CN203715292U - System for producing ammonia gas by evaporation of ammonium hydroxide - Google Patents
System for producing ammonia gas by evaporation of ammonium hydroxide Download PDFInfo
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- CN203715292U CN203715292U CN201420111107.9U CN201420111107U CN203715292U CN 203715292 U CN203715292 U CN 203715292U CN 201420111107 U CN201420111107 U CN 201420111107U CN 203715292 U CN203715292 U CN 203715292U
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- ammoniacal liquor
- ammonia
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Abstract
The utility model discloses a system for producing an ammonia gas by evaporation of ammonium hydroxide. The system comprises an ammonium hydroxide evaporator, an ammonium hydroxide adjusting valve A1, a steam regulating valve A2, an ammonium gas outlet adjusting valve A3, a steam-water separator, an ammonium gas outlet pressure transmitter P, an ammonium hydroxide thermometer T, an ammonium gas outlet flow meter F, a steam hydrophobic valve and an ammonium hydroxide evaporation system control module; seven ports are formed in the ammonium hydroxide evaporator and connected with all the elements; the ammonium hydroxide evaporation control system is respectively connected with the ammonium hydroxide adjusting valve A1, the steam adjusting valve A2, the ammonium gas outlet adjusting valve A3, the ammonia gas outlet pressure transmitter P, the ammonium hydroxide thermometer T and the ammonium gas outlet flow meter F through cables; meanwhile, the ammonium hydroxide evaporation system control module is connected with an SCR (Selective Catalytic Reduction) denitration control system through a communication cable; the required ammonium gas flow of the SCR denitration system is obtained from the SCR denitration control system. The system disclosed by the utility model is simple and reliable in structure, and flexible and convenient to control.
Description
Technical field
The utility model relates to the system that ammonia is produced in the evaporation of a kind of ammoniacal liquor, and it is applicable to provide for equipment for denitrifying flue gas the preparation system of denitrification reducing agent (ammonia).Belong to SCR (SCR) gas denitrifying technology of environmental technology field.
Background technology
The atmospheric polluting material producing after coal combustion mainly contains sulfurous gas, oxynitride, flue dust (pellet) and the carbonic acid gas as greenhouse gases.Due to coal fire discharged and vehicular emission, the pollution of the oxynitride of China is very serious.
In recent years, along with the raising gradually of environmental requirement, in order to reduce the quantity discharged of smoke evacuation nitrogen oxide in tail gas, the boiler of many industries (as electric power, chemical industry, iron and steel, cement, waste incineration etc.) and other equipment (as cement kiln, sinter machine etc.) are set up equipment for denitrifying flue gas one after another.
At present SCR (SCR) denitrating flue gas method, because its efficiency is high, stable performance, is widely used in engineering both domestic and external, becomes smoke evacuation tail gas and remove the mainstream technology of oxynitride.SCR denitrating system refers under the effect of catalyzer, by spray into ammonia in flue gas, the reduction of nitrogen oxide in flue gas is become to nitrogen G&W, and environment is not caused to secondary pollution.For providing denitrating system required ammonia, three kinds, its total liquefied ammonia in source, ammoniacal liquor and urea, ammoniacal liquor is prepared the method for ammonia due to ammoniacal liquor wide material sources, low price, material danger is compared with liquid ammonia process for caustic soda purification safety, and cost of investment and operation energy consumption are low compared with Wyler's process, are therefore with a wide range of applications.
The method that traditional ammoniacal liquor is prepared ammonia is that ammoniacal liquor is warming up to 130～150 DEG C, thereby ammonia component and water component in ammoniacal liquor are together evaporated.This system is owing to having evaporated a large amount of moisture useless to system, thereby causes operation energy consumption very high, and economy is poor; Owing to having carried a large amount of water vapour in ammonia secretly, need the strict temperature of controlling ammonia outlet simultaneously, avoid ammonia dewfall, corrode follow-up pipeline and equipment.
Utility model content
1, object: the purpose of this utility model is to provide the system that ammonia is produced in a kind of ammoniacal liquor evaporation.Ammoniacal liquor is in ammoniacal liquor vaporizer, pass through steam heating, be warming up to 60～90 DEG C, now the water component in ammoniacal liquor is owing to not reaching boiling point, steam output is little, ammonia components can, due to the rising of temperature, promptly be evaporated, and is sent to SCR (SCR) flue gas denitrification system.Weak ammonia after evaporation is by a steam separator, the gas at top returns to the gas phase of ammoniacal liquor vaporizer, and the isolated weak ammonia in bottom is discharged system, can be used for selective non-catalytic reduction (SNCR) flue gas denitrification system, or for desulphurization system, non-secondary pollution produces.
2, technical scheme: in order to reach foregoing invention object, the technical solution of the utility model realizes as follows:
(1) system that ammonia is produced in a kind of ammoniacal liquor evaporation, it is characterized in that, it comprises ammoniacal liquor vaporizer, ammoniacal liquor variable valve A1, steam regulating valve A2, ammonia outlet variable valve A3, steam separator, ammonia outlet pressure unit P, ammonia temperature meter T, ammonia outlet under meter F, steam trap and ammoniacal liquor vapo(u)rization system control module, sees Fig. 1.Position annexation between them is: ammoniacal liquor vaporizer is provided with 7 interfaces: N1 interface connects ammoniacal liquor inlet pipeline, and for the ammoniacal liquor of supplying raw materials to ammonia vapor device, ammoniacal liquor inlet pipeline is provided with ammoniacal liquor variable valve A1; N2 interface connects steam inlet pipeline, and for providing thermal source to ammoniacal liquor vaporizer, vapor interface pipeline is provided with steam regulating valve A2; N3 interface connects ammonia outlet pipeline, and for outwards carrying ammonia, ammonia outlet pipeline is provided with ammonia outlet variable valve A3, ammonia outlet pressure unit P and ammonia outlet under meter F; N4 interface connects vapour outlet pipeline, and for discharging steam drainage, vapour outlet pipeline is provided with steam trap; N5 interface connects ammonia temperature meter T, for measuring the temperature of ammoniacal liquor in ammoniacal liquor vaporizer; N6 interface connects weak ammonia outlet conduit, and for outwards discharging the weak ammonia after evaporation, weak ammonia outlet conduit is provided with steam separator, and the gas at steam separator top returns to the gas phase of ammoniacal liquor vaporizer by N7 interface, and the weak ammonia of bottom is discharged system.N7 interface position, higher than the liquid level of ammoniacal liquor vaporizer, connects the gas phase of ammoniacal liquor vaporizer.
Ammoniacal liquor vapo(u)rization system control module is connected with ammoniacal liquor variable valve A1, steam regulating valve A2, ammonia outlet variable valve A3, ammonia outlet pressure unit P, ammonia temperature meter T and ammonia outlet under meter F respectively by cable.This ammoniacal liquor vapo(u)rization system control module is connected by communication cable with SCR denitration Controlling System simultaneously, obtains the required ammonia flow of SCR denitrating system from SCR denitration Controlling System.
This ammoniacal liquor vaporizer is vertical heat exchanger, and thermal source adopts superheated vapour or saturation steam, and inside is provided with shell and tube steam heating tube, and the heat interchanging area of steam heating tube is definite according to exerting oneself of ammoniacal liquor vaporizer; This ammoniacal liquor variable valve A1, steam regulating valve A2 and ammonia outlet variable valve A3 are the pneumatic or motor-driven control valve of explosion-proof type; This steam separator is mechanical type gas-liquid separator; Ammonia outlet pressure unit P is Anti-explosion intelligent pressure unit; This ammonia temperature meter T is explosion-proof type PT100 type platinum resistance thermometer sensor, (two armourings); This ammonia outlet under meter F is explosion-proof type Coriolis flowmeter; This steam trap is free floating-ball type steam draining valve; Ammoniacal liquor vapo(u)rization system control module adopts PLC or DCS Controlling System.
(2) control method that ammonia is produced in ammoniacal liquor evaporation, the concrete control method of the method is:
Step 1: by regulating the aperture of ammoniacal liquor variable valve A1, adjust the ammoniacal liquor flow that enters ammoniacal liquor vaporizer, thereby the indicating value of control ammonia outlet pressure unit P is stable.If ammonia outlet pressure, lower than set(ting)value, increases the aperture of ammoniacal liquor variable valve A1, thus the inlet of increase ammoniacal liquor; If ammonia outlet pressure, higher than set(ting)value, reduces the aperture of ammoniacal liquor variable valve A1, thus the inlet of minimizing ammoniacal liquor.
Step 2: by the aperture of steam regulation variable valve A2, adjust the steam flow that enters ammoniacal liquor vaporizer, thereby the indicating value of control ammonia temperature meter T is stable.If ammonia temperature, lower than set(ting)value, increases the aperture of steam regulating valve A2, thus the inlet of increase steam; If ammonia temperature, higher than set(ting)value, reduces the aperture of steam regulating valve A2, thus the inlet of minimizing steam.
Step 3: the set(ting)value of ammonia outlet under meter F obtains by SCR (SCR) denitrating flue gas Controlling System.By regulating the aperture of ammonia outlet variable valve A3, obtain the required ammonia flow of SCR (SCR) flue gas denitrification system.If ammonia flow, lower than set(ting)value, increases the aperture of ammonia outlet variable valve A3, thereby increase ammonia flow; If ammonia flow, higher than set(ting)value, reduces the aperture of ammonia outlet variable valve A3, thereby reduce ammonia flow.
Step 4: the liquid level of ammoniacal liquor vaporizer is by the control of N6 interface.N6 interface is positioned at the middle part of ammoniacal liquor vaporizer, and when liquid level is during higher than N6 interface, ammoniacal liquor is discharged after steam separator by the mode of overflow, thereby has kept the level stability in ammoniacal liquor vaporizer.
Step 5: the discharge of steam drainage is that steam trap is realized automatically.By steam trap, outside steam condensate discharge system, steam continues to stay heat exchange in ammoniacal liquor vaporizer.
Wherein, the ammonia outlet pressure set points described in above-mentioned control method is 0.1～0.4MPa.
Wherein, the ammonia temperature set(ting)value described in above-mentioned control method is 60～90 DEG C.
Wherein, the ammonia flow set(ting)value described in above-mentioned control method is obtained from SCR denitration Controlling System.
The mass concentration of wherein, discharging weak ammonia described in above-mentioned control method is 0.1～5%.
3, advantage and effect: the utility model system architecture is simple and reliable, controls flexible.Due in the process of evaporation ammonia, ammonia temperature remains on below boiling point, therefore only has the water of minute quantity to be evaporated, and has therefore greatly reduced the steam consumption quantity of system, thereby has greatly reduced working cost.Because the vapour content in ammonia reduces, therefore greatly reduced the dew point corrosion risk in follow-up pipeline and equipment simultaneously.By product of the present utility model is weak ammonia, and mass concentration is about 0.1～5%, can be used for selective non-catalytic reduction (SNCR) flue gas denitrification system, or for desulphurization system, therefore non-secondary pollution produces.
Brief description of the drawings
Fig. 1 is the utility model system architecture schematic diagram;
In figure, nomenclature is as follows:
1., ammoniacal liquor vaporizer; 2., ammoniacal liquor variable valve A1; 3., steam regulating valve A2; 4., ammonia outlet variable valve A3; 5., steam separator; 6., ammonia outlet pressure unit P; 7., ammonia temperature meter T; 8., ammonia outlet under meter F; 9., steam trap; N1-N7 interface is 7 pipe joint positions that ammoniacal liquor vaporizer is established.
Embodiment
Below in conjunction with the drawings and specific embodiments, the utility model is described further.
(1) referring to Fig. 1, the system that ammonia is produced in a kind of ammoniacal liquor evaporation, it is characterized in that, it comprise ammoniacal liquor vaporizer 1., ammoniacal liquor variable valve A1 2., steam regulating valve A2 3., ammonia outlet variable valve A3 4., steam separator 5., ammonia outlet pressure unit P 6., ammonia temperature meter T 7., ammonia outlet under meter F 8., steam trap 9. with ammoniacal liquor vapo(u)rization system control module.Position annexation between them is: 1. ammoniacal liquor vaporizer is provided with 7 interfaces: N1 interface connects ammoniacal liquor inlet pipeline, and for the ammoniacal liquor of 1. supplying raw materials to ammonia vapor device, 2. ammoniacal liquor inlet pipeline is provided with ammoniacal liquor variable valve A1; N2 interface connects steam inlet pipeline, and for 1. providing thermal source to ammoniacal liquor vaporizer, 3. vapor interface pipeline is provided with steam regulating valve A2; N3 interface connects ammonia outlet pipeline, for outwards carry ammonia, ammonia outlet pipeline be provided with ammonia outlet variable valve A3 4., ammonia outlet pressure unit P 6. with ammonia outlet under meter F 8.; N4 interface connects vapour outlet pipeline, and for discharging steam drainage, 9. vapour outlet pipeline is provided with steam trap; 7. N5 interface connects ammonia temperature meter T, for measuring the 1. temperature of interior ammoniacal liquor of ammoniacal liquor vaporizer; N6 interface connects weak ammonia outlet conduit, for outwards discharging the weak ammonia after evaporation, 5. weak ammonia outlet conduit is provided with steam separator, and the steam separator 5. gas at top returns to ammoniacal liquor vaporizer gas phase 1. by N7 interface, and the weak ammonia of bottom is discharged system.N7 interface position, higher than ammoniacal liquor vaporizer liquid level 1., connects ammoniacal liquor vaporizer gas phase 1..
Ammoniacal liquor vapo(u)rization system control module by cable respectively with ammoniacal liquor variable valve A1 2., steam regulating valve A2 2., ammonia outlet variable valve A3 4., ammonia outlet pressure unit P 6., 8. 7. ammonia temperature meter T be connected with ammonia outlet under meter F.Ammoniacal liquor vapo(u)rization system is connected by communication cable with SCR denitration Controlling System simultaneously, obtains the required ammonia flow of SCR denitrating system from SCR denitration Controlling System.
1. this ammoniacal liquor vaporizer is vertical heat exchanger, and thermal source adopts superheated vapour or saturation steam, and inside is provided with shell and tube steam heating tube, and the heat interchanging area of steam heating tube is definite according to exerting oneself of ammoniacal liquor vaporizer; This ammoniacal liquor variable valve A1 2., 4. 3. steam regulating valve A2 be the pneumatic or motor-driven control valve of explosion-proof type with ammonia outlet variable valve A3; 5. this steam separator is mechanical type gas-liquid separator; 6. ammonia outlet pressure unit P is Anti-explosion intelligent pressure unit; 7. this ammonia temperature meter T is explosion-proof type PT100 type platinum resistance thermometer sensor, (two armourings); 8. this ammonia outlet under meter F is explosion-proof type Coriolis flowmeter; 9. this steam trap is free floating-ball type steam draining valve; Ammoniacal liquor vapo(u)rization system control module adopts PLC or DCS Controlling System.
(2) control method that ammonia is produced in ammoniacal liquor evaporation, the concrete control method of the method is:
A) by regulating ammoniacal liquor variable valve A1 aperture 2., adjust and enter ammoniacal liquor vaporizer ammoniacal liquor flow 1., thereby it is stable to control ammonia outlet pressure unit P indicating value 6..If ammonia outlet pressure lower than set(ting)value, increases ammoniacal liquor variable valve A1 aperture 2., thus the inlet of increase ammoniacal liquor; If ammonia outlet pressure higher than set(ting)value, reduces ammoniacal liquor variable valve A1 aperture 2., thus the inlet of minimizing ammoniacal liquor.
B), by steam regulation variable valve A2 aperture 3., adjust and enter ammoniacal liquor vaporizer steam flow 1., thereby it is stable to control ammonia temperature meter T indicating value 7..If ammonia temperature lower than set(ting)value, increases steam regulating valve A2 aperture 3., thus the inlet of increase steam; If ammonia temperature higher than set(ting)value, reduces steam regulating valve A2 aperture 3., thus the inlet of minimizing steam.
C) ammonia outlet under meter F set(ting)value 8. derives from SCR (SCR) denitrating flue gas Controlling System.By regulating ammonia outlet variable valve A3 aperture 4., obtain the required ammonia flow of SCR (SCR) flue gas denitrification system.If ammonia flow lower than set(ting)value, increases ammonia outlet variable valve A3 aperture 4., thereby increase ammonia flow; If ammonia flow higher than set(ting)value, reduces ammonia outlet variable valve A3 aperture 4., thereby reduce ammonia flow.
D) ammoniacal liquor vaporizer liquid level is 1. by the control of N6 interface.N6 interface is positioned at the middle part of ammoniacal liquor vaporizer, when liquid level is during higher than N6 interface, the ammoniacal liquor vaporizer 1. inner weak ammonia mode by overflow is discharged after 5. through steam separator, thereby has kept 1. interior level stability of ammoniacal liquor vaporizer.
E) discharge of steam drainage is that 9. steam trap is realized automatically.By steam trap 9., outside steam condensate discharge system, steam continues to stay the 1. interior heat exchange of ammoniacal liquor vaporizer.
Wherein, the ammonia outlet pressure set points described in above-mentioned control method is 0.1～0.4MPa.
Wherein, the ammonia temperature set(ting)value described in above-mentioned control method is 60～90 DEG C.
Wherein, the ammonia flow set(ting)value described in above-mentioned control method is obtained from SCR denitration Controlling System.
The mass concentration of wherein, discharging weak ammonia described in above-mentioned control method is 0.1～5%.
Claims (1)
1. the system that ammonia is produced in ammoniacal liquor evaporation, is characterized in that: it comprises ammoniacal liquor vaporizer, ammoniacal liquor variable valve A1, steam regulating valve A2, ammonia outlet variable valve A3, steam separator, ammonia outlet pressure unit P, ammonia temperature meter T, ammonia outlet under meter F, steam trap and ammoniacal liquor vapo(u)rization system control module; Ammoniacal liquor vaporizer is provided with 7 interfaces: N1 interface connects ammoniacal liquor inlet pipeline, and ammoniacal liquor inlet pipeline is provided with ammoniacal liquor variable valve A1; N2 interface connects steam inlet pipeline, and vapor interface pipeline is provided with steam regulating valve A2; N3 interface connects ammonia outlet pipeline, and ammonia outlet pipeline is provided with ammonia outlet variable valve A3, ammonia outlet pressure unit P and ammonia outlet under meter F; N4 interface connects vapour outlet pipeline, and vapour outlet pipeline is provided with steam trap; N5 interface connects ammonia temperature meter T, measures the temperature of ammoniacal liquor in ammoniacal liquor vaporizer; N6 interface connects weak ammonia outlet conduit, weak ammonia outlet conduit is provided with steam separator, the gas at steam separator top returns to the gas phase of ammoniacal liquor vaporizer by N7 interface, the weak ammonia of bottom is discharged system, N7 interface position, higher than the liquid level of ammoniacal liquor vaporizer, connects the gas phase of ammoniacal liquor vaporizer;
Ammoniacal liquor vapo(u)rization system control module is connected with ammoniacal liquor variable valve A1, steam regulating valve A2, ammonia outlet variable valve A3, ammonia outlet pressure unit P, ammonia temperature meter T and ammonia outlet under meter F respectively by cable, this ammoniacal liquor vapo(u)rization system control module is connected by communication cable with SCR denitration Controlling System simultaneously, obtains the required ammonia flow of SCR denitrating system from SCR denitration Controlling System;
This ammoniacal liquor vaporizer is vertical heat exchanger, and thermal source adopts superheated vapour or saturation steam, and inside is provided with shell and tube steam heating tube, and the heat interchanging area of steam heating tube is definite according to exerting oneself of ammoniacal liquor vaporizer; This ammoniacal liquor variable valve A1, steam regulating valve A2 and ammonia outlet variable valve A3 are the pneumatic or motor-driven control valve of explosion-proof type; This steam separator is mechanical type gas-liquid separator; Ammonia outlet pressure unit P is Anti-explosion intelligent pressure unit; This ammonia temperature meter T is explosion-proof type PT100 type platinum resistance thermometer sensor; This ammonia outlet under meter F is explosion-proof type Coriolis flowmeter; This steam trap is free floating-ball type steam draining valve; This ammoniacal liquor vapo(u)rization system control module adopts PLC or DCS Controlling System.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420111107.9U CN203715292U (en) | 2014-03-12 | 2014-03-12 | System for producing ammonia gas by evaporation of ammonium hydroxide |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420111107.9U CN203715292U (en) | 2014-03-12 | 2014-03-12 | System for producing ammonia gas by evaporation of ammonium hydroxide |
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| CN203715292U true CN203715292U (en) | 2014-07-16 |
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| CN201420111107.9U Expired - Fee Related CN203715292U (en) | 2014-03-12 | 2014-03-12 | System for producing ammonia gas by evaporation of ammonium hydroxide |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103803583A (en) * | 2014-03-12 | 2014-05-21 | 北京博智伟德环保科技有限公司 | System for producing ammonia gas by ammonia water evaporation and control method thereof |
| CN106006671A (en) * | 2016-05-19 | 2016-10-12 | 隆达电子股份有限公司 | Ammonia concentration increasing device and method |
| CN107596917A (en) * | 2017-09-29 | 2018-01-19 | 浙江省环境保护科学设计研究院 | The SNCR SCR combined apparatus and technique of cement clinker production line kiln exit gas |
| CN107899411A (en) * | 2017-09-29 | 2018-04-13 | 浙江省环境保护科学设计研究院 | A kind of SCR reaction units and method for the processing of cement clinker production line kiln exit gas |
-
2014
- 2014-03-12 CN CN201420111107.9U patent/CN203715292U/en not_active Expired - Fee Related
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103803583A (en) * | 2014-03-12 | 2014-05-21 | 北京博智伟德环保科技有限公司 | System for producing ammonia gas by ammonia water evaporation and control method thereof |
| CN103803583B (en) * | 2014-03-12 | 2015-09-16 | 北京博智伟德环保科技有限公司 | System and the control method thereof of ammonia are produced in a kind of ammoniacal liquor evaporation |
| CN106006671A (en) * | 2016-05-19 | 2016-10-12 | 隆达电子股份有限公司 | Ammonia concentration increasing device and method |
| CN107596917A (en) * | 2017-09-29 | 2018-01-19 | 浙江省环境保护科学设计研究院 | The SNCR SCR combined apparatus and technique of cement clinker production line kiln exit gas |
| CN107899411A (en) * | 2017-09-29 | 2018-04-13 | 浙江省环境保护科学设计研究院 | A kind of SCR reaction units and method for the processing of cement clinker production line kiln exit gas |
| CN107596917B (en) * | 2017-09-29 | 2019-11-26 | 浙江省环境保护科学设计研究院 | The SNCR-SCR combined apparatus and technique of cement clinker production line kiln exit gas |
| CN107899411B (en) * | 2017-09-29 | 2019-11-26 | 浙江省环境保护科学设计研究院 | A kind of SCR reaction unit and method for the processing of cement clinker production line kiln exit gas |
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| C14 | Grant of patent or utility model | ||
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| CF01 | Termination of patent right due to non-payment of annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20140716 Termination date: 20160312 |