CN107934989B - System for drying ammonium sulfate by utilizing desulfurization regeneration tail gas - Google Patents
System for drying ammonium sulfate by utilizing desulfurization regeneration tail gas Download PDFInfo
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- CN107934989B CN107934989B CN201711351522.6A CN201711351522A CN107934989B CN 107934989 B CN107934989 B CN 107934989B CN 201711351522 A CN201711351522 A CN 201711351522A CN 107934989 B CN107934989 B CN 107934989B
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- ammonium sulfate
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
- C01C1/00—Ammonia; Compounds thereof
- C01C1/24—Sulfates of ammonium
- C01C1/242—Preparation from ammonia and sulfuric acid or sulfur trioxide
-
- 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
- B01D53/58—Ammonia
-
- 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
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
- C01C1/00—Ammonia; Compounds thereof
- C01C1/24—Sulfates of ammonium
- C01C1/249—Deacidifying or drying the crystals
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/50—Inorganic acids
- B01D2251/506—Sulfuric acid
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Organic Chemistry (AREA)
- Environmental & Geological Engineering (AREA)
- Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- Inorganic Chemistry (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Industrial Gases (AREA)
- Gas Separation By Absorption (AREA)
Abstract
The invention relates to a system for drying ammonium sulfate by utilizing desulfurization regeneration tail gas, which comprises a regeneration tower, a drying tower, a heater, an ammonium sulfate drying unit, an ammonium sulfate crystallization unit and a cleaning unit, wherein the drying tower is connected with the heater; the invention adopts the regenerated tail gas of the ammonia wet oxidation desulfurization process as the ammonium sulfate drying gas; the regenerated tail gas is completely sent to an ammonium sulfate drying unit, so that ammonia loss and atmospheric pollution caused by directly discharging the regenerated tail gas to the atmosphere can be avoided; meanwhile, ammonia in the tail gas is recycled to an ammonium sulfate system, so that the yield of ammonium sulfate is increased; the power consumption of an air blower for drying ammonium sulfate can be saved; realizes the harmless treatment of the regenerated tail gas and the effective recycling of ammonia resources.
Description
Technical Field
The invention relates to the technical field of purification deamination of coke oven gas, in particular to a system for treating tail gas generated by desulfurization and regeneration of coke oven gas by a wet oxidation method and drying ammonium sulfate.
Background
The wet oxidation desulfurization process of coke oven gas has the characteristics of high desulfurization efficiency, simple operation and the like, and is popular and widely applied to coking enterprises in China. The wet oxidation desulfurization process can utilize ammonia in the coke oven gas as an alkali source, and does not need to add an alkali source.
The wet oxidation desulfurizing process with ammonia as alkali source consists of desulfurizing and regenerating steps. The main equipment of the regeneration part is a regeneration tower, the desulfurization rich liquid enters the bottom of the regeneration tower, and compressed air is introduced from the bottom of the regeneration tower, so that the desulfurization rich liquid is oxidized and regenerated in the tower. The regenerated desulfurization lean solution is returned to the desulfurization tower from the tower top for recycling. The sulfur foam floating at the top of the regeneration tower flows into a foam groove by utilizing the potential difference, and is concentrated and then is filled into a sulfur melting kettle, and a sulfur product is prepared by heating, dehydrating and melting; or the sulfur paste crude product is pumped into an automatic plate-and-frame filter press for filter pressing by a foam pump, and the obtained sulfur paste crude product is packaged and sold.
The compressed air used in the process of regenerating the desulfurizing liquid has the function of floating sulfur foam besides supplying oxygen to the desulfurizing liquid. Practice proves that the ammonia content in the tail gas discharged from the top of the regeneration tower reaches up to 2-4g/m 3 . The amount of ammonia lost with the regenerated tail gas and the resulting atmospheric pollution are not negligible. GB16171-2012 issued and implemented in 2012 (emission Standard for pollutants for coking chemical industry) prescribes that the emission limit of a desulfurization regeneration tower for particular emission limits of atmospheric pollutants has an ammonia content of 10mg/m 3 . The treatment of regenerated tail gas is a problem to be solved urgently in the current ammonia wet oxidation desulfurization process.
In addition, the deamination process for purifying coke oven gas is widely selected by domestic coking enterprises and is an ammonium sulfate production process, and the ammonium sulfate production process is divided into a crystallization system and a drying system. The ammonium sulfate drying system mainly adopts an air blower to suck air, then the air is heated by a heater, the hot air enters an ammonium sulfate dryer to dry wet ammonium sulfate, and tail gas of the dryer is discharged into the atmosphere after passing through a cleaning tower. Traditional dry air, air blower to provide power and heater to provide dry heat.
Generally, ammonium sulfate processes are often used to replenish water in the system in order to maintain water balance. The drying system absorbs the water in the ammonium sulfate crystal and simultaneously brings a part of water along with the discharge of the drying tail gas; this results in the entire ammonium sulphate process requiring on the one hand water replenishment and on the other hand bringing up a part of the water.
Disclosure of Invention
The invention provides a system for drying ammonium sulfate by utilizing desulfurization regenerated tail gas, which adopts regenerated tail gas of an ammonia wet oxidation desulfurization process as ammonium sulfate drying gas; the regenerated tail gas is completely sent to an ammonium sulfate drying unit, so that ammonia loss and atmospheric pollution caused by directly discharging the regenerated tail gas to the atmosphere can be avoided; meanwhile, ammonia in the tail gas is recycled to an ammonium sulfate system, so that the yield of ammonium sulfate is increased; the power consumption of an air blower for drying ammonium sulfate can be saved; realizes the harmless treatment of the regenerated tail gas and the effective recycling of ammonia resources.
In order to achieve the above purpose, the invention is realized by adopting the following technical scheme:
the system for drying ammonium sulfate by utilizing the desulfurization regeneration tail gas comprises a regeneration tower, wherein the bottom of the regeneration tower is provided with a compressed air inlet, and the top of the regeneration tower is provided with a regeneration tail gas outlet; the device also comprises a drying tower, a heater, an ammonium sulfate drying unit, an ammonium sulfate crystallization unit and a cleaning unit; the regeneration tail gas outlet of the regeneration tower is connected with the regeneration tail gas inlet at the lower part of the drying tower through a pipeline, the top of the drying tower is provided with a sulfuric acid spraying device, the upper part of the drying tower is provided with a drying gas outlet, and the bottom of the drying tower is provided with an air supplementing inlet and a sulfuric acid outlet; the drying gas outlet of the drying tower is sequentially connected with the heater and the ammonium sulfate drying unit through a pipeline, and the sulfuric acid outlet of the drying tower is connected with the sulfuric acid inlet of the ammonium sulfate crystallization unit through a pipeline; the aqueous ammonium sulfate outlet of the ammonium sulfate crystallization unit is connected with the aqueous ammonium sulfate inlet of the ammonium sulfate drying unit through a pipeline; the ammonium sulfate drying unit is provided with a product ammonium sulfate outlet and a drying tail gas outlet; the drying tail gas outlet is connected with the drying tail gas inlet of the cleaning unit through a pipeline, the cleaning unit is provided with a cleaning water inlet, a clean gas outlet and an ammonium sulfate solution outlet, and the ammonium sulfate solution outlet is connected with the ammonium sulfate solution inlet of the ammonium sulfate crystallization unit through a pipeline.
And a split gas outlet is arranged on a pipeline between the drying tail gas outlet of the ammonium sulfate drying unit and the drying tail gas inlet of the cleaning unit, and is connected with the drying gas inlet at the lower part of the drying tower through a pipeline.
Compared with the prior art, the invention has the beneficial effects that:
1) The sulfuric acid required for producing the ammonium sulfate is utilized to remove the escaping ammonia in the desulfurization regeneration tail gas, so that the regeneration tail gas is effectively treated, ammonia resources are recovered, and the ammonium sulfate yield is increased;
2) The heat is provided for drying by effectively utilizing the exothermic reaction and the dilution heat of sulfuric acid, and excessive supplementary heat is not needed, so that the requirements of energy conservation and environmental protection are met;
3) The regenerated tail gas and the water in the air are absorbed by the sulfuric acid required by producing the ammonium sulfate, so that the water quantity required for supplementing in order to maintain the water balance of the whole system is saved.
Drawings
Fig. 1 is a block diagram of a system for drying ammonium sulfate using desulfurization regeneration tail gas according to an embodiment of the present invention.
Fig. 2 is a block diagram of a system for drying ammonium sulfate using desulfurization regeneration tail gas according to a second embodiment of the present invention.
In the figure: 1. regeneration tower 2, drying tower 3, heater 4, ammonium sulfate drying unit 5, ammonium sulfate crystallization unit 6, cleaning unit
Detailed Description
The following is a further description of embodiments of the invention, taken in conjunction with the accompanying drawings:
the invention relates to a system for drying ammonium sulfate by utilizing desulfurization regeneration tail gas, which comprises a regeneration tower 1, wherein the bottom of the regeneration tower 1 is provided with a compressed air inlet, and the top of the regeneration tower 1 is provided with a regeneration tail gas outlet; the device also comprises a drying tower 2, a heater 3, an ammonium sulfate drying unit 4, an ammonium sulfate crystallization unit 5 and a cleaning unit 6; the regeneration tail gas outlet of the regeneration tower 1 is connected with the regeneration tail gas inlet at the lower part of the drying tower 2 through a pipeline, the top of the drying tower 2 is provided with a sulfuric acid spraying device, the upper part is provided with a drying gas outlet, and the bottom is provided with an air supplementing inlet and a sulfuric acid outlet; the drying gas outlet of the drying tower 2 is sequentially connected with the heater 3 and the ammonium sulfate drying unit 4 through a pipeline, and the sulfuric acid outlet of the drying tower 2 is connected with the sulfuric acid inlet of the ammonium sulfate crystallization unit 5 through a pipeline; the aqueous ammonium sulfate outlet of the ammonium sulfate crystallization unit 5 is connected with the aqueous ammonium sulfate inlet of the ammonium sulfate drying unit 4 through a pipeline; the ammonium sulfate drying unit 4 is provided with a product ammonium sulfate outlet and a drying tail gas outlet; the drying tail gas outlet is connected with the drying tail gas inlet of the cleaning unit 6 through a pipeline, the cleaning unit 6 is provided with a cleaning water inlet, a clean gas outlet and an ammonium sulfate solution outlet, and the ammonium sulfate solution outlet is connected with the ammonium sulfate solution inlet of the ammonium sulfate crystallization unit 5 through a pipeline.
A split gas outlet is arranged on a pipeline between the drying tail gas outlet of the ammonium sulfate drying unit 4 and the drying tail gas inlet of the cleaning unit 6, and the split gas outlet is connected with the drying gas inlet at the lower part of the drying tower 2 through a pipeline.
The process of the system for drying ammonium sulfate by utilizing the desulfurization regeneration tail gas comprises the following steps of:
1) Introducing desulfurization rich liquid into the bottom of a regeneration tower 1 of the ammonia wet oxidation desulfurization system, and simultaneously introducing compressed air of 0.4-0.6 MPa into the bottom of the regeneration tower 1 to perform oxidation reaction, so that the desulfurization rich liquid is regenerated; the compressed air provides oxygen for the oxidation reaction, the regenerated desulfurization lean solution is discharged from the upper part of the regeneration tower 1 and returns to the ammonia wet oxidation desulfurization system for recycling;
2) The compressed air floats sulfur foam through the blast intensity, the sulfur foam overflows from the top of the regeneration tower 1 and enters a subsequent sulfur or sulfuric acid production system; the regenerated tail gas is discharged from the top of the regeneration tower 1, and simultaneously ammonia and water in the desulfurizing liquid are carried out; the ammonia content in the regenerated tail gas is 2-4 g/m < 3 >, and the water vapor is saturated; the regenerated tail gas is sent into a drying tower 2 through self pressure;
3) In the drying tower 2, the regenerated tail gas is in countercurrent contact with concentrated sulfuric acid sprayed from the tower top, ammonia in the regenerated tail gas is absorbed, and meanwhile, the regenerated tail gas is dried to form dry gas; air is supplemented to the bottom of the drying tower 2, and concentrated sulfuric acid at the bottom of the drying tower enters an ammonium sulfate crystallization unit 5; heating the drying gas to 110-130 ℃ by a heat source to generate overheated and unsaturated hot drying gas;
4) Introducing the hot drying gas into an ammonium sulfate drying unit 4 to remove the water content in the wet ammonium sulfate with the water content of less than 2% sent by an ammonium sulfate crystallization unit 5, wherein the water content of the final product ammonium sulfate is less than 0.2%;
5) The dry tail gas after drying the ammonium sulfate is discharged into the atmosphere after removing entrained fog drops and ammonium sulfate dust through a cleaning unit 6, and an ammonium sulfate solution formed after washing the dry tail gas in the cleaning unit 6 is returned to the ammonium sulfate crystallization unit 5.
The ammonium sulfate drying unit, the ammonium sulfate crystallization unit and the cleaning unit all adopt the conventional equipment.
The following examples are given by way of illustration of detailed embodiments and specific procedures based on the technical scheme of the present invention, but the scope of the present invention is not limited to the following examples. The methods used in the examples described below are conventional methods unless otherwise specified.
[ example 1 ]
As shown in fig. 1, the process flow for drying ammonium sulfate by using the desulfurization regeneration tail gas is described in this embodiment. The regenerated tail gas comes out of the top of the regeneration tower 1 and enters the drying tower 2, the regenerated tail gas in the drying tower 2 is in countercurrent contact with concentrated sulfuric acid sprayed from the top of the tower, ammonia in the regenerated tail gas is absorbed, and meanwhile, the regenerated tail gas is dried to form dry gas.
Air is supplemented into the bottom of the drying tower 2, and meanwhile, concentrated sulfuric acid at the bottom of the drying tower enters an ammonium sulfate crystallization unit 5. The drying gas is heated to a hot drying gas by the heater 3, and then enters the ammonium sulfate drying unit 4, and the aqueous ammonium sulfate (the water content is less than 2%) sent from the ammonium sulfate crystallization unit 5 is dried, so that a dried ammonium sulfate product is finally formed.
The dry tail gas discharged from the ammonium sulfate drying unit 4 is finally discharged to the atmosphere through the cleaning unit 6. The ammonium sulfate solution formed after washing the dry tail gas in the washing unit 6 is returned to the ammonium sulfate crystallization unit 5.
[ example 2 ]
As shown in fig. 2, the process flow of drying ammonium sulfate by using the desulfurization regeneration tail gas is described in this embodiment. The regenerated tail gas comes out of the top of the regeneration tower 1 and enters the drying tower 2, the regenerated tail gas in the drying tower 2 is in countercurrent contact with concentrated sulfuric acid sprayed from the top of the tower, ammonia in the regenerated tail gas is absorbed, and meanwhile, the regenerated tail gas is dried to form dry gas.
The concentrated sulfuric acid at the bottom of the drying tower 2 enters an ammonium sulfate crystallization unit 5. The drying gas is heated to a hot drying gas by the heater 3, and then enters the ammonium sulfate drying unit 4, and the aqueous ammonium sulfate (the water content is less than 2%) sent from the ammonium sulfate crystallization unit 5 is dried, so that a dried ammonium sulfate product is finally formed.
Part of the drying tail gas discharged from the ammonium sulfate drying unit 4 is used as circulating drying gas to return to the bottom of the drying tower 2, and the other part of the drying tail gas is finally discharged into the atmosphere through the cleaning unit 6. The ammonium sulfate solution formed after washing the dry tail gas in the washing unit 6 is returned to the ammonium sulfate crystallization unit 5.
The foregoing is only a preferred embodiment of the present invention, but the scope of the present invention is not limited thereto, and any person skilled in the art, who is within the scope of the present invention, should make equivalent substitutions or modifications according to the technical scheme of the present invention and the inventive concept thereof, and should be covered by the scope of the present invention.
Claims (2)
1. The system for drying ammonium sulfate by utilizing the desulfurization regeneration tail gas comprises a regeneration tower, wherein the bottom of the regeneration tower is provided with a compressed air inlet, and the top of the regeneration tower is provided with a regeneration tail gas outlet; the device is characterized by further comprising a drying tower, a heater, an ammonium sulfate drying unit, an ammonium sulfate crystallization unit and a cleaning unit; the regeneration tail gas outlet of the regeneration tower is connected with the regeneration tail gas inlet at the lower part of the drying tower through a pipeline, the top of the drying tower is provided with a sulfuric acid spraying device, the upper part of the drying tower is provided with a drying gas outlet, and the bottom of the drying tower is provided with an air supplementing inlet and a sulfuric acid outlet; the drying gas outlet of the drying tower is sequentially connected with the heater and the ammonium sulfate drying unit through a pipeline, and the sulfuric acid outlet of the drying tower is connected with the sulfuric acid inlet of the ammonium sulfate crystallization unit through a pipeline; the aqueous ammonium sulfate outlet of the ammonium sulfate crystallization unit is connected with the aqueous ammonium sulfate inlet of the ammonium sulfate drying unit through a pipeline; the ammonium sulfate drying unit is provided with a product ammonium sulfate outlet and a drying tail gas outlet; the drying tail gas outlet is connected with the drying tail gas inlet of the cleaning unit through a pipeline, the cleaning unit is provided with a cleaning water inlet, a clean gas outlet and an ammonium sulfate solution outlet, and the ammonium sulfate solution outlet is connected with the ammonium sulfate solution inlet of the ammonium sulfate crystallization unit through a pipeline.
2. The system for drying ammonium sulfate by using desulfurization regeneration tail gas according to claim 1, wherein a split gas outlet is arranged on a pipeline between a drying tail gas outlet of the ammonium sulfate drying unit and a drying tail gas inlet of the cleaning unit, and the split gas outlet is connected with a drying gas inlet at the lower part of the drying tower through a pipeline.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201711351522.6A CN107934989B (en) | 2017-12-15 | 2017-12-15 | System for drying ammonium sulfate by utilizing desulfurization regeneration tail gas |
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| CN201711351522.6A CN107934989B (en) | 2017-12-15 | 2017-12-15 | System for drying ammonium sulfate by utilizing desulfurization regeneration tail gas |
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| CN107934989B true CN107934989B (en) | 2023-08-01 |
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| CN108046292B (en) * | 2017-12-15 | 2023-04-11 | 中冶焦耐(大连)工程技术有限公司 | Process for drying ammonium sulfate by using desulfurization regeneration tail gas |
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| CN101985359A (en) * | 2009-07-29 | 2011-03-16 | 中国科学院过程工程研究所 | Method for preparing thiocyanate and sulfate by utilizing desulfuration waste liquor in coking plant |
| CN102181308A (en) * | 2011-03-25 | 2011-09-14 | 建业庆松集团有限公司 | Vacuum potassium carbonate coke oven gas desulfurization-sulfuric acid preparation process and processing system thereof |
| CN103172087A (en) * | 2011-12-26 | 2013-06-26 | 宁波科新化工工程技术有限公司 | Method for preparing sulfuric acid or ammonium sulfate from coal gas wet oxidative desulfurization sulfur pulp |
| WO2014188371A1 (en) * | 2013-05-24 | 2014-11-27 | Saipem S.P.A. | Method and system for recovering ammonium sulphate from a urea plant gas stream |
| CN105600990A (en) * | 2016-01-19 | 2016-05-25 | 天津市碳一有机合成工程设计有限公司 | Method for recycling coke oven gas desulfurization and decyanation waste liquid to reclaim sulfur, ammonium sulfate and catalysts |
| CN207738465U (en) * | 2017-12-15 | 2018-08-17 | 中冶焦耐(大连)工程技术有限公司 | The system for drying sulphur ammonium using desulfurization regeneration tail gas |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US9993770B2 (en) * | 2013-11-11 | 2018-06-12 | Dirk Andrews | Process and apparatus for capturing gaseous ammonia |
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Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101597522A (en) * | 2009-06-29 | 2009-12-09 | 朱春阳 | A kind of desulfuration processing method of coke oven gas and isolated plant thereof |
| CN101985359A (en) * | 2009-07-29 | 2011-03-16 | 中国科学院过程工程研究所 | Method for preparing thiocyanate and sulfate by utilizing desulfuration waste liquor in coking plant |
| CN102181308A (en) * | 2011-03-25 | 2011-09-14 | 建业庆松集团有限公司 | Vacuum potassium carbonate coke oven gas desulfurization-sulfuric acid preparation process and processing system thereof |
| CN103172087A (en) * | 2011-12-26 | 2013-06-26 | 宁波科新化工工程技术有限公司 | Method for preparing sulfuric acid or ammonium sulfate from coal gas wet oxidative desulfurization sulfur pulp |
| WO2014188371A1 (en) * | 2013-05-24 | 2014-11-27 | Saipem S.P.A. | Method and system for recovering ammonium sulphate from a urea plant gas stream |
| CN105600990A (en) * | 2016-01-19 | 2016-05-25 | 天津市碳一有机合成工程设计有限公司 | Method for recycling coke oven gas desulfurization and decyanation waste liquid to reclaim sulfur, ammonium sulfate and catalysts |
| CN207738465U (en) * | 2017-12-15 | 2018-08-17 | 中冶焦耐(大连)工程技术有限公司 | The system for drying sulphur ammonium using desulfurization regeneration tail gas |
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