CN115430262B - Device and method for recycling nitrous gases - Google Patents
Device and method for recycling nitrous gases Download PDFInfo
- Publication number
- CN115430262B CN115430262B CN202211032888.8A CN202211032888A CN115430262B CN 115430262 B CN115430262 B CN 115430262B CN 202211032888 A CN202211032888 A CN 202211032888A CN 115430262 B CN115430262 B CN 115430262B
- Authority
- CN
- China
- Prior art keywords
- absorption tower
- absorption
- gas
- return pipeline
- nitrous
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/18—Absorbing units; Liquid distributors therefor
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1406—Multiple stage absorption
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1412—Controlling the absorption process
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1418—Recovery of products
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B21/00—Nitrogen; Compounds thereof
- C01B21/20—Nitrogen oxides; Oxyacids of nitrogen; Salts thereof
- C01B21/38—Nitric acid
- C01B21/40—Preparation by absorption of oxides of nitrogen
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
- B01D2252/10—Inorganic absorbents
- B01D2252/103—Water
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/40—Nitrogen compounds
Abstract
The utility model provides a nitrite gas recovery unit, includes liquid ring compressor, first, second absorption tower, liquid ring compressor's gas vent links to each other with the lateral wall bottom of first absorption tower through first pipeline, and first absorption tower is the filler tower, from last down the interval setting first, second, third filler absorption section, and is provided with corresponding return line respectively, and the quantity of second absorption tower is one or more, constitutes wholly through the series connection, and the gas phase import of second absorption tower links to each other with the top of the tower of first absorption tower through the second pipeline. The invention has simple structure and convenient operation, can recycle the nitrous gases, especially the nitrous gases in the tail gas with low cost and high efficiency, and meets the environmental protection requirement.
Description
Technical Field
The invention relates to the field of chemical industry, in particular to a device and a method for recovering nitrous gases.
Background
Chemical enterprises utilize cyclohexanol and nitric acid to oxidize and produce adipic acid, tail gas of the chemical enterprises contains a large amount of nitrous gas, and nitrogen oxides (nitric oxide and nitrogen dioxide) contained in the nitrous gas are required to be separated and recovered before the nitrous gas is discharged.
At present, when the tail gas containing nitrous gases is treated by chemical enterprises, the tail gas is firstly mixed with air, nitrogen oxides in the tail gas are all converted into nitrogen dioxide, and then the nitrogen dioxide enters an absorption tower to be in countercurrent contact with spray water, so that nitric acid is obtained at the bottom of the tower.
However, the concentration of the nitric acid obtained by the treatment method is low, the nitric acid is required to be sold as a product after concentration, time and labor are wasted, in addition, in order to reduce the content of nitrogen oxides in the discharged tail gas as much as possible, a plurality of sets of absorption towers are required to be designed, and the alkaline solution is used as the absorption liquid to remove the residual nitrogen oxides in the tail gas, so that the cost of comprehensive treatment is high.
Therefore, how to recycle the nitrous gases in the tail gas with high efficiency and low cost is a problem to be solved by the person skilled in the art.
Disclosure of Invention
One of the purposes of the invention is to provide a nitrous gas recycling device aiming at the defects of the prior art, which has simple structure, convenient operation, low cost and high efficiency for recycling nitrous gas, in particular to nitrous gas in tail gas, and meets the environmental protection requirement.
The second purpose of the invention is to provide a method for recycling the nitrous gas by adopting the device, which has mild process and extremely high nitrous gas utilization rate, and can directly generate and obtain concentrated nitric acid with the concentration of more than 51 percent as a product to be used or directly sold to the outside, thereby effectively improving the utilization value of the nitrous gas.
The technical scheme for realizing one of the purposes of the invention is as follows: the utility model provides a nitrite gas recovery unit, includes liquid ring compressor, first absorption tower, second absorption tower, first return line, second return line, third return line, liquid ring compressor's air inlet is used for being connected with nitrite air supply and oxygen source, and liquid ring compressor's gas vent links to each other with first absorption tower's lateral wall bottom through first pipeline, is provided with compressed air import on this first pipeline, first absorption tower is the filler tower, and first absorption tower is from the last first filler absorption section that sets up down, second filler absorption section, third filler absorption section, and the top of first filler absorption section sets up first distributor, and the below sets up first liquid phase collecting tank, and the top of second filler absorption section sets up the second distributor, and the below sets up the second liquid phase collecting tank, and the top of third filler absorption section sets up the third distributor, the upstream end of first return line links to each other with first liquid phase collecting tank, and the downstream end links to each other with first distributor, and this first return line sets up first return pump, first cooling loop, and the second return line sets up the second return line, and the second return line sets up the downstream end of second return line links to each other with the third return line, and the third return line is connected with the third inlet, and the third return line is connected with the third tower through the first return line, the third return line, the first return line is connected with the third return line.
Preferably, the number of the second absorption towers is three.
Further, the device also comprises a fourth return pipeline, wherein the upstream end of the fourth return pipeline is connected with the bottom of the second absorption tower, the downstream end of the fourth return pipeline is connected with the side wall of the second absorption tower, and a fourth return pump and a fourth cooler are arranged on the fourth return pipeline.
Preferably, the third cooler comprises a precooling heat exchanger and a refrigerating heat exchanger, the precooling heat exchanger and the refrigerating heat exchanger are formed by connecting in series, the precooling heat exchanger is positioned at the upstream of the refrigerating heat exchanger, a cooling medium of the precooling heat exchanger is circulating water, and a cooling medium of the refrigerating heat exchanger is chilled water.
The second technical scheme for realizing the purpose of the invention is as follows: the method for recycling the nitrous gas by adopting any nitrous gas recycling device comprises the following steps:
1) Mixing the nitrous gas with an oxygen source, compressing the mixture by a liquid ring compressor, oxidizing part of the nitrous gas into nitrogen dioxide, and reacting the nitrogen dioxide with liquid ring water to generate nitric acid;
2) The nitric acid produced in the liquid ring compressor discharges the liquid ring compressor, as the absorption lean solution of the first absorption tower, after mixing the remaining nitrous gas with compressed air, enter the first absorption tower, and the air inlet pressure is 0.175-0.195MPa, and the air inlet temperature is 70-80 ℃;
3) The temperature of the gas phase discharged from the top of the first absorption tower is 10-20 ℃, the gas phase enters the second absorption tower, and the concentrated nitric acid is discharged from the bottom of the first absorption tower;
4) Controlling the temperature of the gas phase discharged from the top of the second absorption tower at 15-20 ℃ and sending the gas phase to a laughing gas emission reduction device.
Further, the nitrous gas in step 1) is a tail gas containing nitric oxide and/or nitrogen dioxide and/or nitrous oxide.
Preferably, the oxygen source in step 1) is air.
Preferably, in the step 2), the liquid phase temperature at the upstream end of the third reflux pipeline of the first absorption tower is 45-55 ℃, the liquid phase temperature at the downstream end is 25-35 ℃, the liquid phase temperature at the upstream end of the second reflux pipeline is 25-35 ℃, the liquid phase temperature at the downstream end is 15-25 ℃, the liquid phase temperature at the upstream end of the third reflux pipeline is 15-25 ℃, and the liquid phase temperature at the downstream end is 10-20 ℃.
Further, the concentration of the concentrated nitric acid discharged in the step 3) is more than or equal to 51%.
Further, the nitrogen oxide content in the gas phase sent to the laughing gas emission reduction device in the step 4) is less than or equal to 381ppm.
The technical scheme has the following beneficial effects:
1. the nitrous gas recovery device comprises a liquid ring type compressor, a first absorption tower, a second absorption tower, a first return pipeline, a second return pipeline and a third return pipeline, wherein the liquid ring type compressor is used for pressurizing nitrous gas, and nitrogen dioxide generated by the oxidation of the nitrous gas is absorbed by utilizing liquid ring water, so that the concentration of nitric acid generated by the first absorption tower can be effectively improved as an absorption lean solution of the first absorption tower, in addition, the liquid ring type compressor can also play a role in cooling the nitrous gas, the recycling efficiency of the nitrous gas is improved, and the recycling energy consumption of the nitrous gas is reduced. The gas inlet of the liquid ring type compressor is used for being connected with a nitrous gas source and an oxygen source, the gas outlet of the liquid ring type compressor is connected with the bottom of the side wall of the first absorption tower through a first pipeline, a compressed air inlet is arranged on the first pipeline and used for providing compressed air, the pressure in the first absorption tower is further improved on the basis that all nitrous gas is converted into nitrogen dioxide, the absorption efficiency of nitrogen dioxide generated by oxidation is further promoted, the concentration of generated nitric acid is improved, in addition, the generated nitric acid can be directly discharged outside by utilizing the pressure in the first absorption tower, and the recycling power consumption and cost of the nitrous gas are further reduced. The first absorption tower is a filler tower, the first absorption tower is provided with a first filler absorption section, a second filler absorption section and a third filler absorption section from top to bottom at intervals, the first distributor is arranged above the first filler absorption section, the first liquid phase collecting tank is arranged below the first filler absorption section, the second distributor is arranged above the second filler absorption section, the second liquid phase collecting tank is arranged below the second filler absorption section, the third distributor is arranged above the third filler absorption section, each designed distributor is used for uniformly distributing the absorption lean liquid along the sectional area of the first filler tower, each designed liquid phase collecting tank is used for partially collecting the absorption rich liquid flowing out of the upper filler absorption section, and the nitrogen dioxide in the first absorption tower is repeatedly absorbed as reflux liquid. The upstream end of the first return pipeline is connected with the first liquid phase collecting tank, the downstream end of the first return pipeline is connected with the first distributor, a first return pump and a first cooler are arranged on the first return pipeline, and self-circulation is formed at the upper part of the first absorption tower. The upstream end of the second return pipeline is connected with the second liquid phase collecting tank, the downstream end of the second return pipeline is connected with the second distributor, a second return pump and a second cooler are arranged on the second return pipeline, and self-circulation is formed in the middle of the first absorption tower. The upstream end of the third return pipe is connected with the bottom of the first absorption tower, the downstream end of the third return pipe is connected with a third distributor, a third return pump and a third cooler are arranged on the third return pipe, and self-circulation is formed at the lower part of the first absorption tower. Through three-stage reflux absorption, the absorption efficiency of the absorption lean solution on nitrogen dioxide can be effectively improved. The number of the second absorption towers is one or more, the second absorption towers are connected in series to form a whole, a gas phase inlet of each second absorption tower is connected with the top of each first absorption tower through a second pipeline, and tail gas containing a small amount of nitrogen dioxide discharged by each first absorption tower is absorbed again through each second absorption tower, so that the content of nitrogen oxides in the discharged tail gas can be effectively reduced, and the environment-friendly requirement is met.
2. The third cooler comprises a precooling heat exchanger and a refrigerating heat exchanger which are connected in series, the precooling heat exchanger is positioned at the upstream of the refrigerating heat exchanger, the cooling medium of the precooling heat exchanger is circulating water, the cooling medium of the refrigerating heat exchanger is chilled water, the circulating water is firstly utilized to preliminarily cool the circulating liquid phase, then the chilled water is utilized to further cool, the consumption of the chilled water can be effectively reduced on the premise of improving the solubility of nitrogen dioxide, and the energy consumption of the recycling of nitrous gases is reduced.
3. According to the recycling method, firstly, nitrous gas is mixed with an oxygen source, so that more nitrous gas is oxidized to generate nitrogen dioxide, then the nitrogen dioxide is compressed and pressurized by a liquid ring compressor, wherein a nitrogen dioxide part generated by oxidation reacts with liquid ring water of the liquid ring compressor to obtain nitric acid, heat is released, the heat and the generated nitric acid are discharged along with the liquid ring water of the liquid ring compressor and are used as absorption lean liquid of a first absorption tower, the absorption lean liquid is uniformly sprayed out from a first distributor at the upper part of the first absorption tower, unreacted nitrogen dioxide and compressed air are mixed and enter from the lower part of the first absorption tower, a three-stage cooling absorption, three-stage acid concentration and high-pressure absorption environment is formed, the dissolution rate of nitrogen oxides (nitrogen dioxide) in the absorption liquid can be greatly improved, the acid concentration of absorption rich liquid at the bottom of the first absorption tower reaches more than 51%, the heat and the generated nitric acid is discharged outside under the action of self tower pressure to be used as a nitric acid product for selling, and the nitrous gas is effectively recycled.
4. The recycling method of the invention creates a low-temperature high-pressure environment by controlling the pressure of the nitrous gases and the compressed air entering the first absorption tower to be 0.175-0.195MPa, the inlet temperature to be 70-80 ℃ and the exhaust temperature to be 10-20 ℃, thereby ensuring most NO and N 2 O completes the reaction and removes the heat of reaction, thereby enhancing the positive absorption effect and increasing the nitric acid concentration.
5. The recycling method of the invention comprises the following steps ofThe upstream end liquid phase temperature of the three return pipes is controlled to be 45-55 ℃, the downstream end liquid phase temperature is controlled to be 25-35 ℃, the upstream end liquid phase temperature of the second return pipe is controlled to be 25-35 ℃, the downstream end liquid phase temperature is controlled to be 15-25 ℃, the upstream end liquid phase temperature of the third return pipe is controlled to be 15-25 ℃, the downstream end liquid phase temperature is controlled to be 10-20 ℃, the absorption effect is strengthened step by controlling the temperature drop step by step, and the NO and N in tail gas are ensured 2 The O content reaches the minimum value, and the maximum efficiency recovery effect is achieved.
Further description is provided below with reference to the drawings and detailed description.
Drawings
Fig. 1 is a schematic structural view of the present invention.
In the drawing, 1 is a first absorption tower, 2 is a second absorption tower, 3 is a liquid ring compressor, 4 is a first return pipeline, 5 is a second return pipeline, 6 is a third return pipeline, 7 is a compressed air inlet, 8 is a first filler absorption section, 9 is a second filler absorption section, 10 is a third filler absorption section, 11 is a first distributor, 12 is a first liquid phase collecting tank, 13 is a second distributor, 14 is a second liquid phase collecting tank, 15 is a third distributor, 16 is a first return pump, 17 is a first cooler, 18 is a second return pump, 19 is a second cooler, 20 is a third return pump, 21 is a third cooler, 21a is a precooling heat exchanger, 21b is a refrigeration heat exchanger, 22 is a fourth return pipeline, 23 is a fourth return pump, 24 is a fourth cooler, 101 is a first pipeline, and 102 is a second pipeline.
Detailed Description
Example 1
Referring to fig. 1, the nitrous gas recovery apparatus comprises a liquid ring compressor 3, a first absorption tower 1, a second absorption tower 2, a first return line 4, a second return line 5, and a third return line 6. The inlet of the liquid ring compressor 3 is used for being connected with a nitrous gas source and an oxygen source, wherein the nitrous gas source is typically chemical tail gas containing nitrous gas (nitric oxide), and the oxygen source is typically air. The exhaust port of the liquid ring compressor 3 is connected to the bottom of the side wall of the first absorption tower 1 via a first pipe 101, and the first pipe 101 is provided with a compressed air inlet 7. The first absorption tower 1 is a packed tower, and a first packed absorption section 8, a second packed absorption section 9 and a third packed absorption section 10 are arranged in the first absorption tower 1 from top to bottom at intervals. The first distributor 11 is arranged above the first filler absorption section 8, the first liquid phase collecting tank 12 is arranged below, the second distributor 13 is arranged above the second filler absorption section 9, the second liquid phase collecting tank 14 is arranged below, the third distributor 15 is arranged above the third filler absorption section 10, in this embodiment, the third filler absorption section is positioned above the downstream end of the first pipeline, and obviously, the cross-sectional area of each liquid phase collecting tank is smaller than that of the first absorption tower, so that the absorption rich liquid part passing through the corresponding filler absorption section is trapped. The upstream end of the first return line 4 is connected with the first liquid phase collecting tank 12, the downstream end is connected with the first distributor 11, the first return line 4 is provided with a first return pump 16 and a first cooler 17, the upstream end of the second return line 5 is connected with the second liquid phase collecting tank 14, the downstream end is connected with the second distributor 13, the second return line 5 is provided with a second return pump 18 and a second cooler 19, the upstream end of the third return line 6 is connected with the bottom of the first absorption tower 1, the downstream end is connected with a third distributor 15, and the third return line 6 is provided with a third return pump 20 and a third cooler 21. The three second absorption towers 2 are connected in series to form a whole, a gas phase inlet of the second absorption tower positioned at the upstream is connected with the top of the first absorption tower 1 through a second pipeline 102, a top exhaust outlet of the second absorption tower positioned at the downstream externally discharges the treated tail gas, and obviously, the device also comprises a fourth return pipeline 22, the upstream end of the fourth return pipeline 22 is connected with the bottom of the second absorption tower 2, the downstream end of the fourth return pipeline 22 is connected with the side wall of the second absorption tower 2, and a fourth return pump 23 and a fourth cooler 24 are arranged on the fourth return pipeline 22.
Example 2
The method for recycling the nitrous gas by adopting the nitrous gas recycling device of the embodiment 1 comprises the following steps:
1) Mixing a nitrous gas source with an oxygen source, compressing the mixture by a liquid ring compressor, oxidizing part of nitrous gas into nitrogen dioxide, and reacting the nitrogen dioxide with liquid ring water to generate nitric acid, wherein NO in the nitrous gas source 2 The flow rate of (C) was 0.244kg/h, the flow rate of NO was 15.786kg/h, N 2 The flow rate of O is 14843.694kg/h, and the oxygen source is air;
2) The nitric acid discharge liquid ring compressor generated in the liquid ring compressor is used as an absorption lean solution of the first absorption tower, the residual nitrous gas is mixed with compressed air and enters the first absorption tower, the air inlet pressure is 0.175-0.195MPa, the air inlet temperature is 70-80 ℃, the upstream end liquid phase temperature of the third return pipeline is controlled to be 45-55 ℃ by adjusting the first cooler, the second cooler and the third cooler, the downstream end liquid phase temperature is controlled to be 25-35 ℃, the upstream end liquid phase temperature of the second return pipeline is controlled to be 25-35 ℃, the downstream end liquid phase temperature is controlled to be 15-25 ℃, the upstream end liquid phase temperature of the third return pipeline is controlled to be 15-25 ℃, and the downstream end liquid phase temperature is controlled to be 10-20 ℃;
3) The gas phase temperature discharged from the top of the first absorption tower is 10-20 ℃, the gas phase enters the second absorption tower, and the concentrated nitric acid is discharged from the bottom of the first absorption tower, wherein the concentration is 51%;
4) Controlling the temperature of the gas phase discharged from the top of the second absorption tower at 15-20 ℃, sending the gas phase to a laughing gas emission reduction device, detecting that the nitrogen oxide content is 381ppm, calculating NO in a nitrous gas source 2 The absorption rate of (2) was 99.994%, and the absorption rate of NO was 99.41%.
Claims (8)
1. A method for recovering nitrous gases is characterized in that: the recovery device is adopted to recover the nitrous gases,
the recovery device comprises a liquid ring type compressor (3), a first absorption tower (1), a second absorption tower (2), a first return pipeline (4), a second return pipeline (5) and a third return pipeline (6),
the air inlet of the liquid ring type compressor (3) is used for being connected with a nitrous air source and an oxygen source, the air outlet of the liquid ring type compressor (3) is connected with the bottom of the side wall of the first absorption tower (1) through a first pipeline (101), a compressed air inlet (7) is arranged on the first pipeline (101),
the first absorption tower (1) is a packed tower, the first absorption tower (1) is provided with a first packing absorption section (8), a second packing absorption section (9) and a third packing absorption section (10) from top to bottom at intervals, a first distributor (11) is arranged above the first packing absorption section (8), a first liquid phase collecting tank (12) is arranged below the first distributor, a second distributor (13) is arranged above the second packing absorption section (9), a second liquid phase collecting tank (14) is arranged below the second distributor, a third distributor (15) is arranged above the third packing absorption section (10),
the upstream end of the first return pipeline (4) is connected with a first liquid phase collecting tank (12), the downstream end is connected with a first distributor (11), a first return pump (16) and a first cooler (17) are arranged on the first return pipeline (4),
the upstream end of the second return pipeline (5) is connected with a second liquid phase collecting tank (14), the downstream end is connected with a second distributor (13), a second return pump (18) and a second cooler (19) are arranged on the second return pipeline (5),
the upstream end of the third return pipeline (6) is connected with the bottom of the first absorption tower (1), the downstream end is connected with a third distributor (15), a third return pump (20) and a third cooler (21) are arranged on the third return pipeline (6),
the number of the second absorption towers (2) is one or more, the second absorption towers are connected in series to form a whole, and a gas phase inlet of each second absorption tower (2) is connected with the top of the first absorption tower (1) through a second pipeline (102);
the recovery method comprises the following steps:
1) Mixing the nitrous gas with an oxygen source, compressing the mixture by a liquid ring compressor, oxidizing part of the nitrous gas into nitrogen dioxide, and reacting the nitrogen dioxide with liquid ring water to generate nitric acid;
2) The nitric acid discharge liquid ring compressor generated in the liquid ring compressor is used as an absorption lean liquid of the first absorption tower, the residual nitrous gas is mixed with compressed air and enters the first absorption tower, the air inlet pressure is 0.175-0.195MPa, the air inlet temperature is 70-80 ℃, the upstream end liquid phase temperature of a third return pipeline of the first absorption tower is 45-55 ℃, the downstream end liquid phase temperature is 25-35 ℃, the upstream end liquid phase temperature of a second return pipeline is 25-35 ℃, the downstream end liquid phase temperature is 15-25 ℃, the upstream end liquid phase temperature of the third return pipeline is 15-25 ℃, and the downstream end liquid phase temperature is 10-20 ℃;
3) The temperature of the gas phase discharged from the top of the first absorption tower is 10-20 ℃, the gas phase enters the second absorption tower, and the concentrated nitric acid is discharged from the bottom of the first absorption tower;
4) Controlling the temperature of the gas phase discharged from the top of the second absorption tower at 15-20 ℃ and sending the gas phase to a laughing gas emission reduction device.
2. The method for recovering nitrous gases as claimed in claim 1, wherein: the number of the second absorption towers (2) is three.
3. The method for recovering nitrous gases according to claim 1 or 2, wherein: the device further comprises a fourth return pipeline (22), wherein the upstream end of the fourth return pipeline (22) is connected with the bottom of the second absorption tower (2), the downstream end of the fourth return pipeline (22) is connected with the side wall of the second absorption tower (2), and a fourth return pump (23) and a fourth cooler (24) are arranged on the fourth return pipeline (22).
4. The method for recovering nitrous gases as claimed in claim 1, wherein: the third cooler (21) comprises a precooling heat exchanger (21 a) and a refrigerating heat exchanger (21 b), and is formed by connecting the precooling heat exchanger and the refrigerating heat exchanger in series, wherein the precooling heat exchanger is positioned at the upstream of the refrigerating heat exchanger, the cooling medium of the precooling heat exchanger is circulating water, and the cooling medium of the refrigerating heat exchanger is chilled water.
5. The method according to claim 1, wherein the nitrous gas of step 1) is a tail gas comprising nitric oxide and/or nitrogen dioxide and/or nitrous oxide.
6. The method of claim 1, wherein the oxygen source in step 1) is air.
7. The method for recovering nitrous gases as claimed in claim 1, wherein: the concentration of the concentrated nitric acid discharged in the step 3) is more than or equal to 51 percent.
8. The method for recovering nitrous gases as claimed in claim 1, wherein: the concentration of nitrogen oxides in the gas phase sent to the laughing gas emission reduction device in the step 4) is less than or equal to 381ppm.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202211032888.8A CN115430262B (en) | 2022-08-26 | 2022-08-26 | Device and method for recycling nitrous gases |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202211032888.8A CN115430262B (en) | 2022-08-26 | 2022-08-26 | Device and method for recycling nitrous gases |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN115430262A CN115430262A (en) | 2022-12-06 |
| CN115430262B true CN115430262B (en) | 2023-09-01 |
Family
ID=84244660
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202211032888.8A Active CN115430262B (en) | 2022-08-26 | 2022-08-26 | Device and method for recycling nitrous gases |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN115430262B (en) |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN201012317Y (en) * | 2006-12-06 | 2008-01-30 | 中国石油天然气股份有限公司 | Highly effective absorbing equipment of nitrous acid air |
| CN103566739A (en) * | 2013-10-24 | 2014-02-12 | 南京大学 | Method for resource recovery of nitrogen oxides (NOx) in nitric acid industrial waste gas |
| CN103920384A (en) * | 2014-04-25 | 2014-07-16 | 兰州大学 | Equipment for absorbing high-concentration nitric oxides by adopting normal-pressure process |
| CN209155494U (en) * | 2018-10-24 | 2019-07-26 | 阳泉煤业集团平定化工有限责任公司 | Exhaust treatment system with MN recycling function |
| CN112933915A (en) * | 2021-04-14 | 2021-06-11 | 中国海洋石油集团有限公司 | Nitrogen oxide waste gas recycling treatment device and method |
| CN214680966U (en) * | 2021-04-14 | 2021-11-12 | 中国海洋石油集团有限公司 | Nitrogen oxide waste gas resourceful treatment device |
| CN218249418U (en) * | 2022-08-26 | 2023-01-10 | 重庆华峰化工有限公司 | Nitrous gas recovery unit |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP3372556A1 (en) * | 2017-03-07 | 2018-09-12 | Casale Sa | A plant for the production of nitric acid, a related process and method of revamping |
-
2022
- 2022-08-26 CN CN202211032888.8A patent/CN115430262B/en active Active
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN201012317Y (en) * | 2006-12-06 | 2008-01-30 | 中国石油天然气股份有限公司 | Highly effective absorbing equipment of nitrous acid air |
| CN103566739A (en) * | 2013-10-24 | 2014-02-12 | 南京大学 | Method for resource recovery of nitrogen oxides (NOx) in nitric acid industrial waste gas |
| CN103920384A (en) * | 2014-04-25 | 2014-07-16 | 兰州大学 | Equipment for absorbing high-concentration nitric oxides by adopting normal-pressure process |
| CN209155494U (en) * | 2018-10-24 | 2019-07-26 | 阳泉煤业集团平定化工有限责任公司 | Exhaust treatment system with MN recycling function |
| CN112933915A (en) * | 2021-04-14 | 2021-06-11 | 中国海洋石油集团有限公司 | Nitrogen oxide waste gas recycling treatment device and method |
| CN214680966U (en) * | 2021-04-14 | 2021-11-12 | 中国海洋石油集团有限公司 | Nitrogen oxide waste gas resourceful treatment device |
| CN218249418U (en) * | 2022-08-26 | 2023-01-10 | 重庆华峰化工有限公司 | Nitrous gas recovery unit |
Also Published As
| Publication number | Publication date |
|---|---|
| CN115430262A (en) | 2022-12-06 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN103223292B (en) | Ammonia process flue gas treatment method for acidic tail gas and device | |
| CN103987443B (en) | The nitric acid production improved | |
| CN107551813B (en) | Ship desulfurization and denitrification integrated process and device | |
| CN103363537B (en) | Oxygen-enriched combustion flue gas purification device | |
| CN107789967B (en) | Sintering flue gas low-temperature denitration device and implementation method thereof | |
| CN218249418U (en) | Nitrous gas recovery unit | |
| CN114225671A (en) | Nitrogen oxide tail gas treatment process | |
| CN210826085U (en) | Blast furnace gas catalytic desulfurization device | |
| CN105776385B (en) | Stainless steel spent solution regeneration system and its control method based on spray roasting | |
| CN115430262B (en) | Device and method for recycling nitrous gases | |
| CN209740714U (en) | Device for preparing nitric acid by efficiently oxidizing and absorbing nitrogen oxides | |
| CN103691287A (en) | Nitrogen tetroxide tail gas recycling system | |
| CN210356635U (en) | Nitrogen oxide waste gas purification combination equipment containing acidic gas | |
| CN111963283A (en) | Novel urea hydrolysis system with product gas treatment device and application | |
| CN214829037U (en) | Device for producing dilute nitric acid by magnesium nitrate method | |
| CN212716833U (en) | Novel urea hydrolysis system with product gas treatment device | |
| CN104923052B (en) | A kind of flue gas processing device and method | |
| CN211562418U (en) | Tail gas efficient spraying and absorbing device in polyimide film production | |
| CN208878244U (en) | A kind of device of removal of nitrogen oxide | |
| CN102080920B (en) | Method for separating nitrogen oxides from industrial waste gas by low-temperature refrigerators | |
| CN217431317U (en) | Low-energy consumption device for flue gas CO2 trapping process | |
| CN211338811U (en) | System for retrieve electronic grade nitrous oxide in follow industrial exhaust | |
| CN204656327U (en) | A kind of flue gas processing device | |
| CN217473115U (en) | Carbon capture system for lime kiln flue gas | |
| CN217829533U (en) | System for reducing nitrogen oxides in tail gas |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |