US3822339A - Method for removing sulfur dioxide from the exhaust of a combustion furnace - Google Patents
Method for removing sulfur dioxide from the exhaust of a combustion furnace Download PDFInfo
- Publication number
- US3822339A US3822339A US00256145A US25614572A US3822339A US 3822339 A US3822339 A US 3822339A US 00256145 A US00256145 A US 00256145A US 25614572 A US25614572 A US 25614572A US 3822339 A US3822339 A US 3822339A
- Authority
- US
- United States
- Prior art keywords
- circulating
- solution
- jointly
- coke oven
- ammonium
- 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.)
- Expired - Lifetime
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Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
- C01C1/00—Ammonia; Compounds thereof
- C01C1/02—Preparation, purification or separation of ammonia
- C01C1/12—Separation of ammonia from gases and vapours
-
- 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
- B01D53/48—Sulfur compounds
- B01D53/50—Sulfur oxides
- B01D53/501—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
- C01C1/00—Ammonia; Compounds thereof
- C01C1/24—Sulfates of ammonium
- C01C1/245—Preparation from compounds containing nitrogen and sulfur
- C01C1/246—Preparation from compounds containing nitrogen and sulfur from sulfur-containing ammonium compounds
- C01C1/247—Preparation from compounds containing nitrogen and sulfur from sulfur-containing ammonium compounds by oxidation with free oxygen
Definitions
- This method is characterized by the following steps: causing the exhaust gas of a combustion furnace containing S and coke oven gas containing NH to contact two circulating solutions separately, in each of which there are dissolved ammonium sulfite, ammonium bisulfite and ammonium sulfate; circulating a portion of each of said two self-circulating solutions jointly; continuously drawing out a portion of said jointly circulating solutions; continuously supplementing a decrease of solutions in all the circulation systems with fresh water; and maintaining the pH value of each circulating solution at a level of about 6.5 by controlling the flow rates of said coke oven gas and jointly circulating solution and the rate at which there should be drawn out a portion of said jointly circulating solution,
- This invention relates to a method for removing injurious sulfur dioxide from the exhaust of a fuel combustion furnace or sintering apparatus, and more particularly to the one concurrently capable of removing ammonia from coke oven gas.
- Still another known means is wet desulfurization using an alkaline liquor such as a water solution of caustic soda or a water suspension of slaked lime as an absorbent of sulfur dioxide.
- an alkaline liquor such as a water solution of caustic soda or a water suspension of slaked lime as an absorbent of sulfur dioxide.
- the spent absorbent can never be recovered, so that the operation of this method would be considerably uneconomical.
- the waste liquor could not be put to any further practical use, and would have to be thrown away. This would, therefore, raise another problem of public pollution.
- An object of the present invention is to provide an improved method for removing sulfur dioxide from the exhaust of a large scale fuel combustion furnace such as a 3,822,339 Patented July 2, 1974 boiler furnace of a steam power plant, with ease and at low cost.
- Another object of the present invention is to provide a similar method suitable for desulfurization of the exhaust from an iron ore sintering apparatus of an ironworks.
- a further object of the present invention is to provide a similar method concurrently capable of removing ammonia from coke oven gas which is present near the above-mentioned fuel combustion furnace or the sintering apparatus.
- step (c) Continuously pouring a portion of said first circulating solution of step (a) into said second circulating solution of step (b) and concurrently pouring almost the same amount of said second circulating solution of step (b) into that of step (a), thereby forming a jointly circulation system;
- step (c) Continuously drawing off a portion of the jointly circulating solutions of step (c), and concurrently supplementing a decrease of the solutions in all the circulating systems with fresh water, and utilizing the drawn situs to recover ammonium sulfate by means of oxidation;
- step (e) Maintaining the pH values of the circulating solutions of steps (a) and (b) at prescribed level by controlling the flow rates of the coke oven gas of step (b) and the jointly circulating solution of step (c) and the rate at which there should be drawn off part of the jointly circulating solution of step (d).
- the principle of the process in accordance with this invention consists in neutralizing the sulfur dioxide contained in an exhaust of the boiler furnace of a steam power plant or a sintering apparatus of an ironworks indirectly with ammonia contained in coke oven gas by a wet process.
- an absorber 2 is supplied with an aqueous dissolving liquor 1 containing ammonium sulfite, ammonium bisulfite and ammonium sulfate and having a pH value of from 5.8 to 6.5, and a total concentration of said ammonium salts is from 30 to 40% by weight.
- Exhaust gas from a combustion furnace 3 is passed through the absorber 2 by a blower 4 to contact the liquor 1 in said absorber, thereby dissolving the sulfur dioxide contained in the exhaust in said aqueous solution almost thoroughly.
- the desulfurized gas is released into the air through a chimney 18. In this case the exhaust gas is cooled in advance to a temperature of about 50 C.
- the liquor 1 is circulatingly introduced into the absorber 2 through a pump 5 and a liquor storage tank 6. In this system, the pH value of the circulating liquor decreases gradually as the sulfur dioxide is gradually dissolved therein unless another high pH solution is added.
- Another absorber 8 is supplied with another aqueous dissolving liquor 7 containing the same salts as in the aforementioned liquor 1, having a pH value of from 6.3 to 7.0 and the same range of total concentration as in the liquor 1.
- Exhaust gas from a coke oven 13 is passed through the absorber 8 by a blower 15 to contact the liquor 7 in said absorber, thereby disolving the ammonia contained in the coke oven gas in said aqueous solution almost thoroughly.
- the coke oven gas 17 thus treated to be almost stripped of ammonia is conducted to the place where it is utilized.
- the coke oven gas is also cooled in advance to a temperature of about 50 C.
- the liquor 7 is brought circulatingly into the absorber 8 through a pump 9 and a liquor storage tank 10. In this system, the pH value of the circulating liquor increases gradually as the ammonia is dissolved therein by degrees, unless another low pH solution is added.
- the second circulating solution 7 be continuously drawn off from the storage tank to avoid the accumulation of ammonium salts in all of the circulating systems, and a suitable amount of fresh water 16 be concurrently poured into the storage tank 10 in order to supplement therewith a decreased amount of circulating solutions in all the circulating systems.
- the quantity of the circulating solutions also decreases due to evaporation of the liquors in the absorbers as well as the above-mentioned withdrawal of the second circulating solution 7.
- the drawn liquor is accumulated in another storage tank 14, and supplied to an ammonium sulfate recovering plant.
- the ammonium sulfite and ammonium bisulfite in the drawn liquor may be changed into ammonium sulfate by means of a well-known oxidation method without difficulty.
- the dissolved ammonium thiosulfate circulates through all the circulating systems, and is partly drawn off from the systems together with other ammonium salts, and further, is changed into ammonium sulfate by oxidation in the aforementioned ammonium sulfate recovering plant.
- the main chemical reactions in the absorbers 2 and 8 are as follows:
- the pH values of the first and second circulating solutions 1 and 7 should be kept constant in the range of from 5.8 to 6.5 and from 6.3 to 7.0 respectively.
- the maintenance of these pH values is effected by controlling the flow rates of coke oven gas and the jointly circulating solution and the rate at which there should be drawn off a portion of said jointly circulating solution.
- the total concentrations of ammonium salts in all the circulating systems can be elevated to a relatively high level, for example, 30 to 40 percent, and
- the pH value throughout all the circulation systems may be set at a single level of about 6.4 (or 6.3 to 6.5). This arrangement, enables sulfur dioxide and ammonium to be eliminated from the exhaust of the combustion furnace and coke oven gas in as high amounts as more than respectively.
- Ammonia gas contained in coke oven gas is generally removed by sulfuric acid. In the present invention, however, there is no need of using expensive sulfuric acid, rendering the whole operation very economical and harmless. Furthermore, the waste liquor from the ammonium sulfate recovering plant does not give rise to any public pollution.
- hydrogen sulfide can be removed from coke oven gas in the absorber 8 to an extent of from 20 to 25 percent on the basis of the total weight of the hydrogen sulfide when the second circulating solution 7 has a pH value of from 6.3 to 6.5, and to a much higher extent of from 40 to 45 percent when said pH value ranges from 6.8 to 7.0.
- the absorber 2 can be safely operated at a temperature of about 50 C. without evolving the mist of ammonium sulfite. Moreover, this temperature enables outlet gas from the absorber 2 to be easily drawn off through the chimney 18 by its own buoyancy.
- the total concentration of ammonium salts in all the circulating solutions be kept at from 30 to 40 percent as mentioned 'before.
- the total concentration of ammonium salts in all the circulating solutions be kept at from 30 to 40 percent as mentioned 'before.
- it is able to circulate water first throughout the circulation system. In this case, arrangement is made to cause the total concentration of ammonium salts to increase gradually during operation up to a prescribed level.
- the absorber may consist of any of a spray tower, packed tower, multi-tray tower and wet wall tower, or if necessary several towers arranged in series or parallel. Further, where desired, either counter current system or parallel current system may be adopted for gas absorption.
- the method according to the present invention may be favourably practised in the place where a fuel-fired furnace such as a boiler furnace and a coke oven are located near to each other.
- a fuel-fired furnace such as a boiler furnace and a coke oven are located near to each other.
- composition of coke-oven gas (by volume):
- the exhaust gas cooled to about 50 C. was introduced into a SO -absorbing tower at a bottom thereof at the rate of 484 Nm. per hour, and an absorbing solution, having a temperature of 46 C. and a pH value of 6.3 was circulated through said tower at a rate of 35 liters per minute.
- the S0 content in the outlet gas from the tower was 22 p.p.m., showing that the gas was absorbed to an extent of 96.7%.
- the coke-oven gas cooled to about 50 C. was introduced into an NH -absorbing tower at the bottom thereof at the rate of 177 Nm. per hour, and an absorbing solution having a temperature of 40 C. and pH value of 6.45 was circulated through said tower at the rate of 50 liters per minute.
- the contents of NH, and H 8 in the outlet gas from the tower were 0.88 g./Nm. and 2.7 g./Nm. respectively, indicating that NH and H 8 were absorbed to an extent of 87.3% and 45% respectively.
- a portion of the circulating solution for S0 absorption and a portion of the circulating solution for NH absorption were made to be circulated jointly at the rate of liters per minute, and a portion of said jointly circulating solution was drawn off at a rate of 65 ml. per minute, and further water was supplied to said jointly circulating solution at the rate of 87 ml. per minute.
- concentrations of ammonium salts in the jointly circulating solution were as follows:
- EXAMPLE 2 After being cooled to about 50 C., exhaust gas from a sintering apparatus containing 1165 p.p.m. of S0 was introduced into the same SO -absorbing tower as in Example l at a rate of 438 Nm. per hour, and an absorbing solution, having a temperature of 48 C. and a pH value of 6.11, was circulated through said tower at a rate of 35 liters per minute.
- the S0 content in the outlet gas from the tower was 28 p.p.m., the S0 being removed as much as 97.7%.
- a coke oven gas containing 5.1 g./Nm. of NH, and 5.1 gJNmS of H 8 was introduced, after cooled to about 50 C., into the same NH -absorbing tower as in Example 1 at a rate of 141 Nm. per hour, and an absorbing solution having a temperature of 45 C. and a pH value of 6.5 was circulated through said tower at a rate of 50 liters per minute.
- the contents of NH and H S in the outlet gas from the tower were 0.19 g./ Nm. and 3.8 g./Nm. respectively, the removal of NH and H 8 amounting to 96.6% and 25% respectively.
- a method for removing sulfur dioxide from the exhaust of a combustion furnace comprising:
- step (c) continuously pouring a portion of said first circulating solution of step (a) into said second circulating solution of step (b) and concurrently pouring almost the same amount of said second circulating solution of step (b) into that of step (a), thereby forming a jointly circulating solution;
- step (d) continuously drawing off a portion of the jointly circulating solution of step (c), and concurrently supplementing a decrease of the solutions in all the circulating systems with fresh water, and utilizing the drawn solution to recover ammonium sulfate therefrom by means of oxidation;
- step (e) keeping the pH values of the circulating solutions of steps (a) and (b) at prescribed levels by controlling the flow rates of coke oven gas of step (b) and the jointly circuating solution of step (c) and the rate at which there should be drawn 01f part of the jointly circulating solution of step (d).
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Analytical Chemistry (AREA)
- Inorganic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- Environmental & Geological Engineering (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Treating Waste Gases (AREA)
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP46039800A JPS5111593B1 (it) | 1971-06-08 | 1971-06-08 |
Publications (1)
Publication Number | Publication Date |
---|---|
US3822339A true US3822339A (en) | 1974-07-02 |
Family
ID=12563016
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
US00256145A Expired - Lifetime US3822339A (en) | 1971-06-08 | 1972-05-23 | Method for removing sulfur dioxide from the exhaust of a combustion furnace |
Country Status (9)
Country | Link |
---|---|
US (1) | US3822339A (it) |
JP (1) | JPS5111593B1 (it) |
BE (1) | BE784594A (it) |
DE (1) | DE2227952C3 (it) |
FR (1) | FR2140419B1 (it) |
GB (1) | GB1379101A (it) |
IT (1) | IT958239B (it) |
NL (1) | NL145199B (it) |
SE (1) | SE397922B (it) |
Cited By (8)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US3957951A (en) * | 1974-08-23 | 1976-05-18 | International Telephone And Telegraph Corporation | Process for removing contaminants from hot waste gas streams |
US3959440A (en) * | 1974-05-08 | 1976-05-25 | Nippon Kokan Kabushiki Kaisha | Method for removing SO2 and NOx simultaneously from the exhaust of a combustion furnace |
US4001374A (en) * | 1973-07-02 | 1977-01-04 | Dr. C. Otto & Comp. G.M.B.H. | Process for removing ammonia from gases |
US4042348A (en) * | 1976-08-02 | 1977-08-16 | Apollo Chemical Corporation | Method of conditioning flue gas to electrostatic precipitator |
US4043768A (en) * | 1976-04-05 | 1977-08-23 | Apollo Chemical Corporation | Method of conditioning flue gas to electrostatic precipitator |
US9582705B2 (en) | 2014-08-31 | 2017-02-28 | Qualcomm Incorporated | Layered filtering for biometric sensors |
US9665763B2 (en) * | 2014-08-31 | 2017-05-30 | Qualcomm Incorporated | Finger/non-finger determination for biometric sensors |
US9911184B2 (en) | 2014-08-31 | 2018-03-06 | Qualcomm Incorporated | Air/object determination for biometric sensors |
Families Citing this family (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN100391578C (zh) * | 2006-06-16 | 2008-06-04 | 中国科学院南海海洋研究所 | 一种空气净化材料及其制备方法 |
CN103623689B (zh) | 2013-12-12 | 2016-06-29 | 北京博源恒升高科技有限公司 | 多元醇复合溶液脱除气体中SOx的方法 |
CN114904874B (zh) * | 2021-05-08 | 2023-05-23 | 宜兴大平杆塔制造有限公司 | 一种镀锌车间用锌烟收集装置的使用方法 |
-
1971
- 1971-06-08 JP JP46039800A patent/JPS5111593B1/ja active Pending
-
1972
- 1972-05-23 GB GB2419472A patent/GB1379101A/en not_active Expired
- 1972-05-23 US US00256145A patent/US3822339A/en not_active Expired - Lifetime
- 1972-05-26 SE SE7206902A patent/SE397922B/xx unknown
- 1972-06-02 FR FR7219845A patent/FR2140419B1/fr not_active Expired
- 1972-06-05 NL NL727207578A patent/NL145199B/xx not_active IP Right Cessation
- 1972-06-07 IT IT50733/72A patent/IT958239B/it active
- 1972-06-08 BE BE784594A patent/BE784594A/xx not_active IP Right Cessation
- 1972-06-08 DE DE2227952A patent/DE2227952C3/de not_active Expired
Cited By (8)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4001374A (en) * | 1973-07-02 | 1977-01-04 | Dr. C. Otto & Comp. G.M.B.H. | Process for removing ammonia from gases |
US3959440A (en) * | 1974-05-08 | 1976-05-25 | Nippon Kokan Kabushiki Kaisha | Method for removing SO2 and NOx simultaneously from the exhaust of a combustion furnace |
US3957951A (en) * | 1974-08-23 | 1976-05-18 | International Telephone And Telegraph Corporation | Process for removing contaminants from hot waste gas streams |
US4043768A (en) * | 1976-04-05 | 1977-08-23 | Apollo Chemical Corporation | Method of conditioning flue gas to electrostatic precipitator |
US4042348A (en) * | 1976-08-02 | 1977-08-16 | Apollo Chemical Corporation | Method of conditioning flue gas to electrostatic precipitator |
US9582705B2 (en) | 2014-08-31 | 2017-02-28 | Qualcomm Incorporated | Layered filtering for biometric sensors |
US9665763B2 (en) * | 2014-08-31 | 2017-05-30 | Qualcomm Incorporated | Finger/non-finger determination for biometric sensors |
US9911184B2 (en) | 2014-08-31 | 2018-03-06 | Qualcomm Incorporated | Air/object determination for biometric sensors |
Also Published As
Publication number | Publication date |
---|---|
NL7207578A (it) | 1972-12-12 |
SE397922B (sv) | 1977-11-28 |
FR2140419B1 (it) | 1976-12-03 |
FR2140419A1 (it) | 1973-01-19 |
JPS5111593B1 (it) | 1976-04-12 |
BE784594A (fr) | 1972-10-02 |
NL145199B (nl) | 1975-03-17 |
IT958239B (it) | 1973-10-20 |
DE2227952B2 (de) | 1974-06-27 |
DE2227952C3 (de) | 1975-02-20 |
DE2227952A1 (de) | 1973-01-04 |
GB1379101A (en) | 1975-01-02 |
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