spraying and washing by using an ammonium sulfate aqueous solution with the density of less than 1.02kg/L, and then discharging by using a demisting device.
Example 2
A method for cooperatively treating acid mist by wet desulphurization of acid production tail gas comprises the following steps:
(1) removing in a concentration section; spraying tail gas to be treated (at 70-100 ℃) by using an ammonium sulfate solution with the mass percent concentration of less than 35%, carrying out gas-liquid contact collision, and then carrying out countercurrent contact with an aqueous solution containing ammonium sulfate and ammonium sulfite with the pH value of 4 to obtain the tail gas with the temperature of 20-30 ℃; the mass ratio of the ammonium sulfate to the ammonium sulfite is 5: 1.
(2) Removing in an absorption section; then reacting with absorption liquid with pH value of 6 to obtain tail gas after tail absorption; the absorption liquid is 25% aqueous solution containing ammonium sulfate and ammonium sulfite by mass percentage; the mass ratio of the ammonium sulfate to the ammonium sulfite is 5: 1.
(3) Removing in a washing demisting section; and spraying and washing the tail gas after tail absorption by using an ammonium sulfate aqueous solution with the density of 1.02-1.06 kg/L, then spraying and washing by using an ammonium sulfate aqueous solution with the density of less than 1.02kg/L, and then discharging by using a demisting device.
Example 3
A method for cooperatively treating acid mist by wet desulphurization of acid production tail gas comprises the following steps:
(1) removing in a concentration section; spraying tail gas to be treated (at 70-100 ℃) by using an ammonium sulfate solution with the mass percent concentration of less than 35%, carrying out gas-liquid contact collision, and then carrying out countercurrent contact with an aqueous solution containing ammonium sulfate and ammonium sulfite with the pH value of 2 to obtain the tail gas with the temperature of 20-30 ℃; the mass ratio of the ammonium sulfate to the ammonium sulfite is 1: 1.
(2) Removing in an absorption section; then reacting with absorption liquid with pH value of 4 to obtain tail gas after tail absorption; the absorption liquid is 10% aqueous solution containing ammonium sulfate and ammonium sulfite by mass percentage; the mass ratio of the ammonium sulfate to the ammonium sulfite is 1: 1.
(3) Removing in a washing demisting section; and spraying and washing the tail gas after tail absorption by using an ammonium sulfate aqueous solution with the density of 1.02-1.06 kg/L, then spraying and washing by using an ammonium sulfate aqueous solution with the density of less than 1.02kg/L, and then discharging by using a demisting device.
In the above embodiment, the removal rate of the acid mist in the tail gas at the gas outlet exceeds 90% relative to the tail gas at the gas inlet, which is detected by the standard of ion chromatography for measuring the sulfuric acid mist in the waste gas of the fixed pollution source (HJ544-2016), and completely meets the acid mist removal requirement of the latest standard, and the acid mist is controlled at 25mg/Nm3The following.
Wherein, the acid mist removal efficiency of the concentration section is 30-35%, the acid mist removal efficiency of the absorption section is 40-45%, and the acid mist removal efficiency of the washing demisting section is 75-80%.
In order to embody the technical effects of the utility model, the following experiment is specially made to compare.
Comparative example 1
On the basis of the embodiment 1, in the stage of concentration section removal, other conditions are unchanged, ammonium sulfate solution with mass percent concentration of more than 35% is selected to contact and collide with higher temperature (70-100 ℃) tail gas to be treated, and ammonium sulfate solution with mass percent concentration of 36%, 37%, 38%, 39% and 40% is specifically selected.
Experiments show that the ammonium sulfate solution is crystallized along with the increase of the concentration, so that the acid mist removal efficiency of the concentration section is low, and is within about 15 percent, and the efficiency does not have a linear relation along with the difference of the concentration. Compared with the acid mist removal efficiency within 35 percent, the acid mist removal efficiency is remarkably reduced, and the final tail gas does not meet the latest standard.
Comparative example 2
On the basis of example 1, in the stage of concentration section removal, other conditions are not changed, and the tail gas is countercurrently contacted by an aqueous solution containing ammonium sulfate and ammonia sulfite, wherein the pH value of the aqueous solution is less than 2 or more than 4. Specifically, a pH of 1.5, 1, 4.5 or 5 is selected.
Tests show that when the pH value is less than 2, the acidity is too strong, equipment is easy to corrode, the acid mist removal efficiency of the concentration section is within 25%, and finally the tail gas does not meet the latest standard. When the pH value is more than 4, the acid mist removal efficiency of the concentration section is within 20 percent, and finally the tail gas does not meet the latest standard. Therefore, the acid mist removal efficiency does not show a linear relation along with the increase of the pH value, and the change of the pH value has obvious influence on the acid mist removal.
Comparative example 3
In addition to example 1, in the concentration section removal stage, other conditions were not changed, and different mass ratios of ammonium sulfate to ammonia sulfite were selected when the tail gas was countercurrently contacted with an aqueous solution containing ammonium sulfate and ammonia sulfite. When the mass ratio of the ammonium sulfate to the ammonia sulfite is more than 5:1 or the mass ratio of the ammonium sulfate to the ammonia sulfite is less than 1: 1. Specifically, the mass ratio of ammonium sulfate to ammonium sulfite is selected to be 6:1 or 7:1, and the ammonium sulfate concentration is too high, so that crystallization is easy to occur, acid mist absorption is not facilitated, and the acid mist removal efficiency is low and is about within 25%; when the mass ratio of ammonium sulfate to ammonium sulfite is 1:2 or 1:3, the concentration of ammonium sulfite is too high, which results in a decrease in oxidation efficiency and the generation of new acid mist while removing acid mist, and thus the concentration of ammonium sulfite cannot be too high. Therefore, the mass ratio of the ammonium sulfate to the ammonium sulfite can obviously influence the removal efficiency of the acid mist and influence whether the final tail gas meets the requirements of new standards.
Comparative example 4
On the basis of example 1, in the stage of absorption section removal, other conditions are not changed, and absorption liquid with pH value less than 4 or more than 6 is selected for reaction. Specifically, a pH of 3, 3.5, 6.5 or 7 is selected.
Tests show that when the pH value is less than 4, the acid mist removal efficiency is within 31 percent, and finally the tail gas does not meet the latest standard. When the pH value is more than 6, the acid mist removal efficiency is within 24 percent, and finally the tail gas does not meet the latest standard. Therefore, the acid mist removal efficiency does not show a linear relation along with the increase of the pH value, and the change of the pH value of the absorption liquid has obvious influence on the acid mist removal.
Comparative example 5
On the basis of example 1, in the stage of desorption in the absorption section, other conditions are unchanged, and an aqueous solution containing ammonium sulfate and ammonium sulfite with the mass percent concentration of the absorption liquid being less than 10%, or an aqueous solution containing ammonium sulfate and ammonium sulfite with the mass percent concentration of the absorption liquid being more than 25% is selected for research. Specifically, 35%, 30%, 28%, 8%, 5% or 1% is selected.
Tests show that ammonia escapes when the mass percentage concentration of the absorption liquid is more than 25%, and new acid mist is generated after the acid mist is removed, so that the selection is not suitable. When the mass percentage concentration of the absorption liquid is less than 10%, the acid mist removal efficiency is within 30%, and finally the tail gas does not meet the latest standard.
Comparative example 6
On the basis of example 1, in the stage of the absorption section desorption, other conditions are not changed, and different mass ratios of ammonium sulfate and ammonia sulfite are selected in the absorption liquid. When the mass ratio of the ammonium sulfate to the ammonia sulfite is more than 5:1 or the mass ratio of the ammonium sulfate to the ammonia sulfite is less than 1: 1. Specifically, the mass ratio of ammonium sulfate to ammonium sulfite is selected to be 6:1 or 7:1, and the ammonium sulfate concentration is too high, so that crystallization is easy to occur, acid mist absorption is not facilitated, and the acid mist removal efficiency is low and is about within 28%; when the mass ratio of ammonium sulfate to ammonium sulfite is 1:2 or 1:3, the concentration of ammonium sulfite is too high, which results in a decrease in oxidation efficiency and the generation of new acid mist while removing acid mist, and thus the concentration of ammonium sulfite cannot be too high. Therefore, the mass ratio of the ammonium sulfate to the ammonium sulfite can obviously influence the removal efficiency of the acid mist and influence whether the final tail gas meets the requirements of new standards.
Comparative example 7
On the basis of example 1, in the stage of removing in the demisting section of water washing, other conditions are unchanged, firstly, the water is sprayed and washed by the ammonium sulfate aqueous solution with the density of less than 1.02 or more than 1.06kg/L, and then the water is sprayed and washed by the ammonium sulfate aqueous solution with the density of less than 1.02 kg/L.
Tests show that the ammonium sulfate aqueous solution of more than 1.06kg/L is sprayed and washed, is easy to crystallize, is not beneficial to removing acid mist, and has low acid mist removing efficiency within about 32 percent; the ammonium sulfate aqueous solution less than 1.02kg/L is sprayed and washed, which is not beneficial to removing acid mist, and the acid mist removing efficiency is low, and is about within 40 percent.
Comparative example 8
On the basis of the embodiment 1, in the stage of removing in the water washing demisting section, other conditions are unchanged, firstly, the water washing is carried out by spraying the ammonium sulfate aqueous solution with the density of 1.02-1.06 kg/L, and then, the water washing is carried out by spraying the ammonium sulfate aqueous solution with the density of more than 1.02 kg/L.
Tests show that the spraying and water washing of the ammonium sulfate aqueous solution of more than 1.02kg/L is not beneficial to removing acid mist, the acid mist removing efficiency is low and is about within 45 percent, and finally the tail gas does not meet the requirements of new standards.
In summary, it can be seen that the efficiency of acid mist removal is affected by changes in different processes or changes in technical parameters, so that the tail gas treatment does not meet the requirements of new standards. Therefore, the acid mist can be effectively removed only by the mutual cooperation of the working procedures.
The efficiency for cooperating the acid mist desorption is higher, combines the utility model provides a process has still studied the device of desorption acid mist. As shown in fig. 1, an apparatus for removing acid mist by using the method of any one of embodiments 1 to 3 comprises a tail absorption tower 1, and further comprises a secondary process water tank 34 and a rinsing water tank 36 which are arranged outside the tail absorption tower 1; the tail absorption tower 1 is provided with a tail gas inlet 2 and a tail gas outlet 23; a concentration cooling section 5, an absorption section 9, an ammonia demisting section 12 and a combined super demister 16 are sequentially arranged in the tail absorption tower 1 according to the tail gas flowing direction between the tail gas inlet 2 and the tail gas outlet 23;
the combined super demister 16 sequentially comprises a primary demister 17, a primary demisting section spraying device 18, a secondary demister 19, a secondary demister spraying device 20, a tertiary demister 21 and a tertiary demister spraying device 22 according to the flow direction of the tail gas; the secondary process water tank 34 is connected with the primary demisting section spraying device 18 through a secondary process water pump 35; the washing water tank 36 is respectively connected with the second-stage demister spray device 20 and the third-stage demister spray device 22 through a third washing water pump 37.
Specifically, in order to improve the demisting effect, the number of the secondary demisters 19 is three, and the number of the secondary demister spray devices 20 is matched with the number of the secondary demisters 19; the number of the three-stage demisters 21 is two, and the number of the three-stage demister spray devices 22 is matched with the number of the three-stage demisters 21.
The tail absorption tower also comprises a primary process water tank 29 arranged outside the tail absorption tower 1; the primary process water tank 29 is respectively communicated with the secondary process water tank 34 and the tail absorption tower 1 through pipelines; the secondary process water tank 34 is in communication with an external device for holding rinse liquid via a first process water line 38.
The tail gas absorption tower also comprises a concentration circulating tank 3 which is arranged in the tail gas absorption tower 1 and is positioned below the tail gas inlet 2; the concentration cooling section 5 comprises a concentration cooling section reverse spraying sprayer 6, a concentration cooling section forward spraying sprayer 7 and a first air lifting disc 8 in sequence according to the tail gas flowing direction; the absorption section 9 comprises a plurality of absorption section spraying devices 10 and a second air lifting disc 11 in sequence according to the tail gas flowing direction; the ammonia demisting section 12 sequentially comprises an ammonia demister 1), an ammonia demister section spray device 14 and a third air lifting disc 15 according to the flow direction of the tail gas;
also comprises an oxidation circulation tank 24 arranged outside the tail absorption tower 1; the oxidation circulation tank 24 is divided into an absorption circulation tank 26 and an oxidation tank 28 by a perforated partition plate 27; the absorption circulation tank 26 is respectively communicated with the first air lifting disc 8 and the ammonia water pipeline 40 through pipelines, and is also communicated with the absorption section spray device 10 through an absorption pump 25; the oxidation tank 28 is respectively communicated with the absorption section 9 and the concentration circulating tank 3 through pipelines; the primary process water tank 29 is communicated with the second air lifting disc 11 through a pipeline; the secondary process water tank 34 is communicated with the third air lifting disc 15 through a pipeline;
also includes a first-stage process water pump 30; the primary process water pump 30 is respectively communicated with the primary process water tank 29 and the ammonia demister section spray device 14 through pipelines;
also included is a concentrate pump 31; the concentration pump 31 is respectively communicated with the concentration circulating tank 3 and the concentration cooling section reverse spraying sprayer 6 through pipelines;
a delivery pump 32; the delivery pump 32 is communicated with the concentration circulating tank 3 through a pipeline;
also included is a mixing pump 33; the stirring pump 33 is respectively communicated with the concentration circulating tank 3 through pipelines;
a secondary process water pump 35; the secondary process water pump 35 is respectively communicated with the secondary process water tank 34 and the primary demisting section spray device 18 through pipelines.
Specifically, the number of the absorption stage spray devices 10 is 3. The rinse water tank 36 communicates with an external device for holding rinse water via a second process water pipe 39.
Through the utility model discloses the combined action of technology and device, acid mist dropout rate is high (more than or equal to 90%), and desulfurization efficiency is high (more than or equal to 99%), discharges tail gas SO2 and is less than or equal to 15mg/Nm3, and the acid mist is less than or equal to 25mg/Nm3, and free NH3 is less than or equal to 2mg/Nm3, and the sub-salt can not detect out when the by-product is sent outside with the thiamine solution, and the by-product thiamine is after the drying, and product quality can reach "ammonium sulfate (GB535) first-class article. The equipment type can be selected according to different tail gas conditions, and the investment is reduced.
The embodiments of the present invention have been described in detail with reference to the accompanying drawings, but the present invention is not limited to the described embodiments. It will be apparent to those skilled in the art that various changes, modifications, substitutions and alterations can be made in the embodiments without departing from the principles and spirit of the invention, and the scope of the invention is to be accorded the full scope of the claims.
Claims (6)
1. The utility model provides a device of sour tail gas wet flue gas desulfurization is administered acid mist in coordination which characterized in that: comprises a tail absorption tower (1), and also comprises a secondary process water tank (34) and a flushing water tank (36) which are arranged outside the tail absorption tower (1); the tail gas absorption tower (1) is provided with a tail gas inlet (2) and a tail gas outlet (23); a concentration cooling section (5), an absorption section (9), an ammonia demisting section (12) and a combined super demister (16) are sequentially arranged in the tail absorption tower (1) according to the tail gas flowing direction between the tail gas inlet (2) and the tail gas outlet (23);
the combined super demister (16) sequentially comprises a primary demister (17), a primary demisting section spraying device (18), a secondary demister (19), a secondary demister spraying device (20), a tertiary demister (21) and a tertiary demister spraying device (22) according to the flow direction of the tail gas; the secondary process water tank (34) is connected with the primary demisting section spraying device (18) through a secondary process water pump (35) by a pipeline; and the washing water tank (36) is respectively connected with the second-stage demister spraying device (20) and the third-stage demister spraying device (22) through a third washing water pump (37) by pipelines.
2. The apparatus of claim 1, wherein: the number of the secondary demisters (19) is three, and the number of the secondary demister spraying devices (20) is matched with the number of the secondary demisters (19); the number of the three-stage demisters (21) is two, and the number of the three-stage demister spraying devices (22) is matched with that of the three-stage demisters (21).
3. The apparatus of claim 1, wherein: the tail absorption tower also comprises a primary process water tank (29) arranged outside the tail absorption tower (1); the primary process water tank (29) is respectively communicated with the secondary process water tank (34) and the tail absorption tower (1) through pipelines; the secondary process water tank (34) is communicated with an external device for containing washing liquid through a first process water pipe (38).
4. The apparatus of claim 3, wherein: the tail gas absorption tower also comprises a concentration circulating groove (3) which is arranged in the tail gas absorption tower (1) and is positioned below the tail gas inlet (2);
the concentration cooling section (5) sequentially comprises a concentration cooling section reverse spraying sprayer (6), a concentration cooling section forward spraying sprayer (7) and a first air lifting disc (8) according to the tail gas flowing direction;
the absorption section (9) comprises a plurality of absorption section spraying devices (10) and a second air lifting disc (11) in sequence according to the tail gas flowing direction;
the ammonia demisting section (12) sequentially comprises an ammonia demister (13), an ammonia demister section spray device (14) and a third air lifting disc (15) according to the flow direction of the tail gas;
the tail absorption tower also comprises an oxidation circulation tank (24) arranged outside the tail absorption tower (1); the oxidation circulation tank (24) is divided into an absorption circulation tank (26) and an oxidation tank (28) by a clapboard (27) with holes; the absorption circulation tank (26) is respectively communicated with the first air lifting disc (8) and the ammonia water pipeline (40) through pipelines, and is also communicated with the absorption section spraying device (10) through an absorption pump (25); the oxidation tank (28) is respectively communicated with the absorption section (9) and the concentration circulating tank (3) through pipelines;
the primary process water tank (29) is communicated with the second air lifting disc (11) through a pipeline; the secondary process water tank (34) is communicated with the third air lifting disc (15) through a pipeline;
the system also comprises a primary process water pump (30); the primary process water pump (30) is respectively communicated with the primary process water tank (29) and the ammonia demister section spray device (14) through pipelines;
also comprises a concentration pump (31); the concentration pump (31) is respectively communicated with the concentration circulating tank (3) and the concentration cooling section reverse spraying sprayer (6) through pipelines;
also comprises a delivery pump (32); the delivery pump (32) is communicated with the concentration circulating tank (3) through a pipeline;
also comprises a stirring pump (33); the stirring pump (33) is respectively communicated with the concentration circulating tank (3) through a pipeline;
the system also comprises a secondary process water pump (35); and the secondary process water pump (35) is respectively communicated with the secondary process water tank (34) and the primary demisting section spraying device (18) through pipelines.
5. The apparatus of claim 4, wherein: the number of the absorption section spray devices (10) is 3 groups.
6. The apparatus of claim 4, wherein: the rinsing water tank (36) is communicated with an external device for containing rinsing liquid through a second process water pipe (39).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN110280105A (en) * | 2019-08-02 | 2019-09-27 | 亚太环保股份有限公司 | The method and device of acid mist is administered in a kind of relieving haperacidity tail gas wet method desulfurization collaboration |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN110280105A (en) * | 2019-08-02 | 2019-09-27 | 亚太环保股份有限公司 | The method and device of acid mist is administered in a kind of relieving haperacidity tail gas wet method desulfurization collaboration |
| CN110280105B (en) * | 2019-08-02 | 2024-03-26 | 亚太环保股份有限公司 | Method and device for cooperatively treating acid mist by wet desulfurization of acid making tail gas |
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