CN218924284U - Ammonia desulfurization system for recycling dilute sulfuric acid - Google Patents
Ammonia desulfurization system for recycling dilute sulfuric acid Download PDFInfo
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- CN218924284U CN218924284U CN202223005303.1U CN202223005303U CN218924284U CN 218924284 U CN218924284 U CN 218924284U CN 202223005303 U CN202223005303 U CN 202223005303U CN 218924284 U CN218924284 U CN 218924284U
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Abstract
The utility model discloses an ammonia desulfurization system for recycling dilute sulfuric acid, which comprises a sulfuric acid storage tank, wherein an alkali liquor tank is connected with the top of the sulfuric acid storage tank, an acid discharging pump is introduced into the bottom of the sulfuric acid storage tank, the sulfuric acid storage tank is respectively connected with a concentration tank, a recovery pump and a washing tank through pipelines, and a plurality of valves and acid adding pumps are arranged on the pipelines. According to the utility model, by adopting a system for adding dilute sulfuric acid into each section of the desulfurization tower, the pH of circulating liquid in each section of desulfurization can be effectively controlled, so that the crystallization effect of ammonium sulfate is improved, the quality qualification rate of ammonium sulfate products is ensured to be more than 99.5%, the tailing phenomenon of smoke plume is eliminated, and the escaped ammonia amount is obviously reduced; the ammonia amount escaped before adding acid is 14mg/m and 2. The ammonia amount escaped after adding acid is reduced to 1mg/m, and the ammonia amount is stably controlled below 3 mg/m.
Description
Technical Field
The utility model belongs to the field of environmental protection, and particularly relates to an ammonia desulfurization system for recycling dilute sulfuric acid.
Background
The ammonia desulfurization process is to remove the SO-containing gas after the boiler is denitrated and dedusted 2 The flue gas is contacted with ammonium sulfate solution in a desulfurizing tower, and the flue gas is subjected to concentration and absorption stages successively, and the flue gas is cooled to obtain SO therein 2 The ammonia added circulating liquid is absorbed to form ammonium sulfite, and the flue gas is washed and purified, and is sent to a chimney for discharge after wet electric precipitation. Oxidizing and concentrating ammonium sulfite to obtain ammonium sulfate slurry with solid content less than or equal to 10%, cyclone concentrating, vacuum filtering and packing to obtain ammonium sulfate product.
In the process, the flue gas subjected to denitration enters a concentration section for cooling, the pH of a concentrated solution is influenced by the denitration ammonia adding amount, fluctuation is easy to occur uncontrollably, no adjustment means is adopted, the pH of the concentrated solution is too high to cause crystallization thinning of ammonium sulfate, the crystallization quality of ammonium sulfate is influenced, and the influence on the moisture of the ammonium sulfate is synchronously caused. The pH value of ammonium sulfate solution in the upper recovery section and the washing section of the desulfurizing tower is high, the absorption effect on escaped ammonia in flue gas is reduced, the content of escaped ammonia at the outlet of the desulfurizing tower is directly increased, the length of the flue gas plume at the outlet of the desulfurizing tower is influenced, and adverse environmental protection is caused.
The prior art research CN217312686U discloses an ammonia desulfurization device for controlling ammonia escape, and an online pH meter is utilized to monitor the bottom (NH 4 ) 2 SO 3 The pH value of (2) is controlled to be 3-3.5, so that (NH) 4 ) 2 SO 3 The ammonia content of the catalyst is controlled, and the volatilization of ammonia is reduced. Adding oxygen branch line at bottom of concentrated layer to give concentrated layerMiddle (NH) 4 ) 2 SO 3 Sufficient oxygen is added to increase (NH) 4 ) 2 SO 3 Oxidation rate, can be converted into stable (NH) 4 ) 2 SO 3 . The ammonia desulfurization device for controlling ammonia escape is characterized in that the ammonia desulfurization device is provided with the online pH value, the pH value of an absorption section is monitored to control the escape ammonia, the concentration section, the absorption section, a recovery section and a washing section of the ammonia desulfurization device are all provided with the online pH value, and pH indexes of each section are formulated, so that the ammonia desulfurization device can be used for monitoring and cannot effectively cope with the abnormal condition of the escape ammonia.
The prior art CN217391828U discloses an ammonium sulfate byproduct treatment combined device suitable for treating chemical tail gas, which comprises a horizontal sedimentation tank, a vertical sedimentation tank, a buffer tank, a sludge filter pressing system, a connecting pump, a sludge pump, a reflux pump, a transfer pump and a basket filter; the slurry outlet of the ammonium sulfate slurry tank is connected with the slurry inlet of the basket filter; the slurry outlet of the basket filter is connected with the slurry inlet of the connecting pump; the slurry outlet of the connecting pump is connected with the slurry inlet of the advection type sedimentation tank; the slurry outlet of the horizontal flow sedimentation tank is connected with the slurry inlet of the vertical flow sedimentation tank; the slurry outlet of the vertical flow sedimentation tank is connected with the slurry inlet of the buffer tank; the slurry outlet of the buffer tank is connected with the slurry inlet of the sludge tank; the slurry outlet of the sludge tank is connected with the slurry inlet of the advection type sedimentation tank; the sludge outlet of the sludge pond is connected with the sludge inlet of the sludge pump; the sludge outlet of the sludge pump is connected with the sludge inlet of the sludge filter pressing system; the mud outlet of the horizontal sedimentation tank, the mud outlet of the vertical sedimentation tank and the mud outlet of the buffer tank are all connected with the mud inlet of the transfer pump, and the mud outlet of the transfer pump is connected with the mud inlet of the sludge tank; the inlet of the reflux pump is connected with the slurry outlet of the buffer tank, and the outlet of the reflux pump is connected with the slurry inlet of the ammonium sulfate evaporation crystallization drying packaging system and the slurry inlet of the ammonium sulfate slurry tank. The above "ammonium sulfate byproduct treatment combined device suitable for chemical tail gas treatment" eliminates physical impurities in ammonium sulfate liquid by means of basket filters and sludge pumps, thereby improving ammonium sulfate crystallization effect, and each circulating pump of the existing ammonia desulfurization device is provided with a basket filter, when the circulating liquid (NH 4 ) 2 SO 3 When the content is increased, the crystallization effect of ammonium sulfate and the moisture of ammonium sulfate cannot be effectively ensured.
Disclosure of Invention
In order to utilize the advantages of integration and resource utilization of a chemical industry park, waste sulfuric acid generated in the production process of methane chloride is utilized in an ammonia desulfurization process, so that ammonia escaping from discharged flue gas is eliminated, the crystallization effect of ammonium sulfate is improved, and the quality of ammonium sulfate products is improved.
According to the utility model, by adopting a system for adding dilute sulfuric acid into each section of the desulfurization tower, the pH of circulating liquid in each section of desulfurization can be effectively controlled, so that the crystallization effect of ammonium sulfate is improved, the quality qualification rate of ammonium sulfate products is ensured to be more than 99.5%, the tailing phenomenon of smoke plume is eliminated, and the escaped ammonia amount is obviously reduced; the ammonia amount is reduced to 14mg/m before adding acid, the ammonia amount is reduced to 1mg/m after adding acid, and the ammonia amount is stably controlled below 3 mg/m.
In order to achieve the above purpose, the present utility model adopts the following technical scheme:
the ammonia desulfurization system for recycling dilute sulfuric acid comprises a sulfuric acid storage tank, wherein an alkali liquor tank is connected with the top of the sulfuric acid storage tank, an acid discharging pump is introduced into the bottom of the sulfuric acid storage tank, the sulfuric acid storage tank is respectively connected with a concentration tank, a recovery pump and a washing tank through pipelines, and a plurality of valves and acid adding pumps are arranged on the pipelines.
Further, the sulfuric acid storage tank is arranged on the other pipeline in parallel, and a valve is arranged on the pipeline.
Further, two acid pumps are arranged in parallel. One path is used as standby.
Further, the concentration tank, the recovery pump and the washing tank are provided with 3 groups, and the concentration tank and the washing tank are further provided with two groups.
The beneficial effects of the utility model are as follows:
the system (dilute sulfuric acid consumed by ammonia desulfurization) fully utilizes the desulfurizing tower, enables the sulfuric acid originally containing part of organic matters to react in the desulfurizing tower, optimizes the ammonia desulfurization operation by utilizing the related advantages, and reduces the ammonia escape of the difficult problem of ammonia desulfurization.
(1) The system adds a small amount of sulfuric acid in the desulfurization tower concentration section, and the existing boiler is generally matched with SCR denitration, because the activity of a catalyst is reduced, ammonia escape of denitration flue gas is increased, so that escaped ammonia can enter the desulfurization tower concentration section to damage concentration crystallization, the ammonium sulfate generation environment is unstable, sulfuric acid is added at the moment, the granularity of crystallization can be increased by controlling the acidity, and the problem of ammonium sulfate quality fluctuation is solved in better ammonia desulfurization control.
(2) The system adds partial dilute sulfuric acid into the recovery section of the desulfurizing tower, controls the recovery pH value to 3-5 by utilizing the dilute sulfuric acid, performs secondary spray washing on the flue gas, recovers the ammonia entrained and escaped in the flue gas, and stably controls the discharged escaped ammonia within 3 mg/m.
(3) In the system, part of dilute sulfuric acid is added into a clean water washing section of the desulfurizing tower, the pH value of circulating liquid in the washing section is adjusted to 3-5, the escaped ammonia of the desulfurizing tower is further trapped, the length of smoke plume is reduced, and tailing is eliminated.
Drawings
FIG. 1 is a system diagram of the present utility model;
in the figure, a sulfuric acid storage tank 1, an acid discharging pump 2, an alkali liquid tank 3, an acid adding pump 4, a concentration tank 5, a recovery pump 6, a washing pump 7 and a valve 8 are adopted.
Detailed Description
The present utility model will be further described in detail with reference to the following examples in order to better understand the aspects of the present utility model and to make the above-mentioned objects, features and advantages of the present utility model more apparent to those skilled in the art.
Example 1
The utility model provides an ammonia desulfurization system of dilute sulfuric acid resource utilization, includes sulfuric acid storage tank 1, and the sulfuric acid storage tank 1 top is connected to alkali solution jar 3, and the sulfuric acid storage tank 1 bottom is let in to acid unloading pump 2, and sulfuric acid storage tank 1 passes through pipeline multiunit concentration tank 5 respectively, retrieves pump 6, wash tank 7 links to each other, sets up a plurality of valves 8 and acid adding pump 4 on the pipeline, and two acid adding pumps 4 parallel arrangement. Another pipeline is arranged in parallel between the concentration tank and the sulfuric acid storage tank 1, and a valve 4 is arranged on the pipeline. The valve can control the opening and closing of each pump.
The 5# concentration tank, the 5# recovery pump, the 5# washing tank, the 4# concentration tank, the 4# recovery pump, the 4# washing tank, the 3# concentration tank, the 3# recovery pump, the 3# washing tank, the 2# concentration tank, the 2# washing tank, the 1# concentration tank and the 1# washing tank are arranged according to the distance from the sulfuric acid storage tank.
In order to consume waste sulfuric acid of the chloromethane device, sulfuric acid pipelines are added to a 1-5# concentration tank, a 1-5# washing tank and a 3-5# recovery pump of the desulfurization tower, so that the recycling of dilute sulfuric acid is realized, the quality of ammonium sulfate products is improved, and the ammonia escape of the desulfurization tower is controlled.
The improvement process comprises the following steps:
(1) The sulfuric acid storage tank is used for storing sulfuric acid, a cofferdam is additionally arranged around the acid tank area, an acid adding pump is arranged, and an acid adding pipeline is arranged for each tower.
(2) The top of the acid tank is provided with a DN50 water-sealed pipeline which is led to zero meter, a tee joint is arranged at zero meter, one side is connected with a single suction valve, the control pressure is 1Kpa, the other side goes deep into the alkali liquid tank 3, and the odor is absorbed during acid storage. The water seal can use a DN600 pipeline, and the height is set to be 1.5 meters. The tube was kept 1000mm deep into the liquid.
(3) Two acid adding pumps are arranged in parallel on site, check valves are arranged on the pump outlets, the acid adding pumps are provided with a frequency converter, and the acid adding amount is controlled through frequency conversion.
(4) To avoid corrosion of the pipeline, the acid pump outlet pipeline should be a carbon steel lined tetrafluoro/polypropylene pipeline.
(5) The main pipelines of the sulfuric acid storage tank and the desulfurization tower at each stage use DN50 pipelines, branches of DN25 are respectively prepared at the inlet main pipe of each tower washing tank and the concentrating pump, and in addition, a branch DN25 acid adding pipeline is respectively prepared at the inlet main pipe of the 3-5# tower recovery pump, and the flow is controlled through a regulating valve.
(6) An DN50 flowmeter is arranged on an outlet pipe of the acid adding pump, so that the DCS is convenient for counting the acid adding flow of the system.
(7) In order to ensure acid discharging safety, an acid discharging pump is added, the outlet of the pump is connected with an acid inlet pipe orifice at the bottom of the tank, and a check valve is arranged at the inlet pipe of the pump to prevent sulfuric acid from flowing backwards.
(8) The desulfurizing tower is matched with another alkali water pipe to the sulfuric acid storage tank, so that the leaked sulfuric acid can be neutralized when leakage occurs.
The process implementation process comprises the following steps:
1. acid tank acid unloading:
(1) After the tank truck is connected with an acid unloading pipeline of the acid tank, the flange opening is firmly fastened, and the gasket is free of abnormality;
(2) Firstly, an operator wears acid and alkali resistant work clothes to take acid and alkali resistant gloves and protective masks, closes an acid discharging pipeline pouring valve, opens an acid discharging valve of an acid discharging tank, then opens the acid discharging valve of the tank truck by 1/3 opening, opens an exhaust valve of the acid discharging pipeline to exhaust the acid discharging pipeline, closes an exhaust valve when sulfuric acid flows out, checks whether the acid discharging pipeline has leakage points, immediately closes the acid discharging valve if the leakage points occur, and completely opens the acid discharging valve to discharge acid after the leakage points are not abnormal.
(3) During the acid unloading period, the liquid level of the sulfuric acid tank car and the sulfuric acid storage tank is concerned;
(4) After the acid is discharged, the acid discharging valve of the acid vehicle is closed, the acid discharging pipe pouring valve is opened, sulfuric acid in the acid discharging pipe is discharged, the acid discharging valve is closed, and the acid discharging pipeline is detached from the tank truck connecting flange.
2. Acid adding:
firstly, adding acid into a recovery pump section of a No. 5 tower:
(1) Before adding acid, the ammonia adding amount of the No. 5 tower is increased, the absorption pH is controlled to be about 7.5, and meanwhile, the pH value of the recovered, concentrated and washing liquid is sampled, analyzed and recorded.
(2) The operators carry acid and alkali resistant gloves and protective masks, the inlet valve and the outlet valve of the acid adding pump are opened, the main pipe acid adding valve at the inlet of the recovery pump of the No. 5 tower is opened, the acid adding pump is started, the recovery of the No. 5 tower is added with acid, and the variable frequency initial input of the acid adding pump is started to 25Hz.
(3) After the acid is added into the recovery pump of the No. 5 tower, sampling, analyzing and absorbing and recovering pH once every two hours, controlling the ammonia adding amount according to the change of the absorption pH, adjusting the absorption pH to 7.5-8.0, controlling the sulfuric acid adding amount per shift to 10 tons, observing the change of the recovery pH, opening a valve communicated with an ammonia adding cell and an oxidation pond for 20 percent if the recovery pH is close to 3.0, adjusting the opening of the valve by 5 percent each time according to the change of the recovery pH, and controlling the pH of the recovery stage of the No. 5 tower to be 3.0-5.0.
Acid is added to the recovery section of the No. 4 desulfurizing tower:
(1) Before adding acid into the recovery section of the No. 4 desulfurizing tower, the ammonia adding amount of the No. 4 desulfurizing tower is increased, the absorption pH is controlled to be about 7.5, and meanwhile, the pH value of the recovered, concentrated and washing liquid is sampled, analyzed and recovered, and recorded.
(2) The operators wear acid and alkali resistant gloves and protective masks, and open the main pipe acid adding valve at the inlet of the recovery pump of the No. 4 tower to add acid for recovery of the No. 4 tower.
(3) After the recovery and acid addition of the No. 4 tower are put into the reactor, sampling and analyzing absorption and recovery pH are carried out every two hours, ammonia addition amount is controlled according to absorption pH change, absorption pH is stabilized at about 7.5, recovery pH change is observed, if the recovery pH is close to 3.0, a reducing trend still exists, a valve for communicating an ammonia adding small chamber with an oxidation pond is opened for 20%, the opening of the valve is adjusted every 5% according to the recovery pH change, the recovery pH of the No. 4 tower is controlled between 3.0 and 5.0, sulfur change at the outlet of the No. 4 tower is closely concerned during the period, if the rising trend exists, the acid addition amount is stabilized, and if the index exceeds 10mg/m 3 And reducing the acid adding frequency conversion, and increasing the ammonia adding amount until the outlet sulfur is qualified.
Acid is added to the recovery section of the No. 3 desulfurizing tower:
(1) Before acid is recycled and added into the 3# tower, the ammonia adding amount of the 3# tower is increased, the absorption pH is controlled to be about 7.5, and meanwhile, the pH value of the recycled, concentrated and washing liquid is sampled, analyzed and recorded.
(2) The operators carry acid and alkali resistant gloves and protective masks, and open the main pipe acid adding valve at the inlet of the recovery pump of the No. 3 tower to add acid for recovery of the No. 3 tower.
(3) After the recovery and acid addition of the No. 3 tower are put into the reactor, sampling and analyzing absorption and recovery pH are carried out every two hours, ammonia addition amount is controlled according to absorption pH change, absorption pH is stabilized at about 7.5, recovery pH change is observed, if the recovery pH is close to 3.0, a reducing trend still exists, a valve for communicating an ammonia adding small chamber with an oxidation pond is opened for 20%, the recovery pH is adjusted at 5% opening each time according to the recovery pH change, the recovery pH of the No. 4 tower is controlled between 3.0 and 5.0, sulfur change at an outlet of the No. 4 tower is closely concerned during the recovery pH is controlled, if the rising trend exists, the acid addition amount is stabilized, and if the recovery pH exceeds the index of 10mg/m 3 And reducing the acid adding frequency conversion, and increasing the ammonia adding amount until the outlet sulfur is qualified.
3#4#5 column wash tank add acid:
(1) The frequency conversion of the acid adding pump is reduced to 2Hz, the opening of an acid adding valve of a washing tank of a 3# tower/4 # tower/5 # tower is respectively opened to 1/4, the acid adding adjustment of the washing section is carried out, the change of smoke plume at the outlet is compared, and the pH value of each section is firstly analyzed before switching;
(2) After two hours, the pH value of the washing liquid is analyzed, the frequency conversion of the acid pump is adjusted according to the pH value result, the amplitude of each time is adjusted to 5Hz, the washing pH value is respectively controlled between 3 and 4, and the change of the smoke plume at the outlet is compared.
(3) And during the adjustment period, recording the pH value of each section of the 3#/4#/5# tower, the opening of an ammonia adding valve, the frequency conversion of an acid pump and the position picture of smoke plume.
3#4#5 column concentrating section acid:
if the pH of the 3#/4#/5# concentrated solution exceeds 3.0, respectively adding acid into the 3# -4# -5# tower for concentrating, controlling the concentrated pH to be 2.0-3.0, and controlling the concentrated pH to improve the crystallization quality of ammonium sulfate.
Realizing acid addition in the recovery section, improving the stroke opening of an acid pump from 40% to 100%, reducing the pH value of the circulating liquid in the recovery section from about 6 to 4.31, reducing the escaped ammonia amount in the recovery section, reducing the pH value of the circulating liquid in the washing section from 7.6 to the lowest 3.89, and reducing the escaped ammonia amount from 15mg/m 3 Down to 1.4mg/m 3 The outlet smoke plume has no tailing condition.
The pH change for each stage is shown in Table 1.
pH of each section before and after acid addition is compared with the opening degree of an ammonia adding valve: the pH value of the circulating liquid in the recovery section is reduced by adding dilute sulfuric acid in the recovery section, and the ammonia adding valve of the system is not obviously adjusted.
Claims (4)
1. The utility model provides an ammonia desulfurization system of dilute sulfuric acid resource utilization, includes sulfuric acid storage tank (1), its characterized in that, sulfuric acid storage tank (1) top is connected in alkali lye jar (3), and acid pump (2) lets in sulfuric acid storage tank (1) bottom, and sulfuric acid storage tank (1) link to each other with concentration tank (5), recovery pump (6), washing tank (7) respectively through the pipeline, set up a plurality of valves (8) and add sour pump (4) on the pipeline.
2. The ammonia desulfurization system for recycling dilute sulfuric acid according to claim 1, wherein the sulfuric acid storage tank (1) is arranged on another pipeline in parallel, and a valve (8) is arranged on the pipeline.
3. The ammonia desulfurization system for recycling dilute sulfuric acid according to claim 1, wherein two acid pumps (4) are arranged in parallel.
4. The ammonia desulfurization system for recycling dilute sulfuric acid according to claim 1, wherein the concentration tank (5) and the washing tank (7) are provided with 5 groups, and the recovery pump (6) is provided with 3 groups.
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| CN202223005303.1U CN218924284U (en) | 2022-11-11 | 2022-11-11 | Ammonia desulfurization system for recycling dilute sulfuric acid |
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| CN202223005303.1U CN218924284U (en) | 2022-11-11 | 2022-11-11 | Ammonia desulfurization system for recycling dilute sulfuric acid |
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