A desulfurization and denitrification by-product SO2 acid production device and acid production process

Abstract

The embodiment of the present application provides a kind of desulfurization and denitrification by-product SO acid making device and acid making process, it is related to the field of acid making.The desulfurization and denitrification by-product SO acid making device includes incinerator, waste heat boiler, acid gas acid precipitator and mixer, incinerator is used to burn the acid gas generated by desulfurization, the inlet of waste heat boiler and the outlet of incinerator are connected, acid gas enters waste heat boiler after incinerator, acid gas acid precipitator is used to carry out dust removal treatment to analysis gas, the inlet of mixer and the outlet of acid gas acid precipitator are connected, the outlet of mixer and the outlet of waste heat boiler are connected, and mixer is connected with hot air, analysis gas and hot air are mixed in mixer, and the gas formed by mixing is sprayed from the outlet of mixer and mixed with the acid gas flowing from the outlet of waste heat boiler.The desulfurization and denitrification by-product SO acid making device does not affect the completion of acid making process when in use, and improves the acid making efficiency.

Description

Technical Field

[0001] This invention relates to the field of acid production technology, and more specifically, to an acid production device and process for SO2 produced from desulfurization and denitrification byproducts. Background Technology

[0002] The emission of acidic gases can pollute the surrounding environment, corrode surrounding equipment, and have a strong pungent odor that can affect human health. Therefore, acidic gases are currently treated. The commonly used acid production process is the WSA acid production process, which is a process that produces acidic gases, mainly H2S, during the desulfurization process.

[0003] Existing acid production processes suffer from problems such as pipe blockage and corrosion, causing new pollution and low acid production efficiency. Summary of the Invention

[0004] This invention provides an acid production device and process for SO byproducts from desulfurization and denitrification, which can avoid the blockage and corrosion of pipelines by new substances generated during the reaction of various substances in the acid production process, while avoiding new pollution and improving acid production efficiency.

[0005] The embodiments of the present invention can be implemented as follows:

[0006] An embodiment of the present invention provides a device for producing sulfuric acid from SO2, a byproduct of desulfurization and denitrification, comprising:

[0007] An incinerator for incinerating acidic gases produced during desulfurization;

[0008] A waste heat boiler, wherein the inlet of the waste heat boiler is connected to the outlet of the incinerator, and the acidic gas enters the waste heat boiler through the incinerator;

[0009] Acid gas acid dust collector, which is used to remove dust from the desorbed gas;

[0010] A mixer is provided, with its inlet connected to the outlet of the acid gas dust collector and its outlet connected to the outlet of the waste heat boiler. Hot air is connected to the mixer, and the desorbed gas and the hot air are mixed inside the mixer. The gas formed by the mixture is ejected from the outlet of the mixer and mixed with the acid gas flowing out from the outlet of the waste heat boiler.

[0011] Optionally, the desulfurization and denitrification byproduct SO acid production device includes a first pipe and a second pipe, which are arranged in parallel. The incinerator and the waste heat boiler are both located on the first pipe, and the acid gas dust collector and the mixer are both located on the second pipe. The outlet of the second pipe is connected to the first pipe, and the outlet of the mixer is connected to the first pipe through the second pipe. The mixed gas in the mixer is injected into the first pipe and mixed with the acid gas flowing out from the outlet of the waste heat boiler. The mixed gas flows out from the outlet of the first pipe.

[0012] Optionally, the desulfurization and denitrification byproduct SO2 acid production unit further includes an SCR reactor and a fourth pipeline. One end of the fourth pipeline is connected to the outlet of the first pipeline, and the other end of the fourth pipeline is connected to the inlet of the SCR reactor. The gas mixed in the first pipeline flows through the fourth pipeline into the SCR reactor, where a catalytic reduction reaction is carried out to remove NO2 oxides. X .

[0013] Optionally, an acid gas booster fan is connected to the second pipeline. The acid gas booster fan is located between the outlet of the acid gas dust collector and the inlet of the mixer. The temperature of the acid gas booster fan is greater than 159°C.

[0014] Optionally, the desulfurization and denitrification byproduct SO acid production device further includes a third pipeline connected to the mixer, through which the hot air enters the mixer.

[0015] Embodiments of the present invention also provide a process for producing acid from SO2, a byproduct of desulfurization and denitrification, using an SO2-based acid production device. The acid production process includes:

[0016] The acidic gas produced by desulfurization flows into the incinerator through the first pipeline for combustion, and the incinerated acidic gas is then transported to the waste heat boiler for combustion.

[0017] The desorbed gas enters the mixer through a second pipe;

[0018] The hot air is delivered to the mixer through a third pipe, so that the hot air and the desorbed gas are mixed.

[0019] The mixed gas flows out of the mixer outlet and is injected into the first pipe through the second pipe, so that the mixed gas and the acid gas are mixed.

[0020] The gas mixed in the first pipe enters the SCR reactor through the fourth pipe, where a catalytic reduction reaction is carried out to remove NO oxide. X .

[0021] Optionally, the desorption gas includes sulfur dioxide, carbon dioxide, carbon monoxide, hydrogen chloride, ammonia, water, dust particles, and nitrogen, wherein the content of sulfur dioxide is 12%-16.5%, the content of carbon dioxide is 4.1%, the content of carbon monoxide is 0.2%, the content of hydrogen chloride is less than 0.4%, the content of ammonia is 1%, the content of water is 40.2%, the content of dust particles is less than 10%, and the content of nitrogen is 32.1%-42.1%.

[0022] Optionally, the flow rate of the acidic gas exiting the waste heat boiler in the first pipe is greater than the flow rate of the desorbed gas in the second pipe.

[0023] Optionally, the flow rate of the desorption gas in the second pipeline is 600 Nm³. 3 / h-750Nm 3 / h, the flow rate of the hot air in the third pipe is 750 Nm 3 / h-900Nm 3 / h, the flow rate of the acidic gas in the first pipe before entering the waste heat boiler is 200 Nm³ / h. 3 / h-400Nm 3 / h.

[0024] Optionally, the output temperature of the desorbed gas is higher than 300°C.

[0025] Optionally, the pressure range of the desorbed gas in the second pipe is 15 kPa-20 kPa, and the pressure range of the hot air in the third pipe after being pressurized by the hot air blower is 13 kPa-20.9 kPa. The pressure range of the acidic gas in the first pipe after flowing out of the waste heat boiler is 6 kPa-8 kPa.

[0026] Optionally, the flow rate of the gas mixed in the first pipe in the fourth pipe is in the range of 5000 Nm³. 3 / h-5600Nm 3 Between / h.

[0027] The beneficial effects of the desulfurization and denitrification byproduct SO2 acid production device and acid production process in this invention include, for example:

[0028] The desulfurization and denitrification byproduct SO2 acid production unit includes an incinerator, a waste heat boiler, an acid gas dust collector, and a mixer. The incinerator is used to incinerate the acid gas generated during desulfurization. The inlet of the waste heat boiler is connected to the outlet of the incinerator, and the acid gas enters the waste heat boiler through the incinerator. The acid gas dust collector is used to remove dust from the desorbed gas. The inlet of the mixer is connected to the outlet of the acid gas dust collector, and the outlet of the mixer is connected to the outlet of the waste heat boiler. The mixer is also connected to hot air. The desorbed gas and hot air are mixed in the mixer, and the resulting gas is ejected from the outlet of the mixer and mixed with the acid gas flowing out from the outlet of the waste heat boiler. In operation, this desulfurization and denitrification byproduct SO2-to-acid production unit processes the acidic gas generated during desulfurization. After combustion and heating in the incinerator and waste heat boiler, the gas exits from the waste heat boiler. Because the inlet of the mixer is connected to the outlet of the acid gas and acid dust collector, and the outlet of the mixer is connected to the outlet of the waste heat boiler, the desorbed gas does not enter the incinerator with the acidic gas. This avoids the oxidation-reduction reaction between the desorbed and acidic gases, preventing the precipitation of elemental sulfur. This also prevents elemental sulfur from clogging and corroding pipes, thus avoiding disruption of the acid production process and subsequent pollution. The acidic gas exiting the waste heat boiler mixes with the desorbed gas, and the mixed gas then flows to the SCR reactor for catalytic reduction, ultimately producing concentrated sulfuric acid. This desulfurization and denitrification byproduct SO2-to-acid production unit does not affect the completion of the acid production process, improving acid production efficiency.

[0029] This desulfurization and denitrification byproduct SO2 acid production process utilizes an SO2 acid production unit to produce acid. The process includes: the acidic gas generated during desulfurization flows into an incinerator through a first pipe for combustion, and the incinerated acidic gas is then transported to a waste heat boiler for combustion; the desorbed gas enters a mixer through a second pipe; hot air is transported to the mixer through a third pipe, allowing the hot air and desorbed gas to mix; the mixed gas exits the mixer outlet and is injected into the first pipe through the second pipe, further mixing the mixed gas with the acidic gas; the mixed gas in the first pipe enters the SCR reactor through a fourth pipe, where a catalytic reduction reaction is carried out to remove NO oxide. X This desulfurization and denitrification byproduct SO2 acid production process avoids the oxidation-reduction reaction between the desorbed gas and acidic gas, which precipitates elemental sulfur. This prevents elemental sulfur from clogging and corroding pipelines, avoids the acid production process from malfunctioning and causing new pollution, and improves acid production efficiency. Attached Figure Description

[0030] To more clearly illustrate the technical solutions of the embodiments of the present invention, the accompanying drawings used in the embodiments will be briefly introduced below. It should be understood that the following drawings only show some embodiments of the present invention and should not be regarded as a limitation on the scope. For those skilled in the art, other related drawings can be obtained based on these drawings without creative effort.

[0031] Figure 1 This is a process diagram of a desulfurization and denitrification byproduct SO2 acid production device provided in this embodiment.

[0032] Icons: 10-Incinerator; 20-Waste heat boiler; 30-Acid gas dust collector; 40-Mixer; 50-SCR reactor; 60-Acid gas booster fan; 70-Gas booster fan; 80-Cooler; 90-Acid condenser; 101-First pipeline; 102-Second pipeline; 103-Third pipeline; 104-Fourth pipeline; 100-Desulfurization and denitrification byproduct SO2 acid production unit. Detailed Implementation

[0033] To make the objectives, technical solutions, and advantages of the embodiments of the present invention clearer, the technical solutions of the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings. Obviously, the described embodiments are only some embodiments of the present invention, and not all embodiments. The components of the embodiments of the present invention described and shown in the accompanying drawings can generally be arranged and designed in various different configurations.

[0034] Therefore, the following detailed description of the embodiments of the invention provided in the accompanying drawings is not intended to limit the scope of the claimed invention, but merely to illustrate selected embodiments of the invention. All other embodiments obtained by those skilled in the art based on the embodiments of the invention without inventive effort are within the scope of protection of the invention.

[0035] It should be noted that similar labels and letters in the following figures indicate similar items. Therefore, once an item is defined in one figure, it does not need to be further defined and explained in subsequent figures.

[0036] In the description of this invention, it should be noted that if terms such as "upper," "lower," "inner," or "outer" are used to indicate the orientation or positional relationship based on the orientation or positional relationship shown in the accompanying drawings, or the orientation or positional relationship in which the product of this invention is usually placed, they are only for the convenience of describing this invention and simplifying the description, and do not indicate or imply that the device or element referred to must have a specific orientation, or be constructed and operated in a specific orientation, and therefore should not be construed as a limitation of this invention.

[0037] Furthermore, the terms "first" and "second" are used only to distinguish descriptions and should not be interpreted as indicating or implying relative importance.

[0038] It should be noted that, where there is no conflict, the features in the embodiments of the present invention can be combined with each other.

[0039] The emission of acidic gases can pollute the surrounding environment, corrode surrounding equipment, and have a strong pungent odor that can affect human health. Therefore, acidic gases are currently treated. The commonly used acid production process is the WSA acid production process, which is a process that produces acidic gases, mainly H2S, during the desulfurization process.

[0040] The acid production process in related technologies has problems such as clogging and corroding of pipelines during operation, causing new pollution, and low acid production efficiency.

[0041] Specifically, the WSA acid production process generally involves sending acid gas into an incinerator to burn with air. The H2S in the acid gas is completely burned, converting into a mixture of SO, HCN, and a small amount of NH3. The high-temperature process gas after incineration enters a waste heat boiler to recover excess heat, and then enters an SCR reactor. First, a catalytic reduction reaction is carried out to purify the SO gas, and then a catalytic oxidation reaction is carried out to generate SO3. Finally, SO3 and the water vapor it carries enter a condenser to be directly condensed into acid.

[0042] More commonly, in the activated coke sulfuric acid production process, flue gas passes through activated coke containing a catalyst. SO₂ in the flue gas undergoes a catalytic reaction to form SO₃, which is then adsorbed onto activated carbon. Water is used to adsorb the SO₃ from the activated carbon, forming dilute sulfuric acid, while simultaneously regenerating the activated carbon. Simultaneously, NO is reduced to ammonia using the adsorption and catalytic action of the activated coke in the adsorption tower. Once the activated coke is saturated, it is sent to a desorption tower for further desorption. The desorbed SO₂ enters the degassing section, undergoes high-temperature dust removal (using a low-pressure pulse ceramic tube filter), and is then transported by an acid gas blower (small-flow booster blower, operating temperature 350–450℃) to the desulfurization and sulfuric acid production unit in the chemical production area. The SO₂-rich acid gas is then sent to the sulfuric acid production section to produce sulfuric acid. After cooling, the desorbed activated coke is passed through an air screen to remove wear-related coke dust and returned to the adsorption tower for recycling.

[0043] This embodiment combines the two acid production methods described above, and the combined device is used for acid production. During operation, if the desorbed gas is directly mixed with the feed gas from WSA acid production, activated carbon particles will inevitably accumulate and clog the pipes. Furthermore, activated carbon particles entering the SCR reactor will affect catalyst activity and SO conversion rate, causing the WSA acid production process to malfunction and resulting in pollution. When the acidic gases (H2S and HCN) from the desulfurization process enter the incinerator together with the desorbed gas, a redox reaction occurs: 2H2S + SO = 3S + 2H2O, releasing elemental sulfur, which can lead to pipe blockage and corrosion. To solve these technical problems, this embodiment provides an SO2 acid production device 100 from desulfurization and denitrification byproducts. This device effectively improves the aforementioned technical problems, avoids new substances generated during the acid production process from reactions that clog and corrode pipes, prevents new pollution, and improves acid production efficiency.

[0044] Please refer to Figure 1 The desulfurization and denitrification byproduct SO2 acid production device 100 includes an incinerator 10, a waste heat boiler 20, an acid gas and acid dust collector 30, and a mixer 40. The incinerator 10 is used to incinerate the acid gas generated during desulfurization. The inlet of the waste heat boiler 20 is connected to the outlet of the incinerator 10, and the acid gas enters the waste heat boiler 20 through the incinerator 10. The acid gas and acid dust collector 30 is used to remove dust from the desorbed gas. The inlet of the mixer 40 is connected to the outlet of the acid gas and acid dust collector 30, and the outlet of the mixer 40 is connected to the outlet of the waste heat boiler 20. The mixer 40 is connected to hot air. The desorbed gas and hot air are mixed in the mixer 40. The gas formed by the mixture is ejected from the outlet of the mixer 40 and mixed with the acid gas flowing out from the outlet of the waste heat boiler 20.

[0045] In this embodiment, the desulfurization and denitrification byproduct SO2 acid production device 100 includes a first pipe 101 and a second pipe 102, which are arranged in parallel. The incinerator 10 and the waste heat boiler 20 are both located in the first pipe 101, and the acid gas dust collector 30 and the mixer 40 are both located in the second pipe 102. The outlet of the second pipe 102 is connected to the first pipe 101, and the outlet of the mixer 40 is connected to the first pipe 101 through the second pipe 102. The mixed gas in the mixer 40 is injected into the first pipe 101 and mixed with the acid gas flowing out from the outlet of the waste heat boiler 20. The mixed gas flows out from the outlet of the first pipe 101.

[0046] The desulfurization and denitrification byproduct SO2 acid production device 100 also includes a third pipe 103, which is connected to a mixer 40, through which hot air enters the mixer 40.

[0047] In this embodiment, the hot air before entering the mixer 40 is pressurized by a hot press, and the pressure range of the pressurized hot air is 13 kPa-20.9 kPa, specifically 14 kPa.

[0048] Acid gas booster fan 60 is connected to the second pipe 102. The acid gas booster fan 60 is located between the outlet of the acid gas dust collector 30 and the inlet of the mixer 40.

[0049] Specifically, to prevent the formation of dilute sulfuric acid and sulfurous acid within the second pipe 102, which could corrode the second pipe 102, the temperature of the acid gas booster fan 60 in this embodiment is greater than 159°C, and the output temperature of the desorbed gas is greater than 300°C. That is, the outlet temperature of the acid dust collector needs to be higher than 300°C.

[0050] It should be noted that, in order to ensure that the outlet temperature of the acid dust collector can be higher than 300°C, in this embodiment, an electric heat tracing pipe is installed inside the acid dust collector to heat the inside of the acid dust collector. At the same time, in order to prevent the gas from carrying in water vapor and causing caking inside the acid dust collector, and to prevent the temperature inside the acid dust collector from dropping due to low-temperature gas, inert gas nitrogen is used for blowing. Furthermore, a heating system is added between the nitrogen storage tank and the acid dust collector to ensure that the nitrogen temperature is around 180°C and not lower than 160°C.

[0051] Specifically, the temperature range of the acid dust collector is 300℃-360℃.

[0052] In this embodiment, there are two acid gas booster blowers 60, which are arranged alternately. The acid gas booster blowers 60 can pressurize the desorbed gas and deliver the desorbed gas into the mixer 40.

[0053] Similarly, the first pipeline 101 is equipped with a gas booster fan 70, which blows air toward the incinerator 10 so that the acidic gas entering the incinerator 10 can be fully burned.

[0054] In this embodiment, the number of gas-generating fans is two.

[0055] The desulfurized and denitrified gas flows into the mixer 40 through the second pipe 102, and then hot air is introduced into the mixer 40 through the third pipe 103, so that the hot air and the desulfurized gas are mixed in the mixer 40. The mixed gas flows out from the outlet of the mixer 40 and continues to flow into the first pipe 101 through the second pipe 102 to mix with the acid gas.

[0056] Specifically, by paralleling the acid gas and the desorption gas before they enter the incinerator 10, the acid gas reacts with the desorption gas after exiting the incinerator 10. This avoids the oxidation-reduction reaction between the desorption gas and the acid gas, which could precipitate elemental sulfur and clog the pipes. After entering the SCR reactor 50, the desorption gas and acid gas undergo a catalytic reduction reaction to remove nitrogen oxides (NOx). X The process involves the catalytic oxidation of sulfur dioxide to produce concentrated sulfuric acid. This ensures that the SO2 sulfuric acid production unit 100, a byproduct of desulfurization and denitrification, not only does not affect the operation of the unit but also simultaneously removes nitrogen oxides from the two mixed gases, purifying the sulfur dioxide for subsequent reactions.

[0057] In this embodiment, the desorption gases include sulfur dioxide, carbon dioxide, carbon monoxide, hydrogen chloride, ammonia, water, dust particles, and nitrogen.

[0058] To achieve the optimal ratio between the desorbed gas and the acidic gas from the outlet of the waste heat boiler 20 during the mixing process, increase the proportion of H2SO4 produced for acid production, and avoid impurities affecting the recovery and utilization of the desorbed gas, in this embodiment, the desorbed gas contains 12%-16.5% sulfur dioxide, 4.1% carbon dioxide, 0.2% carbon monoxide, less than 0.4% hydrogen chloride, 1% ammonia, 40.2% water, less than 10% particulate matter, and 32.1%-42.1% nitrogen.

[0059] It should also be noted that the flow rate of the desorption gas in the second pipe 102 is 600 Nm³. 3 / h-750Nm 3 The flow rate of hot air in the third pipe 103 is 750 Nm / h. 3 / h-900Nm 3 / h, the flow rate of acidic gas in the first pipe 101 before entering the waste heat boiler 20 is 200 Nm³ / h. 3 / h-400Nm 3 / h.

[0060] In order to increase the concentration of the final sulfuric acid produced, the flow rate of the acidic gas from the waste heat boiler 20 in the first pipe 101 is greater than the flow rate of the desorption gas in the second pipe 102.

[0061] It should be noted that, in order for the desorbed gas and hot air to mix better after entering the mixer 40, and in order for the mixed gas to be injected into the first pipe 101 to merge with the acid gas, the pressure of the desorbed gas before entering the mixer 40 should be equivalent to the pressure of the hot air before entering the mixer 40.

[0062] In this embodiment, the pressure range of the desorbed gas in the second pipe 102 is 15KPa-20KPa, and the pressure range of the hot air in the third pipe 103 after being pressurized by the hot air blower is 13KPa-20.9KPa. The pressure range of the acidic gas in the first pipe 101 after flowing out of the waste heat boiler 20 is 6KPa-8KPa.

[0063] In this embodiment, the flow rate of the gas mixed in the first pipe 101 in the fourth pipe 104 is in the range of 5000 Nm³. 3 / h-5600Nm 3 Between / h.

[0064] More often, the acidic gases are burned in the incinerator 10 and then flow out through the waste heat boiler 20. The temperature range of the outflowing acidic gases is 480℃-520℃.

[0065] In addition, to prevent the condensation of ammonium bisulfate in the mixer 40 and the injection system at the outlet of the mixer 40, the temperature of the mixed gas inside the mixer 40 needs to be controlled above 325°C.

[0066] In order to ensure that the temperature of the mixed gas inside the mixer 40 can be controlled above 325°C, the air entering the mixer 40 needs to be preheated to above 380°C.

[0067] Therefore, by coordinating the temperature, pressure, and flow rate of the desorption gas, hot air, and acidic gas, it is possible to further reduce the generation of particulate precipitates and corrosive gases such as acidic substances during the acid production process, thereby further increasing the concentration of the final sulfuric acid produced.

[0068] It should also be noted that the desulfurization and denitrification byproduct SO2 acid production unit 100 further includes an SCR reactor 50 and a fourth pipeline 104. One end of the fourth pipeline 104 is connected to the outlet of the first pipeline 101, and the other end of the fourth pipeline 104 is connected to the inlet of the SCR reactor 50. The gas mixed in the first pipeline 101 flows through the fourth pipeline 104 into the SCR reactor 50, where a catalytic reduction reaction is carried out to remove the oxide NO. X .

[0069] In this embodiment, the second pipe 102 is DN200, the third pipe 103 is DN250, and the fourth pipe 104 is DN900.

[0070] More specifically, the acid dust collector in this embodiment is a high-temperature ceramic acid dust collector.

[0071] Furthermore, the desulfurization and denitrification byproduct SO2 acid production unit 100 also includes multiple coolers 80 and acid condensers 90. The inlet of the cooler 80 is connected to the outlet of the SCR reactor 50, and the outlet of the cooler 80 is connected to the inlet of the acid condenser 90. The cooler 80 is externally connected to boiler water and an acid mist controller.

[0072] Take off NO X The SO gas is converted into SO3 in the SO converter and then enters the cooler 80. Boiler water is supplied to the cooler 80 for cooling and temperature reduction, causing SO3 to absorb water vapor and form acid mist under the control of the acid mist controller. After the acid mist flows out of the cooler 80, it is cooled into concentrated sulfuric acid below 50°C by the acid condenser 90.

[0073] The acid condenser 90 is connected to a chimney and an acid tank. The concentrated sulfuric acid formed inside the acid condenser 90 eventually flows into the acid tank for collection, and the excess acid mist is discharged from the chimney under the action of the desulfurization and denitrification induced draft fan.

[0074] Embodiments of the present invention also provide a process for producing acid from SO2, a byproduct of desulfurization and denitrification, utilizing SO2 as a byproduct of desulfurization and denitrification. O2 The acid production unit 100 produces acid, and the acid production process includes:

[0075] S1: The acidic gas generated by desulfurization flows into the incinerator 10 through the first pipeline 101 for combustion, and the incinerated acidic gas is then transported to the waste heat boiler 20 for combustion.

[0076] Acidic gas enters the incinerator 10 through the first pipe 101 for combustion under the action of the gas booster fan. The incinerated acidic gas continues to enter the waste heat boiler 20 for heating, thereby recovering excess heat.

[0077] S2: The desorbed gas enters the mixer 40 through the second pipe 102;

[0078] The desorbed gas enters the acid dust collector for high-temperature dust removal, and then continues to flow along the second pipe 102 into the mixer 40 under the blowing of the acid gas booster fan 60.

[0079] S3: Hot air is delivered to mixer 40 through third pipe 103 so that hot air and desorbed gas are mixed;

[0080] After being heated by the preheater, the air enters the mixer 40 through the third pipe 103, where the hot air and the desorbed gas are mixed.

[0081] S4: The mixed gas flows out of the outlet of the mixer 40 and is injected into the first pipe 101 through the second pipe 102, so that the mixed gas and the acid gas are mixed.

[0082] The mixed gas is injected into the first pipe 101 along the second pipe 102 under the action of the injection system, so that the mixed gas and the acid gas are mixed.

[0083] S5: The gas mixed in the first pipe 101 enters the SCR reactor 50 through the fourth pipe 104, where a catalytic reduction reaction is carried out to remove the oxide NO. X ;

[0084] S6: The NO that was taken off X The SO gas is converted into SO3 in the SO converter and then enters the cooler 80 to form acid mist.

[0085] S7: Acid mist is cooled into concentrated sulfuric acid below 50°C in acid condenser 90.

[0086] In summary, this invention provides an acid production device 100 for SO2 produced from desulfurization and denitrification byproducts and an acid production process. The SO2 acid production device 100 includes an incinerator 10, a waste heat boiler 20, an acid gas dust collector 30, and a mixer 40. The incinerator 10 is used to incinerate the acid gas generated during desulfurization. The inlet of the waste heat boiler 20 is connected to the outlet of the incinerator 10, and the acid gas enters the waste heat boiler 20 after passing through the incinerator 10. The acid gas dust collector 30 is used to remove dust from the desorbed gas. The inlet of the mixer 40 is connected to the outlet of the acid gas dust collector 30, and the outlet of the mixer 40 is connected to the outlet of the waste heat boiler 20. Hot air is connected to the mixer 40. The desorbed gas and the hot air are mixed in the mixer 40, and the gas formed by the mixture is ejected from the outlet of the mixer 40 and mixed with the acid gas flowing out from the outlet of the waste heat boiler 20. In operation, the desulfurization and denitrification byproduct SO2-to-acid production device 100, after the acidic gas generated from desulfurization is burned and heated in the incinerator 10 and waste heat boiler 20, flows out from the outlet of the waste heat boiler 20. Since the inlet of the mixer 40 is connected to the outlet of the acid gas and acid dust collector 30, and the outlet of the mixer 40 is connected to the outlet of the waste heat boiler 20, the desorbed gas will not enter the incinerator 10 together with the acidic gas. This avoids the oxidation-reduction reaction between the desorbed gas and the acidic gas, preventing the precipitation of elemental sulfur. This avoids the elemental sulfur from clogging and corroding the pipes, preventing the acid production process from malfunctioning and causing new pollution. After flowing out of the waste heat boiler 20, the acidic gas mixes with the desorbed gas, and the mixed gas then flows to the SCR reactor 50 for catalytic reduction, ultimately producing concentrated sulfuric acid. This desulfurization and denitrification byproduct SO2-to-acid production device 100 does not affect the completion of the acid production process during operation, thus improving the acid production efficiency.

[0087] The desulfurization and denitrification byproduct SO2 acid production process utilizes a desulfurization and denitrification byproduct SO2 acid production device 100 to produce acid. The acid production process includes: the acidic gas generated from desulfurization flows into the incinerator 10 through the first pipe 101 for combustion, and the after-combustion acidic gas is transported to the waste heat boiler 20 for combustion; the desorbed gas enters the mixer 40 through the second pipe 102; hot air is transported to the mixer 40 through the third pipe 103 to mix the hot air and the desorbed gas; the mixed gas flows out of the outlet of the mixer 40 and is injected into the first pipe 101 through the second pipe 102 to mix the mixed gas with the acidic gas; the mixed gas in the first pipe 101 enters the SCR reactor 50 through the fourth pipe 104, where a catalytic reduction reaction is carried out to remove the oxide NO. X This desulfurization and denitrification byproduct SO2 acid production process avoids the oxidation-reduction reaction between the desorbed gas and acidic gas, which precipitates elemental sulfur. This prevents elemental sulfur from clogging and corroding pipelines, avoids the acid production process from malfunctioning and causing new pollution, and improves acid production efficiency.

[0088] The above description is merely a specific embodiment of the present invention, but the scope of protection of the present invention is not limited thereto. Any variations or substitutions that can be easily conceived by those skilled in the art within the technical scope disclosed in the present invention should be included within the scope of protection of the present invention. Therefore, the scope of protection of the present invention should be determined by the scope of the claims.

Claims

1. A process for producing acid from SO2, a byproduct of desulfurization and denitrification, comprising using an SO2-based acid production device (100) to produce acid, characterized in that, The desulfurization and denitrification byproduct SO2 acid production unit (100) includes: Incinerator (10), the incinerator (10) is used to incinerate the acidic gases produced by desulfurization; Waste heat boiler (20), the inlet of which is connected to the outlet of the incinerator (10), and the acid gas enters the waste heat boiler (20) through the incinerator (10). Acid gas acid dust collector (30), said acid gas acid dust collector (30) is used to remove dust from the desorbed gas; A mixer (40) is connected to the outlet of the acid gas dust collector (30), and the outlet of the mixer (40) is connected to the outlet of the waste heat boiler (20). The mixer (40) is connected to hot air. The desorbed gas and the hot air are mixed in the mixer (40). The gas formed by the mixture is ejected from the outlet of the mixer (40) and mixed with the acid gas flowing out from the outlet of the waste heat boiler (20). The acid production process includes: The acidic gas generated from desulfurization flows into the incinerator (10) through the first pipe (101) for combustion, and the incinerated acidic gas is then transported to the waste heat boiler (20) for combustion. The desorbed gas enters the mixer (40) through the second pipe (102); The hot air is delivered to the mixer (40) through the third pipe (103) so that the hot air and the desorbed gas are mixed; The mixed gas flows out of the outlet of the mixer (40) and is injected into the first pipe (101) through the second pipe (102), so that the mixed gas and the acid gas are mixed; The gas mixed in the first pipe (101) enters the SCR reactor (50) through the fourth pipe (104), where a catalytic reduction reaction is carried out to remove the oxide NO. X ; The desorption gas includes sulfur dioxide, carbon dioxide, carbon monoxide, hydrogen chloride, ammonia, water, dust particles, and nitrogen. The sulfur dioxide content is 12%-16.5%, the carbon dioxide content is 4.1%, the carbon monoxide content is 0.2%, the hydrogen chloride content is less than 0.4%, the ammonia content is 1%, the water content is 40.2%, the dust particle content is less than 10%, and the nitrogen content is 32.1%-42.1%.

2. The process for producing acid from SO2, a byproduct of desulfurization and denitrification, according to claim 1, is characterized in that, The flow rate of the acidic gas flowing out of the waste heat boiler (20) in the first pipe (101) is greater than the flow rate of the desorbed gas in the second pipe (102).

3. The process for producing acid from SO2, a byproduct of desulfurization and denitrification, according to claim 1, is characterized in that, The flow rate of the desorbed gas in the second pipe (102) is 600 Nm. 3 / h -750Nm 3 / h, the flow rate of the hot air in the third pipe (103) is 750 Nm 3 / h -900Nm 3 / h, the flow rate of the acidic gas in the first pipe (101) before entering the waste heat boiler (20) is 200 Nm. 3 / h -400Nm 3 / h.

4. The process for producing acid from SO2, a byproduct of desulfurization and denitrification, according to claim 1, is characterized in that, The output temperature of the desorbed gas is higher than 300°C.

5. The process for producing acid from SO2, a byproduct of desulfurization and denitrification, according to claim 1, is characterized in that, The pressure range of the desorbed gas in the second pipe (102) is 15KPa-20KPa, and the pressure range of the hot air in the third pipe (103) after being pressurized by the hot air blower is 13KPa-20.9KPa. The pressure range of the acidic gas in the first pipe (101) after flowing out of the waste heat boiler (20) is 6KPa-8KPa.

6. The process for producing acid from SO2, a byproduct of desulfurization and denitrification, according to claim 1, is characterized in that, The flow rate of the gas mixed in the first pipe (101) in the fourth pipe (104) is in the range of 5000 Nm. 3 / h -5600Nm 3 Between / h.

7. The process for producing acid from SO2, a byproduct of desulfurization and denitrification, according to claim 1, is characterized in that, The desulfurization and denitrification byproduct SO2 acid production device (100) includes a first pipe (101) and a second pipe (102). The first pipe (101) and the second pipe (102) are arranged in parallel. The incinerator (10) and the waste heat boiler (20) are both located in the first pipe (101). The acid gas dust collector (30) and the mixer (40) are both located in the second pipe (102). The outlet of the second pipe (102) is connected to the first pipe (101). The outlet of the mixer (40) is connected to the first pipe (101) through the second pipe (102). The mixed gas in the mixer (40) is injected into the first pipe (101) and mixed with the acid gas flowing out from the outlet of the waste heat boiler (20). The mixed gas flows out from the outlet of the first pipe (101).

8. The process for producing acid from SO2, a byproduct of desulfurization and denitrification, according to claim 7, is characterized in that, The desulfurization and denitrification byproduct SO2 acid production device (100) further includes an SCR reactor (50) and a fourth pipe (104). One end of the fourth pipe (104) is connected to the outlet of the first pipe (101), and the other end of the fourth pipe (104) is connected to the inlet of the SCR reactor (50). The gas mixed in the first pipe (101) flows through the fourth pipe (104) into the SCR reactor (50), where a catalytic reduction reaction is carried out to remove oxide NO. X .

9. The process for producing acid from SO2, a byproduct of desulfurization and denitrification, according to claim 7, is characterized in that, The second pipeline (102) is connected to an acid gas booster fan (60), which is located between the outlet of the acid gas acid dust collector (30) and the inlet of the mixer (40). The temperature of the acid gas booster fan (60) is greater than 159°C.

10. The process for producing acid from SO2, a byproduct of desulfurization and denitrification, according to claim 1, is characterized in that, The desulfurization and denitrification byproduct SO2 acid production device (100) also includes a third pipe (103), which is connected to the mixer (40), and the hot air enters the mixer (40) through the third pipe (103).

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