CN113332857A - Method for realizing alkali liquor regeneration by nitrogen oxide tail gas absorption through acid-base synchronous separation - Google Patents
Method for realizing alkali liquor regeneration by nitrogen oxide tail gas absorption through acid-base synchronous separation Download PDFInfo
- Publication number
- CN113332857A CN113332857A CN202110636093.7A CN202110636093A CN113332857A CN 113332857 A CN113332857 A CN 113332857A CN 202110636093 A CN202110636093 A CN 202110636093A CN 113332857 A CN113332857 A CN 113332857A
- Authority
- CN
- China
- Prior art keywords
- tail gas
- alkali liquor
- nitrogen oxide
- acid
- flue gas
- 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.)
- Pending
Links
- MWUXSHHQAYIFBG-UHFFFAOYSA-N Nitric oxide Chemical compound O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 title claims abstract description 270
- 239000003513 alkali Substances 0.000 title claims abstract description 85
- 239000007789 gas Substances 0.000 title claims abstract description 71
- 238000010521 absorption reaction Methods 0.000 title claims abstract description 51
- 238000000034 method Methods 0.000 title claims abstract description 43
- 238000000926 separation method Methods 0.000 title claims abstract description 15
- 239000002585 base Substances 0.000 title claims abstract description 12
- 230000008929 regeneration Effects 0.000 title claims abstract description 12
- 238000011069 regeneration method Methods 0.000 title claims abstract description 12
- 230000001360 synchronised effect Effects 0.000 title claims abstract description 12
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims abstract description 95
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 51
- 239000003546 flue gas Substances 0.000 claims abstract description 51
- 238000000197 pyrolysis Methods 0.000 claims abstract description 35
- GRYLNZFGIOXLOG-UHFFFAOYSA-N Nitric acid Chemical compound O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 claims abstract description 28
- 229910017604 nitric acid Inorganic materials 0.000 claims abstract description 28
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 21
- 238000004064 recycling Methods 0.000 claims abstract description 17
- 239000007787 solid Substances 0.000 claims abstract description 17
- 239000002253 acid Substances 0.000 claims abstract description 13
- 238000001816 cooling Methods 0.000 claims abstract description 11
- 239000007788 liquid Substances 0.000 claims abstract description 8
- 238000000889 atomisation Methods 0.000 claims description 11
- 238000004519 manufacturing process Methods 0.000 claims description 4
- 230000001172 regenerating effect Effects 0.000 claims description 3
- 239000011734 sodium Substances 0.000 claims description 2
- LPXPTNMVRIOKMN-UHFFFAOYSA-M sodium nitrite Chemical compound [Na+].[O-]N=O LPXPTNMVRIOKMN-UHFFFAOYSA-M 0.000 abstract description 15
- VWDWKYIASSYTQR-UHFFFAOYSA-N sodium nitrate Chemical compound [Na+].[O-][N+]([O-])=O VWDWKYIASSYTQR-UHFFFAOYSA-N 0.000 abstract description 14
- 235000010344 sodium nitrate Nutrition 0.000 abstract description 7
- 239000004317 sodium nitrate Substances 0.000 abstract description 7
- 235000010288 sodium nitrite Nutrition 0.000 abstract description 7
- 239000002351 wastewater Substances 0.000 abstract description 3
- 239000012535 impurity Substances 0.000 abstract description 2
- 238000004065 wastewater treatment Methods 0.000 abstract 1
- 238000006243 chemical reaction Methods 0.000 description 9
- 229910002651 NO3 Inorganic materials 0.000 description 5
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 description 5
- 238000002156 mixing Methods 0.000 description 4
- 238000003756 stirring Methods 0.000 description 4
- 230000008901 benefit Effects 0.000 description 3
- 238000002425 crystallisation Methods 0.000 description 3
- 230000008025 crystallization Effects 0.000 description 2
- 238000002386 leaching Methods 0.000 description 2
- 238000002360 preparation method Methods 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 229910000272 alkali metal oxide Inorganic materials 0.000 description 1
- 150000001447 alkali salts Chemical class 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 239000013078 crystal Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 239000011504 laterite Substances 0.000 description 1
- 229910001710 laterite Inorganic materials 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 229910052976 metal sulfide Inorganic materials 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000012452 mother liquor Substances 0.000 description 1
- KKCBUQHMOMHUOY-UHFFFAOYSA-N sodium oxide Chemical compound [O-2].[Na+].[Na+] KKCBUQHMOMHUOY-UHFFFAOYSA-N 0.000 description 1
- 229910001948 sodium oxide Inorganic materials 0.000 description 1
Images
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
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/96—Regeneration, reactivation or recycling of reactants
-
- 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
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/54—Nitrogen compounds
- B01D53/56—Nitrogen oxides
-
- 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
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/77—Liquid phase processes
- B01D53/78—Liquid phase processes with gas-liquid contact
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/30—Alkali metal compounds
- B01D2251/304—Alkali metal compounds of sodium
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/60—Inorganic bases or salts
- B01D2251/604—Hydroxides
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
Abstract
The invention discloses a method for realizing alkali liquor regeneration by absorbing nitrogen oxide tail gas through acid-base synchronous separation, which comprises the following steps: a) absorbing alkali liquor by the nitrogen oxide tail gas, atomizing and pyrolyzing to produce solid alkali and pyrolysis flue gas; b) cooling the produced pyrolysis flue gas to obtain condensed water and high-concentration nitrogen oxide flue gas; c) sending the high-concentration nitrogen oxide flue gas into a nitrogen oxide flue gas acid making system to prepare nitric acid; d) dissolving the solid alkali in the step a) by using the condensed water in the step b) to obtain sodium hydroxide alkali liquor, and feeding the alkali liquor into a nitrogen oxide tail gas absorption system for recycling. The method can realize the separation of acid and alkali in the nitric oxide tail gas absorption liquid, realize the recycling of the nitric oxide tail gas absorption liquid, improve the nitric acid recycling rate and realize no new alkali consumption in tail gas absorption. The method has simple process, is easy to be applied in large scale in industrialization, does not introduce other impurity elements, realizes the comprehensive recycling of the sodium nitrate (sodium nitrite) alkaline wastewater, and reduces the wastewater treatment cost.
Description
Technical Field
The invention belongs to the technical field of nitric acid production and application, and relates to a method for realizing alkali liquor regeneration by nitrogen oxide tail gas absorption through acid-base synchronous separation.
Background
In the nitric acid production industry, nitric oxide gas with high concentration is oxidized and absorbed to produce nitric acid, the absorbed tail gas does not reach the emission standard, and partial enterprises adopt sodium hydroxide solution to absorb the tail gas again to reach the emission standard; or in some nitric acid application industries, such as the metallurgical industry using nitric acid as a leaching agent, laterite ore is leached by nitric acid, metal or metal sulfide is leached by nitric acid, in order to realize the recycling of nitric acid in the process, high-concentration nitric oxide flue gas produced in the leaching process is generally prepared into acid by adopting an oxidation-absorption method (the recycling of nitric acid is realized), the process also has the problem that the flue gas after the acid preparation reaches the standard and is discharged, and generally, sodium hydroxide solution is also adopted to absorb nitric oxide gas in the tail gas, so that the absorbed nitric oxide in the tail gas reaches the discharge standard. The main components of the alkali liquor after absorbing the nitrogen oxide tail gas (called nitrogen oxide tail gas absorbing alkali liquor for short) are sodium nitrate, sodium nitrite and a small amount of residual alkali.
At present, the nitric oxide tail gas absorption alkali liquor mostly adopts an evaporation crystallization process to obtain corresponding sodium nitrate and sodium nitrite, crystallization mother liquor is difficult to treat, two components in sodium nitrate and sodium nitrite crystals are mutually contained and difficult to be used as high-quality products for external sales, green terminal open circuits cannot be formed, and a large amount of alkali consumption is the main cost component for tail gas treatment. Meanwhile, by adopting an evaporative crystallization method, most of the nitrogen oxides in the tail gas enter nitrate, so that the loss of nitric acid in the whole process flow is caused, and the recovery rate (or the reuse rate) of the nitric acid is reduced.
Disclosure of Invention
The invention aims to solve the technical problems that the nitric oxide tail gas is difficult to comprehensively treat absorbed alkali liquor, the nitric acid recovery rate (the reuse rate) is reduced due to the loss of nitric oxide in the prior art, the alkali salt absorption is difficult to open a circuit and the like, and provides a method which is simple in process, easy to industrialize and realizes the regeneration of the nitric oxide tail gas absorbed alkali liquor through acid-base synchronous separation.
The purpose of the invention can be realized by the following technical scheme:
a method for realizing regeneration of nitric oxide tail gas absorption alkali liquor through acid-base synchronous separation is disclosed, wherein the nitric oxide tail gas absorption alkali liquor is the absorption alkali liquor of nitric oxide flue gas tail gas produced in the nitric acid production or nitric acid related application field, and the method for regenerating the absorption alkali liquor comprises the following steps:
a) absorbing alkali liquor by the nitrogen oxide tail gas, atomizing and pyrolyzing to produce solid alkali and pyrolysis flue gas;
b) cooling the produced high-temperature pyrolysis flue gas to below 60 ℃ through a heat exchanger to obtain condensed water and high-concentration nitric oxide flue gas, and sending the high-concentration nitric oxide flue gas into a nitric oxide flue gas acid making system to prepare nitric acid;
c) dissolving the solid alkali in the step a) by using the condensed water in the step b) to obtain sodium hydroxide alkali liquor, and returning the alkali liquor to the nitric oxide tail gas absorption system for recycling.
The main components of the nitric oxide tail gas absorption alkali liquor are as follows: na (Na)+ 105~120 g/L、NO3 -/NO2 - 200-250 g/L、OH- 15~20 g/L。
Further, in the step a), the pyrolysis temperature of the atomization pyrolysis is 600-800 ℃, and the pyrolysis time is 3-5 min.
Further, in the step b), the volume fraction of the nitrogen oxides in the high-concentration nitrogen oxide flue gas is 55-60%.
The method is adopted to treat and absorb the alkali liquor, and the high-concentration nitrogen oxide flue gas and the sodium hydroxide alkali liquor can be regenerated in one step in an atomization pyrolysis mode, so that the acid-base synchronous separation and recycling are realized. The essence of the method is that: the nitric oxide gas in the tail gas enters absorption alkali liquor in the liquid alkali absorption process, the reverse reaction of the absorption process is carried out when the absorption alkali liquor is heated and decomposed, namely nitrate in the absorption alkali liquor is decomposed into alkali and nitric oxide gas, in the process of decomposing the nitrate and releasing the nitric oxide, the nitric oxide gas is cooled, and the volume fraction of the nitric oxide in the obtained cooled flue gas can reach 55-60 percent after water vapor is condensed into condensed water, so that the concentration requirement of absorbing and preparing nitric acid is met, and the flue gas can be merged into an absorption acid-making system so as to realize acid recycling; the alkali liquor obtained by dissolving the solid alkali generated by pyrolysis in the condensed water is returned to the absorption process for recycling, so that the regeneration and recycling of the alkali are realized, the generation of new wastewater is avoided, and the water balance of the system is realized.
In conclusion, the method can realize the separation of acid and alkali in the tail gas absorption liquid of the nitrogen oxides by one step, so that the absorption alkali sodium hydroxide is regenerated and reused, the nitrogen oxide gas in the tail gas is enriched, the nitric acid reuse rate is improved, and the comprehensive treatment of the tail gas absorption alkali liquid is realized. The method has simple process, is easy to be applied in large scale in industrialization, does not introduce any other impurity elements, realizes the comprehensive recycling of the sodium nitrate (sodium nitrite) alkaline wastewater, and has obvious cost benefit and environmental benefit.
Drawings
FIG. 1 is a process flow diagram of the method for regenerating the nitric oxide tail gas absorbing alkali liquor. The content in the dotted line frame in the figure is the core content of the process of the invention.
Detailed Description
The process of the present invention is further illustrated by the following specific examples, which are provided to aid in the understanding of the present invention and its advantages, but are not intended to limit the scope of the invention.
Example 1
The components of the absorption lye of the nitrogen oxide tail gas in this example are shown in Table 1.
Conveying the nitrogen oxide tail gas absorbing alkali liquor to an atomization pyrolysis furnace, adjusting the temperature of the pyrolysis furnace to 600 ℃, and carrying out atomization pyrolysis for 5min to obtain solid alkali and pyrolysis flue gas; and cooling the pyrolysis flue gas to obtain condensed water and high-concentration nitrogen oxide flue gas. Mixing and stirring the solid alkali and the condensed water obtained in the cooling procedure in a reaction kettle for reaction to obtain regenerated sodium hydroxide alkali liquor, wherein the alkali liquor can be sent into a nitrogen oxide tail gas absorption system for recycling. And sending the high-concentration nitrogen oxide flue gas into a nitrogen oxide flue gas acid making system to prepare nitric acid.
The main components of the regenerated sodium hydroxide lye and the volume fraction of the nitrogen oxides in the regenerated high-concentration nitrogen oxide flue gas are shown in table 1.
Table 1 example 1 nitrogen oxide tail gas absorption lye, regenerated sodium hydroxide lye principal component (g/L) and regenerated nitrogen oxide gas concentration (%)
Example 2
The components of the absorption lye of the nitrogen oxide tail gas in this example are shown in Table 2.
Conveying the nitrogen oxide tail gas absorbing alkali liquor to an atomization pyrolysis furnace, adjusting the temperature of the pyrolysis furnace to 700 ℃, and carrying out atomization pyrolysis for 4min to obtain solid alkali and pyrolysis flue gas; and cooling the pyrolysis flue gas to obtain condensed water and high-concentration nitrogen oxide flue gas. Mixing and stirring the solid alkali and the condensed water obtained in the cooling procedure in a reaction kettle for reaction to obtain regenerated sodium hydroxide alkali liquor, wherein the alkali liquor can be sent into a nitrogen oxide tail gas absorption system for recycling. And sending the high-concentration nitrogen oxide flue gas into a nitrogen oxide flue gas acid making system to prepare nitric acid.
The main components of the regenerated sodium hydroxide lye and the volume fraction of the nitrogen oxides in the regenerated high-concentration nitrogen oxide flue gas are shown in Table 2.
Table 2 example 2 nitrogen oxide tail gas absorption lye, main component of regenerated sodium hydroxide lye (g/L) and concentration of regenerated nitrogen oxide gas (%)
Example 3
The components of the absorption lye of the nitrogen oxide tail gas in this example are shown in Table 3.
Conveying the nitrogen oxide tail gas absorbing alkali liquor to an atomization pyrolysis furnace, adjusting the temperature of the pyrolysis furnace to 800 ℃, and carrying out atomization pyrolysis for 3min to obtain solid alkali and pyrolysis flue gas; and cooling the pyrolysis flue gas to obtain condensed water and high-concentration nitrogen oxide flue gas. Mixing and stirring the solid alkali and the condensed water obtained in the cooling procedure in a reaction kettle for reaction to obtain regenerated sodium hydroxide alkali liquor, wherein the alkali liquor can be sent into a nitrogen oxide tail gas absorption system for recycling. And sending the high-concentration nitrogen oxide flue gas into a nitrogen oxide flue gas acid making system to prepare nitric acid.
The main components of the regenerated sodium hydroxide lye and the volume fraction of the nitrogen oxides in the regenerated high-concentration nitrogen oxide flue gas are shown in Table 3.
Table 3 example 3 nitric oxide tail gas absorption lye, main component of regenerated sodium hydroxide lye (g/L) and concentration of regenerated nitric oxide gas (%)
Example 4
The components of the absorption lye of the nitrogen oxide tail gas in this example are shown in Table 4.
Conveying the nitrogen oxide tail gas absorbing alkali liquor to an atomization pyrolysis furnace, adjusting the temperature of the pyrolysis furnace to 750 ℃, and carrying out atomization pyrolysis for 2min to obtain solid alkali and pyrolysis flue gas; and cooling the pyrolysis flue gas to obtain condensed water and high-concentration nitrogen oxide flue gas. Mixing and stirring the solid alkali and the condensed water obtained in the cooling procedure in a reaction kettle for reaction to obtain regenerated sodium hydroxide alkali liquor, wherein the alkali liquor can be sent into a nitrogen oxide tail gas absorption system for recycling. And sending the high-concentration nitrogen oxide flue gas into a nitrogen oxide flue gas acid making system to prepare nitric acid.
The main components of the regenerated sodium hydroxide lye and the volume fraction of the nitrogen oxides in the regenerated high-concentration nitrogen oxide flue gas are shown in Table 4.
Table 4 example 4 nitric oxide tail gas absorption lye, regenerated sodium hydroxide lye principal component (g/L) and regenerated nitric oxide gas concentration (%)
The method is characterized in that the alkali liquor absorbing the nitric oxide tail gas is atomized and pyrolyzed within a certain temperature range, sodium nitrate and sodium nitrite in the alkali liquor are decomposed and water is vaporized to obtain a pyrolyzed solid alkali product (a mixture, the main component of which is sodium oxide containing sodium hydroxide and a small amount of undecomposed nitric acid/sodium nitrite salt and the like) and pyrolyzed flue gas containing nitrogen oxide gas, and the pyrolyzed flue gas is cooled to obtain condensed water and high-concentration nitric oxide flue gas; and (3) enabling the high-concentration nitrogen oxide flue gas to enter a nitric acid preparation system, dissolving the pyrolyzed solid alkali product with condensed water to obtain a sodium hydroxide solution again, namely a circulating absorption liquid, and returning the circulating absorption liquid to a tail gas absorption process for use.
The process method avoids the problem of difficult separation treatment caused by the coexistence of sodium nitrate, sodium nitrite and residual alkali in the absorption alkali liquor, and adopts a high-temperature pyrolysis mode to decompose nitrate with different valence states to generate nitrogen oxide gas and alkali, the alkali is recycled, and the nitrogen oxide gas returns to an acid making system. The acid-base synchronous separation mode is a simple feasible route without secondary pollution products for realizing the regeneration of the absorption alkali liquor.
Claims (4)
1. The method for realizing the regeneration of the alkali liquor absorbed by the nitric oxide tail gas through acid-base synchronous separation is characterized in that the alkali liquor absorbed by the nitric oxide tail gas is the absorption alkali liquor generated by the absorption of the tail gas containing the nitric oxide by the liquid alkali in the nitric acid production or nitric acid related application field, and the method for regenerating the absorption alkali liquor comprises the following steps:
a) absorbing alkali liquor by the nitrogen oxide tail gas, atomizing and pyrolyzing to produce solid alkali and pyrolysis flue gas;
b) cooling the produced pyrolysis flue gas to obtain condensed water and high-concentration nitrogen oxide flue gas;
c) sending the high-concentration nitrogen oxide flue gas into a nitrogen oxide flue gas acid making system to prepare nitric acid;
d) dissolving the solid alkali in the step a) by using the condensed water in the step b) to obtain sodium hydroxide alkali liquor again, and returning the alkali liquor to the nitric oxide tail gas absorption system for recycling.
2. The method for realizing the regeneration of the nitric oxide tail gas absorption alkali liquor through acid-base synchronous separation according to claim 1, wherein the nitric oxide tail gas absorption alkali liquor comprises the following main components: na (Na)+ 105~120 g/L、NO3 -/NO2 - 200-250 g/L、OH- 15~20 g/L。
3. The method for realizing alkali liquor regeneration by nitrogen oxide tail gas absorption through acid-base synchronous separation according to claim 1 or 2, wherein in the step a), the pyrolysis temperature of the atomization pyrolysis is 600-800 ℃, and the pyrolysis time is 3-5 min.
4. The method for realizing alkali liquor regeneration by nitrogen oxide tail gas absorption through acid-base synchronous separation according to claim 1 or 2, wherein in step b), the volume fraction of nitrogen oxides in the high-concentration nitrogen oxide flue gas is 55-60%.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202110636093.7A CN113332857A (en) | 2021-06-08 | 2021-06-08 | Method for realizing alkali liquor regeneration by nitrogen oxide tail gas absorption through acid-base synchronous separation |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202110636093.7A CN113332857A (en) | 2021-06-08 | 2021-06-08 | Method for realizing alkali liquor regeneration by nitrogen oxide tail gas absorption through acid-base synchronous separation |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN113332857A true CN113332857A (en) | 2021-09-03 |
Family
ID=77475205
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202110636093.7A Pending CN113332857A (en) | 2021-06-08 | 2021-06-08 | Method for realizing alkali liquor regeneration by nitrogen oxide tail gas absorption through acid-base synchronous separation |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN113332857A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115155287A (en) * | 2022-06-16 | 2022-10-11 | 西安明时工程技术有限责任公司 | Process for improving gas conversion efficiency in sodium sulfate production device |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB1411330A (en) * | 1973-09-19 | 1975-10-22 | Tsukishima Kikai Co | Process for desulphurisation of waste gas |
| JPH0523535A (en) * | 1991-07-19 | 1993-02-02 | Hitachi Ltd | Removal of acidic gas from combustion exhaust gas |
| CN1362279A (en) * | 2001-12-21 | 2002-08-07 | 四川师范大学 | Recovery and utilization method of nitroxide in waste gas |
| CN103987443A (en) * | 2011-08-22 | 2014-08-13 | 琳德股份公司 | Improved nitric acid production |
| CN109721038A (en) * | 2019-02-19 | 2019-05-07 | 眉山顺应动力电池材料有限公司 | A kind of nitrate pyrolysis recycling method of nitric acid and apparatus system |
-
2021
- 2021-06-08 CN CN202110636093.7A patent/CN113332857A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB1411330A (en) * | 1973-09-19 | 1975-10-22 | Tsukishima Kikai Co | Process for desulphurisation of waste gas |
| JPH0523535A (en) * | 1991-07-19 | 1993-02-02 | Hitachi Ltd | Removal of acidic gas from combustion exhaust gas |
| CN1362279A (en) * | 2001-12-21 | 2002-08-07 | 四川师范大学 | Recovery and utilization method of nitroxide in waste gas |
| CN103987443A (en) * | 2011-08-22 | 2014-08-13 | 琳德股份公司 | Improved nitric acid production |
| CN109721038A (en) * | 2019-02-19 | 2019-05-07 | 眉山顺应动力电池材料有限公司 | A kind of nitrate pyrolysis recycling method of nitric acid and apparatus system |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115155287A (en) * | 2022-06-16 | 2022-10-11 | 西安明时工程技术有限责任公司 | Process for improving gas conversion efficiency in sodium sulfate production device |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| AU2014383726B2 (en) | Method for recycling lead oxide-containing waste material | |
| CN211521596U (en) | System for preparing analytically pure sulfuric acid from smelting flue gas | |
| CN109468468B (en) | Method for comprehensively utilizing and treating molybdenum-copper slag | |
| CN113332857A (en) | Method for realizing alkali liquor regeneration by nitrogen oxide tail gas absorption through acid-base synchronous separation | |
| CN104498974A (en) | Method for recycling mixed acid from cold-rolling stainless steel acid washing waste liquid | |
| CN113415813A (en) | Method for recovering lithium nickel cobalt manganese from waste ternary battery material | |
| TW201532714A (en) | Method and apparatus for producing copper oxide therewith | |
| CN102755829A (en) | Desulfurizer and application thereof | |
| WO2018113177A1 (en) | Process for clean production of electronic grade high-purity copper oxide | |
| CN109336177B (en) | Method for cleanly producing high-purity vanadium pentoxide by using hydrogen peroxide and ammonia water | |
| CN111183726B (en) | Method for treating waste acid generated by nitration of dinitrotoluene | |
| CN112174209B (en) | Green molybdenum smelting ion exchange process | |
| CN106379875B (en) | A kind of production method of nitrosylsulfuric acid and application | |
| CN101792862B (en) | Method for recovering metal through purified flue gas of scrap nickel-hydrogen battery | |
| CN112619399B (en) | Tail gas treatment method in nitrosyl sulfuric acid preparation process | |
| CN112591722B (en) | Method for co-producing industrial-grade nitric acid and electronic-grade nitric acid | |
| CN112279275A (en) | Method for removing potassium and sodium chloride in ore sintering fly ash and recycling potassium and sodium chloride | |
| CN112642431B (en) | Preparation process of methanol synthesis catalyst | |
| CN102992469A (en) | Method for treating sodium sulfide waste water | |
| CN103086419B (en) | Wet-method zinc oxide preparation method | |
| CN106517116A (en) | Industrial waste nitric acid comprehensive utilization process | |
| CN114349043A (en) | Method for recovering lead oxide from waste lead paste | |
| CN113149082A (en) | Method for producing high-purity ferrous sulfate water and ferrous sulfate heptahydrate by using waste acid | |
| CN101695625A (en) | Method for treating tail gas generated by preparing nickel sulfate solution by metal nickel method | |
| CN102351218B (en) | Process for removing carbon dioxide in combined alkali preparation method |
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 | ||
| RJ01 | Rejection of invention patent application after publication | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20210903 |