CN103803583B - System and the control method thereof of ammonia are produced in a kind of ammoniacal liquor evaporation - Google Patents
System and the control method thereof of ammonia are produced in a kind of ammoniacal liquor evaporation Download PDFInfo
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Abstract
A system for ammonia is produced in ammoniacal liquor evaporation, and 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 and is connected with above-mentioned each element: ammoniacal liquor vapo(u)rization system control module is then 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 ammonia flow needed for SCR denitration system from SCR denitration Controlling System.A control method for ammonia is produced in ammoniacal liquor evaporation, and it has five large steps.Present system is simple and reliable for structure, and control method is flexible.
Description
Technical field
The present invention relates to the evaporation of a kind of ammoniacal liquor and produce the system of ammonia and control method thereof, it is applicable to as equipment for denitrifying flue gas provides preparation system and the control method of denitrification reducing agent (ammonia).Belong to SCR (SCR) gas denitrifying technology of environmental technology field.
Background technology
The atmospheric polluting material produced 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, boiler and other equipment (as cement kiln, sinter machine etc.) of many industries (as electric power, chemical industry, iron and steel, cement, waste incineration etc.) set up equipment for denitrifying flue gas one after another.
Current SCR (SCR) denitrating flue gas method, because its efficiency is high, stable performance, is widely used in engineering both domestic and external, becomes the mainstream technology that smoke evacuation tail gas removes oxynitride.SCR denitration system refers under the effect of catalyzer, by spraying into ammonia in flue gas, the reduction of nitrogen oxide in flue gas being become nitrogen G&W, does not cause secondary pollution to environment.For providing ammonia needed for denitrating system, total three kinds, liquefied ammonia, ammoniacal liquor and the urea in its source, ammoniacal liquor prepares the method for ammonia due to ammoniacal liquor wide material sources, low price, material danger is liquid ammonia process for caustic soda purification safety comparatively, and cost of investment and operation energy consumption comparatively Wyler's process is low, be therefore with a wide range of applications.
The method that traditional ammoniacal liquor prepares ammonia is that ammoniacal liquor is warming up to 130 ~ 150 DEG C, thus the ammonia component in ammoniacal liquor and water component is together evaporated.This system owing to having evaporated a large amount of moisture useless to system, thus causes operation energy consumption very high, and econmics comparison is poor; Simultaneously owing to having carried a large amount of water vapour in ammonia secretly, need the strict temperature controlling ammonia outlet, avoid ammonia to condense, corrosion subsequent pipeline and equipment.
Summary of the invention
1, object: the object of this invention is to provide system and control method thereof that ammonia is produced in the evaporation of a kind of ammoniacal liquor.Ammoniacal liquor is in ammoniacal liquor vaporizer, pass through steam heating, be warming up to 60 ~ 90 DEG C, water component now in ammoniacal liquor is not owing to reaching boiling point, steam output is little, ammonia components then due to the rising of temperature, promptly can be evaporated, and is sent to SCR (SCR) flue gas denitrification system.Weak ammonia after evaporation is then by a steam separator, the gas at top returns the gas phase of ammoniacal liquor vaporizer, and the isolated weak ammonia in bottom then discharges 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, technical scheme of the present invention realizes as follows:
(1) system of 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 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, 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 the gas phase of ammoniacal liquor vaporizer by N7 interface, the weak ammonia of bottom then discharges 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 then 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 ammonia flow needed for SCR denitration 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 determined 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 armouring); 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 for ammonia is produced in ammoniacal liquor evaporation, and the concrete control method of the method is:
Step one: by regulating the aperture of ammoniacal liquor variable valve A1, adjustment enters the ammoniacal liquor flow of ammoniacal liquor vaporizer, thus the indicating value controlling ammonia outlet pressure unit P is stablized.If ammonia outlet pressure is lower than set(ting)value, then increase the aperture of ammoniacal liquor variable valve A1, thus increase the inlet of ammoniacal liquor; If ammonia outlet pressure is higher than set(ting)value, then reduce the aperture of ammoniacal liquor variable valve A1, thus reduce the inlet of ammoniacal liquor.
Step 2: by the aperture of steam regulation variable valve A2, adjustment enters the steam flow of ammoniacal liquor vaporizer, thus the indicating value controlling ammonia temperature meter T is stablized.If ammonia temperature is lower than set(ting)value, then increase the aperture of steam regulating valve A2, thus increase the inlet of steam; If ammonia temperature is higher than set(ting)value, then reduce the aperture of steam regulating valve A2, thus reduce the inlet of steam.
Step 3: the set(ting)value of ammonia outlet under meter F is obtained by SCR (SCR) denitrating flue gas Controlling System.By regulating the aperture of ammonia outlet variable valve A3, obtain the ammonia flow needed for SCR (SCR) flue gas denitrification system.If ammonia flow is lower than set(ting)value, then increase the aperture of ammonia outlet variable valve A3, thus increase ammonia flow; If ammonia flow is higher than set(ting)value, then reduce the aperture of ammonia outlet variable valve A3, thus reduce ammonia flow.
Step 4: the liquid level of ammoniacal liquor vaporizer is by N6 Interface Controller.N6 interface is positioned at the middle part of ammoniacal liquor vaporizer, and when liquid level is higher than N6 interface, ammoniacal liquor is discharged after steam separator by the mode of overflow, thus maintains the level stability in ammoniacal liquor vaporizer.
Step 5: the discharge of steam drainage is that steam trap realizes automatically.By steam trap, outside steam condensate discharge system, steam then 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 obtains from SCR denitration Controlling System.
Wherein, the mass concentration of discharging weak ammonia described in above-mentioned control method is 0.1 ~ 5%.
3, advantage and effect: present system is simple and reliable for structure, 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, therefore greatly reduces the steam consumption quantity of system, thus greatly reduce working cost.Simultaneously because the vapour content in ammonia reduces, therefore greatly reduce the dew point corrosion risk in subsequent pipeline and equipment.By product of the present invention 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.
Accompanying drawing explanation
Fig. 1 is present system structural representation;
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 present invention will be further described.
(1) referring to Fig. 1, the system of 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 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, 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 carrying 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 measure ammoniacal liquor vaporizer 1. in the temperature of ammoniacal liquor; 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 gas at steam separator 5. top returns ammoniacal liquor vaporizer gas phase 1. by N7 interface, and the weak ammonia of bottom then discharges 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 then 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 ammonia flow needed for SCR denitration 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 determined 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 armouring); 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 for ammonia is produced in ammoniacal liquor evaporation, and the concrete control method of the method is:
A) by regulating ammoniacal liquor variable valve A1 aperture 2., adjustment enters ammoniacal liquor vaporizer ammoniacal liquor flow 1., thus it is stable to control ammonia outlet pressure unit P indicating value 6..If ammonia outlet pressure is lower than set(ting)value, then increase ammoniacal liquor variable valve A1 aperture 2., thus increase the inlet of ammoniacal liquor; If ammonia outlet pressure is higher than set(ting)value, then reduce ammoniacal liquor variable valve A1 aperture 2., thus reduce the inlet of ammoniacal liquor.
B) by steam regulation variable valve A2 aperture 3., adjustment enters ammoniacal liquor vaporizer steam flow 1., thus it is stable to control ammonia temperature meter T indicating value 7..If ammonia temperature is lower than set(ting)value, then increase steam regulating valve A2 aperture 3., thus increase the inlet of steam; If ammonia temperature is higher than set(ting)value, then reduce steam regulating valve A2 aperture 3., thus reduce the inlet of 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 ammonia flow needed for SCR (SCR) flue gas denitrification system.If ammonia flow is lower than set(ting)value, then increase ammonia outlet variable valve A3 aperture 4., thus increase ammonia flow; If ammonia flow is higher than set(ting)value, then reduce ammonia outlet variable valve A3 aperture 4., thus reduce ammonia flow.
D) ammoniacal liquor vaporizer liquid level is 1. by N6 Interface Controller.N6 interface is positioned at the middle part of ammoniacal liquor vaporizer, when liquid level is higher than N6 interface, the 1. inner weak ammonia of ammoniacal liquor vaporizer by the mode of overflow through steam separator 5. after discharge, thus maintain ammoniacal liquor vaporizer 1. in level stability.
E) discharge of steam drainage is that 9. steam trap realizes automatically.By steam trap 9., outside steam condensate discharge system, steam then 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 obtains from SCR denitration Controlling System.
Wherein, the mass concentration of discharging weak ammonia described in above-mentioned control method is 0.1 ~ 5%.
Claims (5)
1. a system for ammonia is produced in 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; Ammoniacal liquor vaporizer is provided with 7 interfaces: N1 interface connects ammoniacal liquor inlet pipeline, and for 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, 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, for outwards discharging the weak ammonia after evaporation, weak ammonia outlet conduit is provided with steam separator, the gas at steam separator top returns the gas phase of ammoniacal liquor vaporizer by N7 interface, the weak ammonia of bottom then discharges 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 then 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 ammonia flow needed for SCR denitration 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 determined 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 two explosion-proof type PT100 armoured Pt thermal resistances; 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.
2. a control method for ammonia is produced in ammoniacal liquor evaporation, it is characterized in that: the concrete control method of the method is:
Step one: by regulating the aperture of ammoniacal liquor variable valve A1, adjustment enters the ammoniacal liquor flow of ammoniacal liquor vaporizer, thus the indicating value controlling ammonia outlet pressure unit P is stablized; If ammonia outlet pressure is lower than set(ting)value, then increase the aperture of ammoniacal liquor variable valve A1, thus increase the inlet of ammoniacal liquor; If ammonia outlet pressure is higher than set(ting)value, then reduce the aperture of ammoniacal liquor variable valve A1, thus reduce the inlet of ammoniacal liquor;
Step 2: by the aperture of steam regulation variable valve A2, adjustment enters the steam flow of ammoniacal liquor vaporizer, thus the indicating value controlling ammonia temperature meter T is stablized; If ammonia temperature is lower than set(ting)value, then increase the aperture of steam regulating valve A2, thus increase the inlet of steam; If ammonia temperature is higher than set(ting)value, then reduce the aperture of steam regulating valve A2, thus reduce the inlet of steam;
Step 3: the set(ting)value of ammonia outlet under meter F is obtained by SCR SCR denitrating flue gas Controlling System; By regulating the aperture of ammonia outlet variable valve A3, obtain the ammonia flow needed for SCR SCR flue gas denitrification system; If ammonia flow is lower than set(ting)value, then increase the aperture of ammonia outlet variable valve A3, thus increase ammonia flow; If ammonia flow is higher than set(ting)value, then reduce the aperture of ammonia outlet variable valve A3, thus reduce ammonia flow;
Step 4: the liquid level of ammoniacal liquor vaporizer is by N6 Interface Controller; N6 interface is positioned at the middle part of ammoniacal liquor vaporizer, and when liquid level is higher than N6 interface, ammoniacal liquor is discharged after steam separator by the mode of overflow, thus maintains the level stability in ammoniacal liquor vaporizer;
Step 5: the discharge of steam drainage is that steam trap realizes automatically; By steam trap, outside steam condensate discharge system, steam then continues to stay heat exchange in ammoniacal liquor vaporizer;
Ammonia outlet pressure set points described in this control method is 0.1 ~ 0.4MPa.
3. the control method of ammonia is produced in a kind of ammoniacal liquor evaporation according to claim 2, it is characterized in that: the ammonia temperature set(ting)value described in this control method is 60 ~ 90 DEG C.
4. the control method of ammonia is produced in a kind of ammoniacal liquor evaporation according to claim 2, it is characterized in that: the ammonia flow set(ting)value described in this control method obtains from SCR denitration Controlling System.
5. the control method of ammonia is produced in a kind of ammoniacal liquor evaporation according to claim 2, it is characterized in that: the mass concentration of discharging weak ammonia described in this control method is 0.1 ~ 5%.
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| CN106006672B (en) * | 2016-05-26 | 2019-05-24 | 隆达电子股份有限公司 | Ammonia density lifting system and its method |
| CN106696028B (en) * | 2016-12-28 | 2018-04-17 | 江苏天舒电器股份有限公司 | A kind of control method of the double air-flow ammonium hydroxide fumigation systems of wooden colour developing |
| CN106625953B (en) * | 2016-12-28 | 2018-04-17 | 江苏天舒电器股份有限公司 | A kind of wooden colour developing pair air-flow ammonium hydroxide fumigation system and its equipment |
| CN110963507A (en) * | 2019-12-30 | 2020-04-07 | 北京华电光大环境股份有限公司 | Ammonia water ammonia production system and process for coke oven flue gas denitration |
| CN112870949B (en) * | 2021-01-05 | 2021-10-29 | 福建省福能龙安热电有限公司 | Denitration method and device for heating ammonia water to generate ammonia gas |
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| CN202529862U (en) * | 2012-05-10 | 2012-11-14 | 毕节金河化工有限公司 | Negative pressure generating device for synthesis ammonia vaporization system |
| CN202609957U (en) * | 2012-05-11 | 2012-12-19 | 山东洪达化工有限公司 | Device for solving low temperature of ammonia still for recovering medium-pressure ammonia in synthesis ammonia |
| CN203715292U (en) * | 2014-03-12 | 2014-07-16 | 北京博智伟德环保科技有限公司 | System for producing ammonia gas by evaporation of ammonium hydroxide |
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| KR20130138377A (en) * | 2012-06-11 | 2013-12-19 | 주식회사녹색기술단 | Method and apparatus for recovering high concentration ammonia water from wastewater containing ammonia |
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Patent Citations (3)
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|---|---|---|---|---|
| CN202529862U (en) * | 2012-05-10 | 2012-11-14 | 毕节金河化工有限公司 | Negative pressure generating device for synthesis ammonia vaporization system |
| CN202609957U (en) * | 2012-05-11 | 2012-12-19 | 山东洪达化工有限公司 | Device for solving low temperature of ammonia still for recovering medium-pressure ammonia in synthesis ammonia |
| CN203715292U (en) * | 2014-03-12 | 2014-07-16 | 北京博智伟德环保科技有限公司 | System for producing ammonia gas by evaporation of ammonium hydroxide |
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Effective date of registration: 20170110 Address after: 100084 Beijing, Zhongguancun, North Street, building 123, building five, level 2508, 64, Patentee after: Beijing Ledao Zhiyuan Technology Co. Ltd. Address before: 100084 Beijing, Zhongguancun, North Street, building 2108, room 64, room 123, No. Patentee before: Beijing Bo Zhi Wade Environmental Protection Technology Co., Ltd |
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