CN110075687B - System and process for separating chlorine in ammonia-containing gas by direct stripping method - Google Patents
System and process for separating chlorine in ammonia-containing gas by direct stripping method Download PDFInfo
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- CN110075687B CN110075687B CN201910410037.4A CN201910410037A CN110075687B CN 110075687 B CN110075687 B CN 110075687B CN 201910410037 A CN201910410037 A CN 201910410037A CN 110075687 B CN110075687 B CN 110075687B
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/34—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping with one or more auxiliary substances
- B01D3/38—Steam distillation
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- 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
- B01D53/68—Halogens or halogen compounds
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- 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
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- 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
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/20—Halogens or halogen compounds
- B01D2257/206—Organic halogen compounds
- B01D2257/2064—Chlorine
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P70/00—Climate change mitigation technologies in the production process for final industrial or consumer products
- Y02P70/10—Greenhouse gas [GHG] capture, material saving, heat recovery or other energy efficient measures, e.g. motor control, characterised by manufacturing processes, e.g. for rolling metal or metal working
Abstract
The invention provides a system and a process for separating chlorine in ammonia-containing gas by a direct stripping method, wherein the process for separating chlorine in ammonia-containing gas by the direct stripping method comprises the following steps: mixing and stripping the high-temperature gas and the alkali liquor in a stripping tower, reacting alkali metal in the alkali liquor with chlorine to generate a chlorine alkali metal compound, and allowing the chlorine alkali metal compound to enter stripping waste water to realize chlorine separation, wherein the ammonia nitrogen content in the stripping waste water is lower than 200 mg/l; and after the gas escaping from the top of the stripping tower is condensed and cooled in a partial condenser of the stripping tower, the gas phase (ammonia vapor) is sent to a subsequent system, and the liquid phase returns to the first tower plate on the stripping tower. The invention makes the ammonia nitrogen content in the stripping waste water lower than 200mg/l by adding alkali for stripping, and effectively improves the separation degree of ammonia and chlorine.
Description
Technical Field
The invention relates to a process for separating chlorine from ammonia-containing gas, in particular to a system and a process for separating chlorine from ammonia-containing gas by a direct stripping method.
Background
There is no technology for directly separating chlorine from ammonia-containing gas at high temperature of 100-300 ℃.
Disclosure of Invention
The invention aims to provide a process for separating chlorine in ammonia-containing gas by a direct stripping method, aiming at solving the problem that a method for separating ammonia and chlorine from high-temperature gas at 100-300 ℃ does not exist.
In order to achieve the purpose, the invention adopts the technical scheme that: a process for separating chlorine from ammonia-containing gas by direct stripping comprises the following steps: mixing and stripping the high-temperature gas and the alkali liquor in a stripping tower, reacting alkali metal (sodium or potassium) in the alkali liquor with chlorine to generate a chlorine alkali metal compound, and allowing the chlorine alkali metal compound to enter stripping wastewater to realize chlorine separation; and after the gas escaping from the top of the stripping tower is condensed and cooled in a partial condenser of the stripping tower, the gas phase (ammonia vapor) is sent to a subsequent system, and the liquid phase returns to the first tower plate on the stripping tower.
Further, high-temperature gas enters the middle part of the stripping tower, and 5-25 tower plates and 1-30 tower plates are respectively arranged above and below a feed plate of the stripping tower; the alkali liquor directly enters the second or third tower plate on the stripping tower.
Further, the temperature of the high-temperature gas is 100-300 ℃, and the gas contains hydrogen, carbon monoxide, carbon dioxide, hydrogen sulfide and water vapor besides ammonia and chlorine; wherein the volume concentration of ammonia and chlorine in the gas is 1-75% and 0.01-5%, respectively.
Further, the content of ammonia nitrogen in the stripping wastewater is lower than 200 mg/l.
Further, the alkali liquor is one or more of a sodium hydroxide solution, a sodium hydroxide potassium solution, a sodium carbonate solution, a sodium bicarbonate solution, a potassium carbonate solution and a potassium bicarbonate solution, and the mass concentration of the alkali liquor is 1-nearly saturated.
Further, the molar ratio of alkali metal in the alkali liquor to chlorine in the high-temperature gas is 1-2.
The invention also discloses a system for separating chlorine in ammonia-containing gas by the direct stripping method, which comprises a stripping dephlegmator and a stripping tower, wherein a gas outlet at the top of the stripping tower is communicated with an inlet of the stripping dephlegmator, and a liquid phase outlet at the bottom of the stripping dephlegmator is communicated with the stripping tower; 5-25 tower plates and 1-30 tower plates are respectively arranged above and below the feeding plate of the stripping tower; the alkali liquor inlet is positioned on the second tower plate or the third tower plate which is arranged on the stripping tower.
Further, the stripping dephlegmator is arranged at the top of the stripping tower, or the stripping dephlegmator and the stripping tower are independently arranged.
The tower bottom liquid outlet is communicated with a refrigerant inlet of the stripping heater, and the tower bottom liquid inlet is communicated with a refrigerant outlet of the stripping heater.
And further, a stripping waste water cooler is included, and a bottom liquid outlet of the stripping tower is communicated with a heating medium inlet of the stripping waste water cooler.
The invention is based on the principle of acid-base reaction, chlorine reacts with alkali metal sodium or potassium to produce stable strong acid-base salt, the salt is dissolved in liquid phase, and ammonia remains in gas phase, thus realizing the separation of chlorine in ammonia-containing gas. By adding alkali for stripping, the ammonia nitrogen content in the stripping waste water is lower than 200mg/l, and the separation degree of ammonia and chlorine is improved. The process for separating the chlorine in the ammonia-containing gas by the direct stripping method is simple and easy to implement and has a good separation effect.
Drawings
FIG. 1 is a schematic structural diagram of a system for separating chlorine from an ammonia-containing gas by direct stripping in example 1 of the present invention.
FIG. 2 is a schematic structural diagram of a system for separating chlorine from an ammonia-containing gas by direct stripping in example 3 of the present invention.
Wherein the reference numerals are respectively:
1-a stripping column; 2-steam stripping dephlegmator; 3-a stripping heater; 4-stripping waste water cooler.
Detailed Description
The invention discloses a process for separating chlorine in ammonia-containing gas by a direct stripping method, which comprises the following steps:
the high-temperature gas containing ammonia and chlorine directly enters the middle part of the stripping tower and is contacted with a liquid phase containing alkali metal sodium or potassium from top to bottom plate by plate, the chlorine and the alkali metal sodium or potassium react to generate sodium chloride or potassium chloride until the chlorine is completely separated from a gas phase, and the alkali metal chloride completely enters the liquid phase and is finally discharged along with stripping waste water; the ammonia left in the gas phase escapes from the top of the stripping tower along with the ammonia vapor, enters a stripping dephlegmator, is cooled and segregated by cooling water or heat recovery media, and then ammonia vapor without chlorine is sent to a subsequent system, and the liquid phase of the stripping dephlegmator is used as reflux and returns to the 1 st tower plate on the upper part of the stripping tower;
the alkali liquor is counted from the 2 nd or 3 rd tower plate on the stripping tower, and reacts with chlorine and ammonium chloride in the liquid phase in the process of going down from plate to plate;
in order to ensure that the reaction of alkali metal sodium or potassium and chlorine is complete, 2-22 tower plates are arranged between an alkali feeding plate and a high-temperature ammonia-and-chlorine-containing gas feeding plate;
in order to ensure that chlorine is completely reacted, the molar ratio of alkali metal in the alkali liquor to chlorine in the high-temperature gas is 1-2;
in order to ensure that the alkali metal and ammonium chloride completely react, the content of ammonia nitrogen in the stripping wastewater is controlled to be lower than 200mg/l, and 1-30 tower plates are arranged below a high-temperature ammonia and chlorine-containing gas feeding plate.
The top of the stripping tower is provided with a stripping dephlegmator, or the stripping dephlegmator and the stripping tower are independently arranged; the ammonia gas without chlorine entering the stripping dephlegmator is condensed and cooled by cooling water or heat recovery medium, the liquid phase of the stripping dephlegmator is used as reflux, and flows out from the bottom of the stripping dephlegmator and enters the 1 st tower plate on the stripping tower. The ammonia steam without chlorine escaping from the top of the stripping dephlegmator is sent to a subsequent system;
the stripping tower can be a plate tower or a packed tower or a combined tower of a plate tower and a packing;
the number of the tower plates of the plate tower can be converted into equivalent filler height according to the performance of the filler;
the invention adopts the plate tower, which is convenient for description;
both tray columns and packed columns are commercially available technologies.
In order to further reduce the ammonia content in the liquid phase, a stripping heater is arranged at the bottom of the stripping tower, and heating media such as steam or heat transfer oil are used as heating sources.
The stripping waste water discharged from the bottom of the stripping tower is cooled by cooling water or a heat recovery medium in a stripping waste water cooler and then is sent to a subsequent system.
The temperature of chlorine and ammonia gas is 100-300 ℃, the gas also contains hydrogen, carbon monoxide, carbon dioxide, hydrogen sulfide, water vapor and other components, and the volume concentration of ammonia and chlorine in the gas is 1-75% and 0.01-5% respectively.
The alkali liquor is sodium hydroxide solution, potassium hydroxide solution, sodium carbonate solution and sodium bicarbonate solution, potassium carbonate solution and potassium bicarbonate solution.
The mass concentration of the alkali liquor is 1-nearly saturated.
The invention also discloses a system for separating chlorine in ammonia-containing gas by direct stripping, which comprises a stripping tower, a stripping dephlegmator, a stripping heater and a stripping waste water cooler;
the steam stripping dephlegmator is connected with the steam stripping tower, and the gas phase escaping from the top of the steam stripping tower enters the steam stripping dephlegmator; in the stripping dephlegmator, after the vapor phase is cooled and dephlegmated by cooling water or heat recovery medium, the ammonia vapor is sent to the subsequent system from the top outlet of the stripping dephlegmator, the liquid phase at the bottom outlet of the stripping dephlegmator is used as reflux, and returns to the 1 st tower plate on the stripping tower;
the high-temperature ammonia and chlorine-containing gas directly enters the middle part of the stripping tower and contacts with a liquid phase in the tower, chlorine reacts with alkali metal sodium or potassium to generate sodium chloride or potassium chloride, and the sodium chloride or potassium chloride flows down to the bottom of the stripping tower along with the liquid phase; the ammonium chloride in the liquid phase reacts with the alkali metal sodium or potassium in the liquid phase to generate sodium chloride or potassium chloride;
high-temperature gas containing chlorine and ammonia is arranged on a feed plate in the middle of the stripping tower, and 5-25 tower plates and 1-30 tower plates are respectively arranged at the upper part and the lower part of the feed plate, so that chlorine can completely react with alkali metal sodium or potassium; and the ammonia nitrogen content in the stripping wastewater is lower than 200 mg/l.
The alkali liquor enters from the upper part of the stripping tower and flows from top to bottom along with the liquid phase, wherein the alkali metal sodium or potassium reacts with chlorine plate by plate, so that the chlorine reacts with the alkali metal sodium or potassium to generate sodium chloride or potassium chloride;
in order to avoid entrainment, an alkali liquor feeding plate is arranged on the 2 nd or 3 rd tower plate at the upper part of the stripping tower.
And the reflux of the stripping tower comes from a stripping dephlegmator.
The reflux was returned to the upper 1 st tray of the stripper column to maintain stable operation of the stripper column.
The heat supply of the stripping tower is from a stripping tower heater.
The heated liquid phase returns to the lower part of the stripping tower, and ammonia in the liquid phase is stripped into a gas phase, so that the content of ammonia nitrogen in the stripping wastewater is lower than 200 mg/l.
The temperature of the gas containing ammonia and chlorine is 100-300 ℃, the gas also contains components such as hydrogen, carbon monoxide, carbon dioxide, hydrogen sulfide, water vapor and the like, and the volume concentration of the ammonia and the chlorine in the gas is 1-75% and 0.01-5% respectively.
The alkali liquor is one or more of sodium hydroxide solution, potassium hydroxide solution, sodium carbonate solution and sodium bicarbonate solution, potassium carbonate solution and potassium bicarbonate solution, and the mass concentration of the alkali liquor is 1-nearly saturated.
The stripper heater is connected with the stripper; the liquid phase at the bottom of the stripping tower enters a stripping tower heater; in the stripper heater, the liquid phase is heated by a heating medium such as steam or heat transfer oil, and the liquid phase brings heat back to the stripper to supply heat for stripping.
The stripper wastewater cooler is connected with the stripper, and the liquid phase at the bottom of the stripper enters the stripper wastewater cooler; in the stripper wastewater cooler, after the liquid phase is cooled by cooling water or a heat recovery medium, the stripping wastewater is sent to a subsequent system from an outlet of the stripper wastewater cooler.
The invention is further illustrated by the following examples:
example 1
The embodiment discloses a system and a process for separating chlorine in ammonia-containing gas by a direct stripping method, and the system and the process are shown in figure 1 and comprise a stripping tower 1, a stripping dephlegmator 2, a stripping heater 3 and a stripping waste water cooler 4.
The stripping dephlegmator 2 is arranged at the top of the stripping tower 1, a gas outlet at the top of the stripping tower 1 is communicated with an inlet of the stripping dephlegmator 2, and a liquid phase outlet at the bottom of the stripping dephlegmator 2 is communicated with the stripping tower 1; 5-25 tower plates and 1-30 tower plates are respectively arranged above and below the feeding plate of the stripping tower 1; the alkali liquor inlet is positioned on the second tower plate or the third tower plate which is arranged on the stripping tower.
A tower bottom liquid outlet and a tower bottom liquid inlet are formed in the side wall below the tower plate at the bottom of the stripping tower 1, the tower bottom liquid outlet is communicated with the refrigerant inlet of the stripping heater 3, and the tower bottom liquid inlet is communicated with the refrigerant outlet of the stripping heater 3.
And a tower bottom liquid outlet at the bottom of the stripping tower 1 is communicated with a heating medium inlet of a stripping waste water cooler 4.
The high-temperature tower plate comprises components such as chlorine, ammonia, hydrogen, carbon monoxide, carbon dioxide, hydrogen sulfide, water vapor and the like at the temperature of 205-210 ℃, the volume concentration of the ammonia and the chlorine is respectively 20-25% and 0.1-0.2%, and the gas directly enters the 8 th tower plate (a feed plate) on the stripping tower 1; below the feed plate 30 trays were placed.
A sodium hydroxide solution with the mass concentration of 5-6% enters from the 2 nd tower plate on the stripping tower 1, sodium reacts with chlorine in a gas phase and a liquid phase to generate sodium chloride in the process of plate-by-plate descending on the feeding plate, and the sodium chloride is discharged along with stripping waste water; in the process of stripping plate by plate below the feeding plate, the ammonia nitrogen content in the wastewater after stripping is 150-180 mg/l.
The molar ratio of sodium to chlorine is 1.1 to 1.2.
The gas phase without chlorine at the temperature of 95-98 ℃ escapes from the top of the stripping tower 1 and enters the stripping dephlegmator 2, after being cooled and segregated by cooling water or heat recovery media, the ammonia gas at the temperature of 85-90 ℃ escapes from the outlet of the stripping dephlegmator 2 and is sent to a subsequent system; the liquid phase flows out from the bottom of the stripping dephlegmator 2 and returns to the 1 st tray at the upper part of the stripping tower 1.
Heating medium such as steam or heat transfer oil heats the waste water from the bottom of the stripping tower 1 in the stripping heater 3, and the heated waste water brings heat back to the stripping tower 1.
The stripping waste water discharged from the bottom of the stripping tower 1 is cooled by cooling water or a heat recovery medium in a stripping waste water cooler 4, and then discharged to a subsequent system.
Example 2
The embodiment discloses a system and a process for separating chlorine in ammonia-containing gas by a direct stripping method, which have the same structure as that of the embodiment 1, and comprise a stripping tower 1, a stripping dephlegmator 2, a stripping heater 3 and a stripping wastewater cooler 4.
The high-temperature tower comprises components such as chlorine, ammonia, hydrogen, carbon monoxide, carbon dioxide, hydrogen sulfide, water vapor and the like at the temperature of 115-125 ℃, the volume concentration of the ammonia and the chlorine is respectively 30-35% and 1.0-1.3%, the gas directly enters the middle part (a feed plate) of the stripping tower 1, 25 tower plates are arranged above the feed plate, and 20 tower plates are arranged below the feed plate.
A sodium carbonate solution with the mass concentration of 10-12% enters from the No. 3 tower plates on the stripping tower 1, sodium and chlorine in the gas phase react to generate sodium chloride in the process of descending from plate to plate above the feeding plate, and the sodium chloride is discharged along with stripping waste water; in the process of stripping plate by plate under the feeding plate, the ammonia nitrogen content in the wastewater after stripping is 50-80 mg/l.
The molar ratio of sodium to chlorine is 1.2 to 1.3.
The chlorine-free vapor phase at the temperature of 110-115 ℃ escapes from the top of the stripping tower 1 and enters the stripping dephlegmator 2, and after being cooled by cooling water and condensed to 110-115 ℃, ammonia vapor at the temperature of 105-115 ℃ escapes from the outlet of the stripping dephlegmator 2 and is sent to a subsequent system; the liquid phase flows out from the bottom of the stripping dephlegmator 2 and returns to the 1 st tray at the upper part of the stripping tower 1.
The steam heats the waste water from the bottom of the stripping column 1 in a stripping heater 3, and the heated waste water brings the heat back to the stripping column 1.
The stripping waste water discharged from the bottom of the stripping tower 1 is cooled by cooling water in a stripping waste water cooler 4 and then discharged to a subsequent system.
Example 3
The embodiment discloses a system and a process for separating chlorine in ammonia-containing gas by a direct stripping method, and the system and the process structurally comprise a stripping tower 1, a stripping dephlegmator 2, a stripping heater 3 and a stripping wastewater cooler 4 as shown in 3.
The stripping dephlegmator 2 and the stripping tower 1 are independently arranged, a gas outlet at the top of the stripping tower 1 is communicated with an inlet of the stripping dephlegmator 2, and a liquid phase outlet at the bottom of the stripping dephlegmator 2 is communicated with the stripping tower 1; 5-25 tower plates and 1-30 tower plates are respectively arranged above and below the feeding plate of the stripping tower 1; the alkali liquor inlet is positioned on the second tower plate or the third tower plate which is arranged on the stripping tower.
A tower bottom liquid outlet and a tower bottom liquid inlet are formed in the side wall below the tower plate at the bottom of the stripping tower 1, the tower bottom liquid outlet is communicated with the refrigerant inlet of the stripping heater 3, and the tower bottom liquid inlet is communicated with the refrigerant outlet of the stripping heater 3.
And a tower bottom liquid outlet of the stripping tower 1 is communicated with a heating medium inlet of a stripping waste water cooler 4.
The high-temperature stripping tower comprises components such as chlorine, ammonia, hydrogen, carbon monoxide, carbon dioxide, hydrogen sulfide, water vapor and the like at the temperature of 240-245 ℃, the volume concentration of the ammonia and the chlorine is respectively 55-60% and 1.5-1.6%, the gas directly enters the middle part of the stripping tower 1, 12 tower plates and fillers equivalent to the 12 tower plates are arranged on a feed plate, and the fillers equivalent to the 25 tower plates are arranged below the feed plate.
Potassium carbonate solution with the mass concentration of 20-22% enters from the 3 rd tower plate on the stripping tower 1, potassium and chlorine in the gas phase are completely reacted to generate potassium chloride in the process of plate-by-plate descending on the feeding plate, and the potassium chloride is discharged along with stripping waste water; in the process of stripping plate by plate under the feeding plate, the ammonia nitrogen content in the wastewater after stripping is 20-30 mg/l.
The molar ratio of potassium to chlorine is 1.5 to 1.6.
A chlorine-free vapor phase at the temperature of 140-150 ℃ escapes from the top of the stripping tower 1 and enters the stripping dephlegmator 2, and after being cooled and dephlegmated to 125-130 ℃ by a heat recovery medium, ammonia vapor at the temperature of 125-130 ℃ escapes from the outlet of the stripping dephlegmator 2 and is sent to a subsequent system; the liquid phase flows out from the bottom of the stripping dephlegmator 2 and returns to the 1 st tray at the upper part of the stripping tower 1.
The heat conducting oil heats the waste water from the bottom of the stripping tower 1 in the stripping heater 3, and the heated waste water brings the heat back to the stripping tower 1.
The stripping waste water discharged from the bottom of the stripping tower 1 is cooled by cooling water in a stripping waste water cooler 4 and then discharged to a subsequent system.
Finally, it should be noted that: the above embodiments are only used to illustrate the technical solution of the present invention, and not to limit the same; while the invention has been described in detail and with reference to the foregoing embodiments, it will be understood by those skilled in the art that: the technical solutions described in the foregoing embodiments may still be modified, or some or all of the technical features may be equivalently replaced; and the modifications or the substitutions do not make the essence of the corresponding technical solutions depart from the scope of the technical solutions of the embodiments of the present invention.
Claims (8)
1. A process for separating chlorine in ammonia-containing gas by a direct stripping method is characterized by comprising the following steps: mixing and stripping the high-temperature gas and alkali liquor in a stripping tower, wherein the molar ratio of alkali metal in the alkali liquor to chlorine in the high-temperature gas is 1-2; alkali metal in the alkali liquor reacts with chlorine to generate chlorine alkali metal compound, and the chlorine alkali metal compound enters the stripping wastewater to realize chlorine separation; after the gas escaping from the top of the stripping tower is condensed and cooled in a stripping tower dephlegmator, the gas phase is sent to a subsequent system, and the liquid phase returns to the first tower plate on the stripping tower;
the high-temperature gas enters the middle part of the stripping tower, and 5-25 tower plates and 1-30 tower plates are respectively arranged above and below a feed plate of the stripping tower; the alkali liquor directly enters the second or third tower plate on the stripping tower.
2. The process for separating chlorine from ammonia-containing gas by direct stripping according to claim 1, wherein the temperature of the high-temperature gas is 100-300 ℃, and the gas contains hydrogen, carbon monoxide, carbon dioxide, hydrogen sulfide and water vapor besides ammonia and chlorine; wherein the volume concentration of ammonia and chlorine in the gas is 1-75% and 0.01-5%, respectively.
3. The process for separating chlorine from ammonia-containing gas by direct stripping according to claim 1, wherein the ammonia nitrogen content in the stripping waste water is less than 200 mg/l.
4. The process for separating chlorine from ammonia-containing gas by direct stripping according to claim 1, wherein the alkali liquor is one or more of sodium hydroxide solution, potassium hydroxide solution, sodium carbonate solution, sodium bicarbonate solution, potassium carbonate solution and potassium bicarbonate solution, and the mass concentration of the alkali liquor is 1% to nearly saturation.
5. A system for separating chlorine in ammonia-containing gas by a direct stripping method is characterized by comprising a stripping dephlegmator and a stripping tower, wherein a gas outlet at the top of the stripping tower is communicated with an inlet of the stripping dephlegmator, and a liquid phase outlet at the bottom of the stripping dephlegmator is communicated with the stripping tower; 5-25 tower plates and 1-30 tower plates are respectively arranged above and below the feeding plate of the stripping tower; the alkali liquor inlet is positioned on the second tower plate or the third tower plate which is arranged on the stripping tower.
6. The system for separating chlorine in ammonia-containing gas by direct stripping according to claim 5, wherein the stripping dephlegmator is arranged at the top of the stripping tower, or the stripping dephlegmator and the stripping tower are arranged independently.
7. The system for separating chlorine in ammonia-containing gas by direct stripping according to claim 5 or 6, which comprises a stripping heater, wherein a bottom liquid outlet and a bottom liquid inlet are arranged on the side wall below the bottom tray of the stripping heater, the bottom liquid outlet is communicated with a refrigerant inlet of the stripping heater, and the bottom liquid inlet is communicated with a refrigerant outlet of the stripping heater.
8. The system for separating chlorine in ammonia-containing gas by direct stripping according to claim 5 or 6, which is characterized by comprising a stripping waste water cooler, wherein the bottom liquid outlet of the stripping tower is communicated with a heating medium inlet of the stripping waste water cooler.
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| CN1271690A (en) * | 1999-04-28 | 2000-11-01 | 辽宁中绿环境工程有限公司 | Process for treating ammonia-contained waste water |
| CN104445474A (en) * | 2014-12-10 | 2015-03-25 | 上海国际化建工程咨询公司 | Method and device for preparing diluted ammonia water from ammonia-containing shift condensate wastewater |
| CN104986817A (en) * | 2015-08-05 | 2015-10-21 | 贵州赤天化桐梓化工有限公司 | Method for treating sewage containing sulfur and ammonia during alternation working procedure of synthetic ammonia by using steam stripping method |
| CN106673012A (en) * | 2016-11-11 | 2017-05-17 | 中冶焦耐(大连)工程技术有限公司 | Process and device for producing strong ammonia water through negative pressure operation |
| CN106745062A (en) * | 2017-01-23 | 2017-05-31 | 中冶焦耐(大连)工程技术有限公司 | The technique and device of a kind of negative-pressure operation production concentrated ammonia liquor |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| BR112016020196B8 (en) * | 2014-03-05 | 2022-08-02 | Bechtel Hydrocarbon Technology Solutions Inc | SYSTEM AND METHOD FOR PURIFICATION OF AMMONIA |
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- 2019-05-17 CN CN201910410037.4A patent/CN110075687B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1271690A (en) * | 1999-04-28 | 2000-11-01 | 辽宁中绿环境工程有限公司 | Process for treating ammonia-contained waste water |
| CN104445474A (en) * | 2014-12-10 | 2015-03-25 | 上海国际化建工程咨询公司 | Method and device for preparing diluted ammonia water from ammonia-containing shift condensate wastewater |
| CN104986817A (en) * | 2015-08-05 | 2015-10-21 | 贵州赤天化桐梓化工有限公司 | Method for treating sewage containing sulfur and ammonia during alternation working procedure of synthetic ammonia by using steam stripping method |
| CN106673012A (en) * | 2016-11-11 | 2017-05-17 | 中冶焦耐(大连)工程技术有限公司 | Process and device for producing strong ammonia water through negative pressure operation |
| CN106745062A (en) * | 2017-01-23 | 2017-05-31 | 中冶焦耐(大连)工程技术有限公司 | The technique and device of a kind of negative-pressure operation production concentrated ammonia liquor |
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